CA1333376C - Method of continuously carbonizing a mixture of primarily organic waste material - Google Patents
Method of continuously carbonizing a mixture of primarily organic waste materialInfo
- Publication number
- CA1333376C CA1333376C CA000613928A CA613928A CA1333376C CA 1333376 C CA1333376 C CA 1333376C CA 000613928 A CA000613928 A CA 000613928A CA 613928 A CA613928 A CA 613928A CA 1333376 C CA1333376 C CA 1333376C
- Authority
- CA
- Canada
- Prior art keywords
- barrel
- region
- mixer
- vent
- shafts
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000000463 material Substances 0.000 title claims abstract description 412
- 238000000034 method Methods 0.000 title claims abstract description 51
- 238000010000 carbonizing Methods 0.000 title claims abstract description 27
- 239000000203 mixture Substances 0.000 title claims abstract description 25
- 239000010815 organic waste Substances 0.000 title claims abstract description 18
- 238000011049 filling Methods 0.000 claims abstract description 26
- 239000003039 volatile agent Substances 0.000 claims abstract description 24
- 239000011368 organic material Substances 0.000 claims abstract description 16
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 15
- 238000002156 mixing Methods 0.000 claims description 33
- 238000013022 venting Methods 0.000 claims description 24
- 238000012546 transfer Methods 0.000 claims description 20
- 230000008569 process Effects 0.000 claims description 19
- 239000002699 waste material Substances 0.000 claims description 17
- 239000004033 plastic Substances 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 12
- 230000015572 biosynthetic process Effects 0.000 claims description 10
- 238000011144 upstream manufacturing Methods 0.000 claims description 10
- 230000008016 vaporization Effects 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 239000002023 wood Substances 0.000 claims description 6
- 238000003763 carbonization Methods 0.000 claims description 2
- 239000005539 carbonized material Substances 0.000 claims description 2
- 239000000047 product Substances 0.000 description 28
- 239000003245 coal Substances 0.000 description 7
- 239000000123 paper Substances 0.000 description 7
- 238000012545 processing Methods 0.000 description 7
- 239000002184 metal Substances 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 238000000280 densification Methods 0.000 description 5
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 239000002801 charged material Substances 0.000 description 3
- 230000006837 decompression Effects 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000012809 cooling fluid Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000013529 heat transfer fluid Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
Abstract
A method of continuously carbonizing a mixture of primarily organic waste material to a high British Thermal Unit char product wherein a stream of comminuted garbage material with a substantial organic material content is fed to one end of a mixer barrel, the material is compressed to form a barrel filling mass functioning as a first vapor block, and the work energy required to compress it and squeeze out entrapped air is used virtually exclusively to raise the temperature of the material adiabatically, air and any steam created are vented, the material downstream from the first vapor block is decompressed in a second vent region, the material is recompressed in the absence of air to form another vapor block, while exclusively utilizing the work energy required to compress it to raise the temperature of the material adiabatically to a volatile releasing temperature in the neighborhood of 400°F. to 600°F. and to carbonize the material, the volatiles are vented, and the product is discharged as a dry, friable particulate char.
Description
AN IMPROVED METHOD OF CONTI~UOUSLY CARBONIZING
A MIXTURE OF PRIMARILY ORGANIC WASTE MATERIAL
The present invention is concerned with an improved method of destructively distilling comminuted mixtures of primarily organic waste materials, which includes paper, garbage, and other refuse material and reducing them to a useful, combustible friable char product, which can be mixed with coal particles, for example, and usefully burned by utility companies and the like to produce electrical power.
- The method to be disclosed involves certain novel, useful and unobvious improvements in processes which have been proposed for converting organic waste material to a char material, such as the processes disclosed in United States patents 4,098,649; 4,123,332; and 4,308,103. The conversion of industrial and municipal waste by incinerating it in conven-tional incinerators and/or burying it in landfill areas is no longer viable for the future. The conventional incineration of the material releases fumes and smoke to the atmosphere which are objectionable, and cause pollution problems. Moreover, presently practiced incineration is expensive and does not re`sult in the recovery of any useful products which can offset the cost of incineration. The burying of waste in landfill areas is also unsatisfactory in this society in view of the tremendous volumes of waste which are generated nationwide, and the scarcity of landfill areas which, afterward are no longer useful for most other purposes.
Prior art methods, such as the method disclosed in patent 4,098,649, have initially separated the trash into organic and inorganic materials. Principally, this division of the trash or refuse has resulted in the separation of the metals and glass, from organic materials such as paper, wood, ~0 1 - ~k ,7 rags, plastic, and vegetable matter.
It is the organic material which is treated in the process described in patent 4,098,649, and with which the present invention is concerned. As in the process described in patent 4,098,649, the organic material is initially shredded into small particles, and then passes through a drying station from which it is fed to a mixer-reactor for further processing of the material.
The present invention utilizes a twin screw mixer or reactor which receives the material at one end, and discharges it as a char at the other. During the processing, lighter volatiles are vented at one point, and may be usefully combusted or further processed to separate them and reduce them to useful products. Heavier volatiles are vented from another region downstream, and may also be usefully combusted or separated and further processed to provide useful products. The waste product is reduced to an easily handled product having a far greater BTU value per pound than the original product.
In the present method, the twin screw mixer-reactor which is very satisfactorily employed comprises a pair of co-rotating axially extending shafts, with substantially co-wiping material advancing elements thereon, which also substantially wipe the interior of the barrel. Rather than seeking to apply external heat to the barrel, according to the method practiced in the prior systems to which reference is made, the work energy imparted to the material during the advancing and compression of the material which is necessary to the process, is utilized to raise the temperature of the material adiabatically. In so processing the material, tremendous cost savings are, of course, possible, and waste disposal is immediately rendered more economically viable.
Essentially the process is controlled by the mixer or agitator element geometry which determines energy input, and we have determined that smaller processing reactors can be used to produce larger volumes of char than previously.
The present method further involves processing the material at much lower temperatures than previously, so that the char material discharged includes a greater optimum percentage of the heavier hydrocarbons which increase the BTU
output of the char when it is later usefully combusted in a plant such as a coal-fired power plant.
In one aspect, the present invention provides a method of continuously carbonizing a mixture of primarily organic waste material which consists essentially of shredded paper, garbage, wood, and a minor proportion of synthetic plastic on the order of 4-8 percent by weight of the mixture, and reducing the mixture to a useful combustible char product comprising the steps of:
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture, content into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a , ,:
3a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
3b .
g. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the neighborhood of the range 450F. - 600F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
In a second aspect, the present invention provides a method of continuously carbonizing a mixture of primarily organic waste material which principally includes comminuted, cellulosic material, garbage, and a minor proportion of synthetic plastic material, and reducing the mixture to a useful combustible char product comprising the steps of:
3c it 1333~7~
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utilizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream zone by advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, while working the material against itself to create heat in the material which raises the temperature of the material 3d adiabatically to volatile releasing and material carbonizing temperature without applying any material external heat to the mixer for transfer to the moving material;
f. venting volatiles from said vent in said another region; and g. discharging the carbonized material from said further downstream zone.
In a third aspect, the present invention provides a higher BTU friable dry char produced by continuously carbonizing a mixture of primarily organic waste material which consists essentially of paper, garbage, wood, and a minor proportion of synthetic plastic, and reducing the mixture to a useful combustible char product wherein the steps followed are:
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture, content, into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat 3e 133337~
to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
g. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent 3f region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the range 450F. - 600F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
In a fourth aspect, the present invention provides a higher BTU friable dry char produced by continuously carbonizing a mixture of primarily organic waste material which principally includes paper, garbage, and a minor proportion of synthetic plastic material, and reducing it to a useful combustible char product wherein the steps followed are:
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one 3g 133337~
end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utlizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream mixer zone advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent in said another region;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, 3h while working the material against itself to create heat in the material which raises the temperature of the material adiabatically, without applying any material external heat to the mixer for transfer to the moving material, to a volatile releasing and material carbonizing temperature in the range 450F. - 600F.;
f. venting volatiles from said vent in said another region; and g. discharging a friable particulate char from said further downstream zone.
In a fifth aspect, the present invention provides a method of continuously carbonizing a mixture of primarily organic waste material which principally includes paper, garbage, and a minor proportion of synthetic plastic material, and reducing it to a useful combustible char product comprising the steps of:
a. continuouly feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the 3i ,~ , i3333~ ~
barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region;
e. and discharging the carbonized product as a burnable char from said downstream region.
In a sixth aspect, the present invention provides a method of continuously carbonizing a mixture of comminuted primarily organic waste material comprising the steps of:
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material 3j 1/33~7~
adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region; and e. discharging the carbonized product.
In one possible embodiment, the present invention may provide a method of converting organic waste materials to useful materials wherein the materials and heat energy salvaged can, in considerable part, pay for the costs of disposal, without creating pollution and landfill problems.
In another possible embodiment, the invention may provide a process in which the pyrolyzing of the material in the reactor is better controlled, cylindering of the material in the mixer is avoided, and the low-bulk density material being processed is more positively advanced as a moving stream with the result that the product obtained is a more homogeneous product.
Still another possible embodiment of the invention may provide a final product which has a higher BTU value than previously has been obtained, and which discharges as a dry friable product which does not agglomerate, and can be more easily handled and utilized when mixed with coal particles.
Another possible embodiment of the invention may provide a continuous process which can very efficiently process a large volume of material in a manner to create economy of scale efficiencies and obtain maximum benefits from the disposal of hitherto unwanted refuse material.
3k 13333~6 Figure 1 is a partially schematic, side sectional elevational view, illustrating the reactor in which the material is processed;
Figure 2 is a sectional, top plan view of the reactor illustrated in Figure l;
Figure 3 is a transverse, sectional view through the twin screws, taken on any of the lines 3-3 of Figure l;
Figure 4 is a transverse, sectional view of the self wiping paddles employed in certain regions, taken on any of the lines 4-4 of Figure l;
Figure 5 is a transverse, sectional view taken on the line 5-5 of Figure l;
Figure 6 is a fragmentary, sectional, plan view on an enlarged scale of the charge end of the reactor;
Figure 7 is a fragmentary, sectional, plan view of the discharge end of the reactor;
Figure 8 is an enlarged side elevational view schematically illustrating the manner in which the paddle elements are arranged in helical formation on each shaft in several regions of the reactor;
Figure 9 is an end elevational view of the elements illustrated in Figure 8;
Figure 10 is a densification graph illustrating how the material is compressed and decompressed in its passage 133337~
through the reactor; and Figure ll is a graph which portrays the temperature ranges at which the present process produces a more useful char than has been previously produced. Referring now more particularly to the accompanying drawings, and in the first instance particularly to Figure l, it is to be understood that the refuse which is to be carbonized will first have been processed to remove metal and glass. It will, in other words, consist essentially of organic material and have a relatively high paper content with relation to the other organic material which typically comprises garbage, wood and plastic material. This material then will be shredded, ground and dried, and will enter the mixer-reactor generally designated R, via a feed port lO, communicating with a hopper H supplied by a horizontally disposed, power-driven screw feed element ll, which positively feeds the material into the figure 8-shaped barrel chamber 12 (see Figures 3 and 4) at ` a predetermined rate. The material being fed typically will enter the reactor in pieces up to l-l/2 inches in diameter and have a plastic content on the order of 4-8 percent by weight dependent on the degree to which the material is presorted prior to being fed. The rate of feed of the material by screw ll, will be such as to maintain the barrel chamber 12 partially ` ~ filled with the material as the material proceeds in a continuous stream from the feed port end of the machine to the discharge end of the machine, traveling from right to left in Figures l and 2.
Generally speaking, in tests which were conducted, it was found that the material had relatively good flow properties, and, in order to process it at suitable commercial 133~3~
rates, it was necessary to compress the relatively fluffy material and work it against itself in order to impart the work energy required to heat it to the desired temperatures.
As the figures indicate, the axially extending barrel chamber 12 provided in the barrel, generally designated 12a, houses a pair of co-rotating shafts 13 and 14, driven from a motor, generally designated M, through a gear system, generally designated 15, which includes gears which are more or less schematically indicated at 15a, 15b, and 15c, for driving the shafts in the same direction and at the same speed of rotation.
As will become apparent, the mixing and forwarding elements which are provided on the shafts from one end of the reactor R to the other, are of both screw and paddle form, and have differing configurations in different zones of the reactor chamber 12 to perform designated tasks. Throughout the reactor R, both the screws and paddles are of the co-wiping character illustrated in Figures 3, 4, and 5, so that, as the material proceeds from one end of the reactor to the other, the radial surfaces of the screws and paddles are completely co-wiped, as are the entire interior surfaces of the figure 8-shaped barrel 12. The particular screw and paddle cross-sectional configura-tions which have been illustrated are preferred, and work very satisfactorily in the practice of the method involved in the present invention. It is believed that other paddle shapes are also possible, however, such as paddles of generally triangular, or tri-lobe type.
Fixed on the shafts 13 and 14 at the charge, or feed, end of the reactor R, are the helical advancing screw sections 16 and 17 which are of the lenticular cross-section illustrated in Figure 3. These sections 16 and 17 extend slightly beyond a 13~337 6 first barrel vent 18, which, principally, removes steam from the reactor. While the material charged will have been predried, it typically will have a low residual moisture content in the range of 8 to 9 percent.
Further, while it is desired that carbonization in the reactor occurs as near as possible in the absence of oxygen, inevitably, there is a minor amount of air entrapped or entrained in the product which is also released at vent 18.
While not shown, if desired, a pipe could lead into the barrel 12 at the charge end of the reactor R to flood the product with nitrogen gas, as an oxidation control agent.
Immediately downstream from the advancing screw sections 16 and 17, is a first material chopping and compressing reqion, generally designated 19, in which lenticular paddles 20a and 20b, of the same configuration as the paddles 31a and 31b disclosed in Figure 4, are disposed on the respective shafts in 90 out of phase relationship. These radially abutting paddles 20a and 20b, which are fixed on - ! shafts 14 and 13, respectively, are progressively axially angularly out of phase or offset on each shaft, with the axially adjacent paddles on each shaft arranged in helical formation. The paddles 20a and 20b in the upstream and middle portions of reyion 19 are arranged in a helical array which moves the greater proportion of material forwardly in a downstream direction. The material is moved by drag flow, with some of the material being moved in a direction to work against the material being moved forwardly. This material working action of the paddles 20a and 20b is enhanced at the discharge end of region 19 by arranging the several paddles 20a and 20b in the downstream end of region 19 in reverse helical formation on each shaft 13 and 14 as shown in Figure 8 at x so that the greater proportion of material in this part of the reactor tends to be directed rearwardly or reversely. Of course, the far greater number of paddles 20a and 20b tend to force the 5 material forwardly so the net effect is forward movement of the mass. In Figure 8, where the paddle lobes are shaded for purposes of illustrating the helical formation and in Figure 9, the paddles 20 and 20b are shown in more detail and it will be observed that the interface of the paddles of forwarding hand and of reversing hand is at x'. While the paddles 20a and 20b are shown as disposed in helical, product-moving formation, it should be understood they could also or alternatively, each be helically configured for product-moving purposes. While the successive paddles 20a and 20b are shown as 30 degrees out of phase on each shaft 13 and 14 in Figures 8 and 9 for purposes of better illustrating the helical formation, it is to be understood they more normally would be 45 or 60 degrees out of phase in their helical formation.
The function of paddles 20a and 20b in region 19, is to so compress the charged material as to form a vapor block at the downstream end of region 19, in the area l9a, and to also chop, or further shred, the material to further reduce it in particle size. In view of the formation of the barrel-filling, compressed moving mass of material in the downstream end of region 19, steam, and any small amounts of air which are released, flow countercurrently in an upstream or reverse direction to vent 18. These vapors may be found useful in a heat exchanger, generally designated HE, which can be used to provide heat for useful purposes, either for an industrial 133~376 process in which heat is required, for heating a building, or for some like function.
The region 19 may be aptly described as a product-steaming region in which the product is further dried and steam is driven off, but substantially no pyrolysis of the charged material occurs. The temperature attained, via work energy inputted to the material by paddle sections 20a and 20b, will be in the neighborhood of 225 F at vent 18, and in the neighborhood of 400 F at the discharge end of region 19.
The temperature rise in the charged material, commencing with the ambient temperature at which the material is charged to the machine, to the temperature of 400F., which is reached at the downstream end l9a of region 19, is virtually solely a function of the work energy imparted to the material by working it via the paddles 20a and 20b, and is reached gradually, or progressively in region 19. The jacket 21, which surrounds the barrel 12a and provides a plurality of surrounding chambers 22, 22a, 22b, 22c, and 22d, is filled with a heat transfer fluid which, in effect, only warms the metal and imparts no heat to the material being processed. The metal warming heating fluids in chamber 22 are recirculating fluids, which are expediently utilized at start-up, when no material is being pro~e~sed, to warm the metal initially to the equilibrium temperature of the process, so that the metal does not remove heat from the charge during processing. This barrel warming heat could also be electrically applied to the barrel.
Immediately downstream from region 19, is a first decompression zone, generally designated 23. In this region the helical advancing screw section 24 and 25 fixed on shafts 13 and 14, are of the same pitch and lenticular cross-section g as screw sections 16 and 17. The screw sections 24 and 25 accordingly are configured for a lower degree of fill than region l9a and the material is permitted to relax sufficiently so that it does not flow out a second vent 26. In this respect, the screw sections 24 and 25 are like the screw sections 16 and 17, in the sense that the pressure within the barrel 12 at these vents is not such as to force solid material out the vents. While considered unnecessary, once the machine is in operation, suction pumps or fans may be connected with any of the vents which are used in the system to aid process start-up, or even to aid the withdrawal of vaporous or off-gas material, should that be deemed desirable.
The vent 26 is a vent which egresses light volatiles which are released downstream from region 19, and the vent 26 can lead to and supply a suitable condensor when there is a reason to trap these volatiles and separate useful products -- from them, or may lead to a burner for combusting them.
Downstream from region 23, and fixed on shafts 13 and 14, are helical screw sections 27 and 28 of the single lead or lobe configuration disclosed in Figure 5, which have such a pitch, relative to the pitch of screw sections 24 and 25, as to - commence to recompress the material. The region 29 of the barrel, occupied by screw sections 27 and 28 functions as an initial recompression zone, and leads to a region 30 in which paddle sections 31a and 31b, of the same lenticular -~ configuration and helical formation as paddles 20a and 20b, further chop and reduce the material while further compressing and densifying it. The paddles 31a and 31b are arranged identically to the illustration of paddles 20a and 20b in ~O Figures 8 and 9. Here again, far more paddles 31a and 31b are arranged helically to forward the flow, than to reverse it in the downstream end of region 30, where the forwarding and reversing paddles confront at an interface z, and the net flow is forward. In regions 23 and 29, the charged fluffy material has begun to toast, and further toasts in region 30, such that, by the time it reaches the adjacent downstream region 31, it has taken on a dark brown color. The color of the material proceeding from region 23 in a downstream direction gradually changes from tan to the dark brown color it assumes at the discharge end of region 30, where a temperature in the neighborhood of 450F has been reached.
In region 31, single lobe screw sections 32 and 33, identical to the helical sections 27 and 28, are fixed on shafts 13 and 14 at the upstream end of region 31. Single lobe, screw sections 34 and 35 of exactly the same configuration, but of reverse hand, are fixed on shafts 13 and - 14 at the downstream end of region 31, confronting the forwarding screw sections 32 and 33 at an interface z. The screw sections 34 and 35 function with the screw sections 32 and 33 to work the material against itself and provide a significantly increased work input of heat to the material.
The material proceeding through regions 29, 30 and 31 is, during the process of pyrolyzing, being greatly reduced in volume and particle size, so that, at least at region 36, near the interface z between the screw sections 34 and 35, and 32 and 33, a vapor block of compressed material, which fills the barrel 12, is provided. The lighter volatiles which are released in regions 29, 30 and 31, thus proceed ~ countercurrently in a rearward or upstream direction to be ; 30 vented at vent 26.
13333~6 Downstream from the region 31, is a second decompression region 37, from which a vent 38 extends. In this region 37, advancing screw sections 39 and 40, which are fixed on shafts 13 and 14 and are of the same configuration as the screw sections 24, 25 and 16, 17, are of such pitch as to permit decompression of the material at vent 38. Vent 38 is a heavy volatiles vent, and may lead to a suitable condensor which permits separation and recovery of the useful, heavy vapors. Alternatively, these vapors may be efficiently combusted to furnish the requisite heat for an industrial process or the like.
Downstream from region 37, where temperatures have reached a temperature in the neighborhood of 575-600F, single lobe decompressing forwarding screw sections 41 and 42, of the same configuration as screws 27 and 28, are fixed on shafts 13 and 14 in a region generally designated 43, and function with identically configured single lobe screw sections of opposite hand 44 and 45 fixed on the shafts 13 and 14, to recompress the material, and form a third vapor block at 46 which forces the heavy volatiles being given off in this region and region 37 to proceed countercurrently in a reverse or upstream direction to vent 38. At the vapor block area 46, the temperature has been raised to a temperature in the neighborhood of 600F., and final charring of the material occurs. The product in screw 2~ sections 39 and 40, has taken on a dark brown/black cast, ; whereas in the region 43, the material is completely black and has a charcoal-like appearance.
The material from region 43 extrudes directly into a conventional energy recovery cooler which cools the char below auto-ignition temperature, before releasing it to atmosphere.
Typically, the cooler may comprise a barrel housing a hollow forwarding screw through which a circulating cooling fluid is passed. Such a heated recirculating cooling fluid may be further used, of course, to furnish heat for a useful purpose.
During its passage through the reactor R, the material charged will have been reduced approximately 50-60 percent in weight and will have been greatly reduced in volume also. In ; the reactor, it is necessary that ever higher degrees of densification be achieved as the temperature increases and the pyrolyzation progressively proceeds. Figure lO discloses the densification curve which occurs in the process on a scale of 0-lO to illustrate relative densification where the value of lO
indicates the extruding densification at discharge. The product is released from the cooler to atmosphere as a dry, friable particulate which can be utilized, without further processing, as a coal additive in a utility power plant, for instance. Such an additive may be used in a mixture fed to the utility company burner in a ratio by weight of coal to additive in the range of 90 percent pulverized coal to lO percent char produced by the present system. The char product released by the present system will, as indicated, be friable, and will not tend to agglomerate due to the presence of sticky, heavy tars or the like, on the surfaces of the char particles. By pyrolyzing the material gradually and raising its temperature 25 gradually to a final temperature in the range 550F. to 600F., a char product is obtained which retains certain organic materials in a chemically combined state such that the char provides a higher BTU content, when burned, than previously.
The char product produced by the present lower temperature process typically provides BTU per pound values much like a high grade coal where the product provided by previous processes produced BTU ratings similar to low grade coal.
Combustibility, also, is considerably enhanced in the present product. In Figure ll, a graph is provided which illustrates the values provided.
While one embodiment of the invention has been described in detail, it will be apparent to those skilled in the art that the disclosed embodiment may be modified.
Therefore, the foregoing description in all aspects is to be considered exemplary rather than limiting in any way, and the true scope of the invention is that defined in the following claims .
,.~
~0
A MIXTURE OF PRIMARILY ORGANIC WASTE MATERIAL
The present invention is concerned with an improved method of destructively distilling comminuted mixtures of primarily organic waste materials, which includes paper, garbage, and other refuse material and reducing them to a useful, combustible friable char product, which can be mixed with coal particles, for example, and usefully burned by utility companies and the like to produce electrical power.
- The method to be disclosed involves certain novel, useful and unobvious improvements in processes which have been proposed for converting organic waste material to a char material, such as the processes disclosed in United States patents 4,098,649; 4,123,332; and 4,308,103. The conversion of industrial and municipal waste by incinerating it in conven-tional incinerators and/or burying it in landfill areas is no longer viable for the future. The conventional incineration of the material releases fumes and smoke to the atmosphere which are objectionable, and cause pollution problems. Moreover, presently practiced incineration is expensive and does not re`sult in the recovery of any useful products which can offset the cost of incineration. The burying of waste in landfill areas is also unsatisfactory in this society in view of the tremendous volumes of waste which are generated nationwide, and the scarcity of landfill areas which, afterward are no longer useful for most other purposes.
Prior art methods, such as the method disclosed in patent 4,098,649, have initially separated the trash into organic and inorganic materials. Principally, this division of the trash or refuse has resulted in the separation of the metals and glass, from organic materials such as paper, wood, ~0 1 - ~k ,7 rags, plastic, and vegetable matter.
It is the organic material which is treated in the process described in patent 4,098,649, and with which the present invention is concerned. As in the process described in patent 4,098,649, the organic material is initially shredded into small particles, and then passes through a drying station from which it is fed to a mixer-reactor for further processing of the material.
The present invention utilizes a twin screw mixer or reactor which receives the material at one end, and discharges it as a char at the other. During the processing, lighter volatiles are vented at one point, and may be usefully combusted or further processed to separate them and reduce them to useful products. Heavier volatiles are vented from another region downstream, and may also be usefully combusted or separated and further processed to provide useful products. The waste product is reduced to an easily handled product having a far greater BTU value per pound than the original product.
In the present method, the twin screw mixer-reactor which is very satisfactorily employed comprises a pair of co-rotating axially extending shafts, with substantially co-wiping material advancing elements thereon, which also substantially wipe the interior of the barrel. Rather than seeking to apply external heat to the barrel, according to the method practiced in the prior systems to which reference is made, the work energy imparted to the material during the advancing and compression of the material which is necessary to the process, is utilized to raise the temperature of the material adiabatically. In so processing the material, tremendous cost savings are, of course, possible, and waste disposal is immediately rendered more economically viable.
Essentially the process is controlled by the mixer or agitator element geometry which determines energy input, and we have determined that smaller processing reactors can be used to produce larger volumes of char than previously.
The present method further involves processing the material at much lower temperatures than previously, so that the char material discharged includes a greater optimum percentage of the heavier hydrocarbons which increase the BTU
output of the char when it is later usefully combusted in a plant such as a coal-fired power plant.
In one aspect, the present invention provides a method of continuously carbonizing a mixture of primarily organic waste material which consists essentially of shredded paper, garbage, wood, and a minor proportion of synthetic plastic on the order of 4-8 percent by weight of the mixture, and reducing the mixture to a useful combustible char product comprising the steps of:
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture, content into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a , ,:
3a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
3b .
g. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the neighborhood of the range 450F. - 600F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
In a second aspect, the present invention provides a method of continuously carbonizing a mixture of primarily organic waste material which principally includes comminuted, cellulosic material, garbage, and a minor proportion of synthetic plastic material, and reducing the mixture to a useful combustible char product comprising the steps of:
3c it 1333~7~
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utilizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream zone by advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, while working the material against itself to create heat in the material which raises the temperature of the material 3d adiabatically to volatile releasing and material carbonizing temperature without applying any material external heat to the mixer for transfer to the moving material;
f. venting volatiles from said vent in said another region; and g. discharging the carbonized material from said further downstream zone.
In a third aspect, the present invention provides a higher BTU friable dry char produced by continuously carbonizing a mixture of primarily organic waste material which consists essentially of paper, garbage, wood, and a minor proportion of synthetic plastic, and reducing the mixture to a useful combustible char product wherein the steps followed are:
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture, content, into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat 3e 133337~
to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
g. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent 3f region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the range 450F. - 600F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
In a fourth aspect, the present invention provides a higher BTU friable dry char produced by continuously carbonizing a mixture of primarily organic waste material which principally includes paper, garbage, and a minor proportion of synthetic plastic material, and reducing it to a useful combustible char product wherein the steps followed are:
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one 3g 133337~
end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utlizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream mixer zone advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent in said another region;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, 3h while working the material against itself to create heat in the material which raises the temperature of the material adiabatically, without applying any material external heat to the mixer for transfer to the moving material, to a volatile releasing and material carbonizing temperature in the range 450F. - 600F.;
f. venting volatiles from said vent in said another region; and g. discharging a friable particulate char from said further downstream zone.
In a fifth aspect, the present invention provides a method of continuously carbonizing a mixture of primarily organic waste material which principally includes paper, garbage, and a minor proportion of synthetic plastic material, and reducing it to a useful combustible char product comprising the steps of:
a. continuouly feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the 3i ,~ , i3333~ ~
barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region;
e. and discharging the carbonized product as a burnable char from said downstream region.
In a sixth aspect, the present invention provides a method of continuously carbonizing a mixture of comminuted primarily organic waste material comprising the steps of:
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material 3j 1/33~7~
adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region; and e. discharging the carbonized product.
In one possible embodiment, the present invention may provide a method of converting organic waste materials to useful materials wherein the materials and heat energy salvaged can, in considerable part, pay for the costs of disposal, without creating pollution and landfill problems.
In another possible embodiment, the invention may provide a process in which the pyrolyzing of the material in the reactor is better controlled, cylindering of the material in the mixer is avoided, and the low-bulk density material being processed is more positively advanced as a moving stream with the result that the product obtained is a more homogeneous product.
Still another possible embodiment of the invention may provide a final product which has a higher BTU value than previously has been obtained, and which discharges as a dry friable product which does not agglomerate, and can be more easily handled and utilized when mixed with coal particles.
Another possible embodiment of the invention may provide a continuous process which can very efficiently process a large volume of material in a manner to create economy of scale efficiencies and obtain maximum benefits from the disposal of hitherto unwanted refuse material.
3k 13333~6 Figure 1 is a partially schematic, side sectional elevational view, illustrating the reactor in which the material is processed;
Figure 2 is a sectional, top plan view of the reactor illustrated in Figure l;
Figure 3 is a transverse, sectional view through the twin screws, taken on any of the lines 3-3 of Figure l;
Figure 4 is a transverse, sectional view of the self wiping paddles employed in certain regions, taken on any of the lines 4-4 of Figure l;
Figure 5 is a transverse, sectional view taken on the line 5-5 of Figure l;
Figure 6 is a fragmentary, sectional, plan view on an enlarged scale of the charge end of the reactor;
Figure 7 is a fragmentary, sectional, plan view of the discharge end of the reactor;
Figure 8 is an enlarged side elevational view schematically illustrating the manner in which the paddle elements are arranged in helical formation on each shaft in several regions of the reactor;
Figure 9 is an end elevational view of the elements illustrated in Figure 8;
Figure 10 is a densification graph illustrating how the material is compressed and decompressed in its passage 133337~
through the reactor; and Figure ll is a graph which portrays the temperature ranges at which the present process produces a more useful char than has been previously produced. Referring now more particularly to the accompanying drawings, and in the first instance particularly to Figure l, it is to be understood that the refuse which is to be carbonized will first have been processed to remove metal and glass. It will, in other words, consist essentially of organic material and have a relatively high paper content with relation to the other organic material which typically comprises garbage, wood and plastic material. This material then will be shredded, ground and dried, and will enter the mixer-reactor generally designated R, via a feed port lO, communicating with a hopper H supplied by a horizontally disposed, power-driven screw feed element ll, which positively feeds the material into the figure 8-shaped barrel chamber 12 (see Figures 3 and 4) at ` a predetermined rate. The material being fed typically will enter the reactor in pieces up to l-l/2 inches in diameter and have a plastic content on the order of 4-8 percent by weight dependent on the degree to which the material is presorted prior to being fed. The rate of feed of the material by screw ll, will be such as to maintain the barrel chamber 12 partially ` ~ filled with the material as the material proceeds in a continuous stream from the feed port end of the machine to the discharge end of the machine, traveling from right to left in Figures l and 2.
Generally speaking, in tests which were conducted, it was found that the material had relatively good flow properties, and, in order to process it at suitable commercial 133~3~
rates, it was necessary to compress the relatively fluffy material and work it against itself in order to impart the work energy required to heat it to the desired temperatures.
As the figures indicate, the axially extending barrel chamber 12 provided in the barrel, generally designated 12a, houses a pair of co-rotating shafts 13 and 14, driven from a motor, generally designated M, through a gear system, generally designated 15, which includes gears which are more or less schematically indicated at 15a, 15b, and 15c, for driving the shafts in the same direction and at the same speed of rotation.
As will become apparent, the mixing and forwarding elements which are provided on the shafts from one end of the reactor R to the other, are of both screw and paddle form, and have differing configurations in different zones of the reactor chamber 12 to perform designated tasks. Throughout the reactor R, both the screws and paddles are of the co-wiping character illustrated in Figures 3, 4, and 5, so that, as the material proceeds from one end of the reactor to the other, the radial surfaces of the screws and paddles are completely co-wiped, as are the entire interior surfaces of the figure 8-shaped barrel 12. The particular screw and paddle cross-sectional configura-tions which have been illustrated are preferred, and work very satisfactorily in the practice of the method involved in the present invention. It is believed that other paddle shapes are also possible, however, such as paddles of generally triangular, or tri-lobe type.
Fixed on the shafts 13 and 14 at the charge, or feed, end of the reactor R, are the helical advancing screw sections 16 and 17 which are of the lenticular cross-section illustrated in Figure 3. These sections 16 and 17 extend slightly beyond a 13~337 6 first barrel vent 18, which, principally, removes steam from the reactor. While the material charged will have been predried, it typically will have a low residual moisture content in the range of 8 to 9 percent.
Further, while it is desired that carbonization in the reactor occurs as near as possible in the absence of oxygen, inevitably, there is a minor amount of air entrapped or entrained in the product which is also released at vent 18.
While not shown, if desired, a pipe could lead into the barrel 12 at the charge end of the reactor R to flood the product with nitrogen gas, as an oxidation control agent.
Immediately downstream from the advancing screw sections 16 and 17, is a first material chopping and compressing reqion, generally designated 19, in which lenticular paddles 20a and 20b, of the same configuration as the paddles 31a and 31b disclosed in Figure 4, are disposed on the respective shafts in 90 out of phase relationship. These radially abutting paddles 20a and 20b, which are fixed on - ! shafts 14 and 13, respectively, are progressively axially angularly out of phase or offset on each shaft, with the axially adjacent paddles on each shaft arranged in helical formation. The paddles 20a and 20b in the upstream and middle portions of reyion 19 are arranged in a helical array which moves the greater proportion of material forwardly in a downstream direction. The material is moved by drag flow, with some of the material being moved in a direction to work against the material being moved forwardly. This material working action of the paddles 20a and 20b is enhanced at the discharge end of region 19 by arranging the several paddles 20a and 20b in the downstream end of region 19 in reverse helical formation on each shaft 13 and 14 as shown in Figure 8 at x so that the greater proportion of material in this part of the reactor tends to be directed rearwardly or reversely. Of course, the far greater number of paddles 20a and 20b tend to force the 5 material forwardly so the net effect is forward movement of the mass. In Figure 8, where the paddle lobes are shaded for purposes of illustrating the helical formation and in Figure 9, the paddles 20 and 20b are shown in more detail and it will be observed that the interface of the paddles of forwarding hand and of reversing hand is at x'. While the paddles 20a and 20b are shown as disposed in helical, product-moving formation, it should be understood they could also or alternatively, each be helically configured for product-moving purposes. While the successive paddles 20a and 20b are shown as 30 degrees out of phase on each shaft 13 and 14 in Figures 8 and 9 for purposes of better illustrating the helical formation, it is to be understood they more normally would be 45 or 60 degrees out of phase in their helical formation.
The function of paddles 20a and 20b in region 19, is to so compress the charged material as to form a vapor block at the downstream end of region 19, in the area l9a, and to also chop, or further shred, the material to further reduce it in particle size. In view of the formation of the barrel-filling, compressed moving mass of material in the downstream end of region 19, steam, and any small amounts of air which are released, flow countercurrently in an upstream or reverse direction to vent 18. These vapors may be found useful in a heat exchanger, generally designated HE, which can be used to provide heat for useful purposes, either for an industrial 133~376 process in which heat is required, for heating a building, or for some like function.
The region 19 may be aptly described as a product-steaming region in which the product is further dried and steam is driven off, but substantially no pyrolysis of the charged material occurs. The temperature attained, via work energy inputted to the material by paddle sections 20a and 20b, will be in the neighborhood of 225 F at vent 18, and in the neighborhood of 400 F at the discharge end of region 19.
The temperature rise in the charged material, commencing with the ambient temperature at which the material is charged to the machine, to the temperature of 400F., which is reached at the downstream end l9a of region 19, is virtually solely a function of the work energy imparted to the material by working it via the paddles 20a and 20b, and is reached gradually, or progressively in region 19. The jacket 21, which surrounds the barrel 12a and provides a plurality of surrounding chambers 22, 22a, 22b, 22c, and 22d, is filled with a heat transfer fluid which, in effect, only warms the metal and imparts no heat to the material being processed. The metal warming heating fluids in chamber 22 are recirculating fluids, which are expediently utilized at start-up, when no material is being pro~e~sed, to warm the metal initially to the equilibrium temperature of the process, so that the metal does not remove heat from the charge during processing. This barrel warming heat could also be electrically applied to the barrel.
Immediately downstream from region 19, is a first decompression zone, generally designated 23. In this region the helical advancing screw section 24 and 25 fixed on shafts 13 and 14, are of the same pitch and lenticular cross-section g as screw sections 16 and 17. The screw sections 24 and 25 accordingly are configured for a lower degree of fill than region l9a and the material is permitted to relax sufficiently so that it does not flow out a second vent 26. In this respect, the screw sections 24 and 25 are like the screw sections 16 and 17, in the sense that the pressure within the barrel 12 at these vents is not such as to force solid material out the vents. While considered unnecessary, once the machine is in operation, suction pumps or fans may be connected with any of the vents which are used in the system to aid process start-up, or even to aid the withdrawal of vaporous or off-gas material, should that be deemed desirable.
The vent 26 is a vent which egresses light volatiles which are released downstream from region 19, and the vent 26 can lead to and supply a suitable condensor when there is a reason to trap these volatiles and separate useful products -- from them, or may lead to a burner for combusting them.
Downstream from region 23, and fixed on shafts 13 and 14, are helical screw sections 27 and 28 of the single lead or lobe configuration disclosed in Figure 5, which have such a pitch, relative to the pitch of screw sections 24 and 25, as to - commence to recompress the material. The region 29 of the barrel, occupied by screw sections 27 and 28 functions as an initial recompression zone, and leads to a region 30 in which paddle sections 31a and 31b, of the same lenticular -~ configuration and helical formation as paddles 20a and 20b, further chop and reduce the material while further compressing and densifying it. The paddles 31a and 31b are arranged identically to the illustration of paddles 20a and 20b in ~O Figures 8 and 9. Here again, far more paddles 31a and 31b are arranged helically to forward the flow, than to reverse it in the downstream end of region 30, where the forwarding and reversing paddles confront at an interface z, and the net flow is forward. In regions 23 and 29, the charged fluffy material has begun to toast, and further toasts in region 30, such that, by the time it reaches the adjacent downstream region 31, it has taken on a dark brown color. The color of the material proceeding from region 23 in a downstream direction gradually changes from tan to the dark brown color it assumes at the discharge end of region 30, where a temperature in the neighborhood of 450F has been reached.
In region 31, single lobe screw sections 32 and 33, identical to the helical sections 27 and 28, are fixed on shafts 13 and 14 at the upstream end of region 31. Single lobe, screw sections 34 and 35 of exactly the same configuration, but of reverse hand, are fixed on shafts 13 and - 14 at the downstream end of region 31, confronting the forwarding screw sections 32 and 33 at an interface z. The screw sections 34 and 35 function with the screw sections 32 and 33 to work the material against itself and provide a significantly increased work input of heat to the material.
The material proceeding through regions 29, 30 and 31 is, during the process of pyrolyzing, being greatly reduced in volume and particle size, so that, at least at region 36, near the interface z between the screw sections 34 and 35, and 32 and 33, a vapor block of compressed material, which fills the barrel 12, is provided. The lighter volatiles which are released in regions 29, 30 and 31, thus proceed ~ countercurrently in a rearward or upstream direction to be ; 30 vented at vent 26.
13333~6 Downstream from the region 31, is a second decompression region 37, from which a vent 38 extends. In this region 37, advancing screw sections 39 and 40, which are fixed on shafts 13 and 14 and are of the same configuration as the screw sections 24, 25 and 16, 17, are of such pitch as to permit decompression of the material at vent 38. Vent 38 is a heavy volatiles vent, and may lead to a suitable condensor which permits separation and recovery of the useful, heavy vapors. Alternatively, these vapors may be efficiently combusted to furnish the requisite heat for an industrial process or the like.
Downstream from region 37, where temperatures have reached a temperature in the neighborhood of 575-600F, single lobe decompressing forwarding screw sections 41 and 42, of the same configuration as screws 27 and 28, are fixed on shafts 13 and 14 in a region generally designated 43, and function with identically configured single lobe screw sections of opposite hand 44 and 45 fixed on the shafts 13 and 14, to recompress the material, and form a third vapor block at 46 which forces the heavy volatiles being given off in this region and region 37 to proceed countercurrently in a reverse or upstream direction to vent 38. At the vapor block area 46, the temperature has been raised to a temperature in the neighborhood of 600F., and final charring of the material occurs. The product in screw 2~ sections 39 and 40, has taken on a dark brown/black cast, ; whereas in the region 43, the material is completely black and has a charcoal-like appearance.
The material from region 43 extrudes directly into a conventional energy recovery cooler which cools the char below auto-ignition temperature, before releasing it to atmosphere.
Typically, the cooler may comprise a barrel housing a hollow forwarding screw through which a circulating cooling fluid is passed. Such a heated recirculating cooling fluid may be further used, of course, to furnish heat for a useful purpose.
During its passage through the reactor R, the material charged will have been reduced approximately 50-60 percent in weight and will have been greatly reduced in volume also. In ; the reactor, it is necessary that ever higher degrees of densification be achieved as the temperature increases and the pyrolyzation progressively proceeds. Figure lO discloses the densification curve which occurs in the process on a scale of 0-lO to illustrate relative densification where the value of lO
indicates the extruding densification at discharge. The product is released from the cooler to atmosphere as a dry, friable particulate which can be utilized, without further processing, as a coal additive in a utility power plant, for instance. Such an additive may be used in a mixture fed to the utility company burner in a ratio by weight of coal to additive in the range of 90 percent pulverized coal to lO percent char produced by the present system. The char product released by the present system will, as indicated, be friable, and will not tend to agglomerate due to the presence of sticky, heavy tars or the like, on the surfaces of the char particles. By pyrolyzing the material gradually and raising its temperature 25 gradually to a final temperature in the range 550F. to 600F., a char product is obtained which retains certain organic materials in a chemically combined state such that the char provides a higher BTU content, when burned, than previously.
The char product produced by the present lower temperature process typically provides BTU per pound values much like a high grade coal where the product provided by previous processes produced BTU ratings similar to low grade coal.
Combustibility, also, is considerably enhanced in the present product. In Figure ll, a graph is provided which illustrates the values provided.
While one embodiment of the invention has been described in detail, it will be apparent to those skilled in the art that the disclosed embodiment may be modified.
Therefore, the foregoing description in all aspects is to be considered exemplary rather than limiting in any way, and the true scope of the invention is that defined in the following claims .
,.~
~0
Claims (20)
1. A method of continuously carbonizing a mixture of primarily organic waste material which consists essentially of shredded paper, garbage, wood, and a minor proportion of synthetic plastic on the order of 4-8 percent by weight of the mixture, and reducing the mixture to a useful combustible char product comprising the steps of:
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture content, into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts ;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
g. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the neighborhood of the range 450°F. - 600°F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture content, into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts ;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
g. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the neighborhood of the range 450°F. - 600°F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
2. The method of claim 1 in which said char is passed through a cooler to lower its temperature below an auto-ignition temperature.
3. The method of claim 1 in which carbonization of said material is completed upstream of said third vent region due to the air starved atmosphere in said barrel.
4. The method of claim 1 in which said mixing and material conveying elements for compressing the material to squeeze out the air and form said first block are bi-lobe elements of substantially lenticular configuration.
5. The method of claim 4 in which said mixing and material conveying elements for recompressing the material to form said mass of moving material functioning as a second block are bi-lobe elements of substantially lenticular configuration.
6. The method of claim 1 in which said mixing and material conveying elements recompressing the material to form said mass of moving material functioning as a third block are single lobe elements.
7. The method of claim 1 wherein at said first vent region the temperature of the material has been raised to a downstream direction.
level in the neighborhood of 225° F.
level in the neighborhood of 225° F.
8. The method of claim 7 wherein at said second vent region the temperature of the material has been raised to a level in the neighborhood of 400°F.
9. The method of claim 1 wherein at said second recompression region the temperature of the material has been raised to a level in the neighborhood of 400°F.
10. The method of claim 1 wherein at said third vent region the temperature of the material has been raised to a level in the neighborhood of 590°F.
11. The method of claim 1 wherein in said first and second recompression regions, said mixing and material conveying elements move material countercurrently to work against material being moved by said mixing and material conveying elements in a downstream direction.
12. The method of claim 1 wherein at said first vapor block said mixing and material conveying elements move material countercurrently to work against material being advanced by said mixing and material conveying elements in a downstream direction to aid compression and create work energy.
13. The method of claim 1 wherein said mixing and material conveying elements in step b include elements arranged in opposing helical formation on said shafts to provide a net forwarding and compressing pressure on said material.
14. The process of claim 1 wherein said material is decompressed in a third vent region and then recompressed and further compressed downstream from said third vent region.
15. A method of continuously carbonizing a mixture of primarily organic waste material which principally includes comminuted, cellulosic material, garbage, and a minor proportion of synthetic plastic material, and reducing the mixture to a useful combustible char product comprising the steps of:
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utilizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream zone by advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to volatile releasing and material carbonizing temperature without applying any material external heat to the mixer for transfer to the moving material;
f. venting volatiles from said vent in said another region; and g. discharging the carbonized material from said further downstream zone.
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utilizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream zone by advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to volatile releasing and material carbonizing temperature without applying any material external heat to the mixer for transfer to the moving material;
f. venting volatiles from said vent in said another region; and g. discharging the carbonized material from said further downstream zone.
16. The process of claim 15 wherein said first level of compression in said first region is generally in the neighbor-hood of about 75 percent of the final extruding compression of the material at discharge and said second level of compression at said second vapor block is generally in the neighborhood of about 90 percent of the final extruding compression of the material.
17. A higher BTU friable dry char produced by continuously carbonizing a mixture of primarily organic waste material which consists essentially of paper, garbage, wood, and a minor proportion of synthetic plastic, and reducing the mixture to a useful combustible char product wherein the steps followed are:
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture, content, into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
9. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the range 450°F. - 600°F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
a. continuously feeding a stream of the shredded waste material with a substantial organic, and some moisture, content, into one end of a twin screw mixer having an axially extending, elongate barrel, with a barrel chamber of uniform size figure-eight cross section from said one end to the other end, and housing a pair of co-rotating axially extending shafts;
b. progressively compressing the material fed into one end of the mixer by advancing the material continuously through co-rotating mixing and material conveying elements on said shafts which leave a reduced volume of space in the uniform size barrel for the material to the extent of forming a barrel-filling mass of moving material functioning as a first vapor block, and utilizing the work energy imparted to the material required to compress the material to squeeze out entrapped air, and without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a moisture vaporizing temperature;
c. venting air and vaporized moisture at a first vent region upstream from said first vapor block;
d. continuing to advance the material in a downstream direction from said first vapor block by advancing the material through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a second vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said second vent region;
e. progressively recompressing the material in the absence of air in a first recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a second vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the material, to raise the temperature of the material adiabatically to a lighter volatile vaporizing temperature;
f. venting lighter volatiles from said second vent region;
9. continuing to advance the material by advancing it through co-rotating mixing and material conveying elements on said shafts and decompressing the material in a third vent region, having a vent, to provide a traveling mass of material which does not so fill the barrel as to be forced out the vent in said third vent region;
h. progressively again advancing and recompressing the material in the absence of air in a second recompression region by passing the material through co-rotating mixing and material conveying elements on said shafts which leave a relatively reduced volume of space in the uniform size barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a third vapor block, while utilizing the work energy required to recompress the material, without applying any material external heat to the mixer for transfer to the moving material, to raise the temperature of the material adiabatically to a material carbonizing and heavier volatile releasing temperature in the range 450°F. - 600°F.;
i. venting heavier volatiles from said third vent region;
and j. discharging a friable particulate char from the other end of the mixer.
18. A higher BTU friable dry char produced by continuously carbonizing a mixture of primarily organic waste material which principally includes paper, garbage, and a minor proportion of synthetic plastic material, and reducing it to a useful combustible char product wherein the steps followed are:
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utilizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream mixer zone advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent in said another region;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically, without applying any material external heat to the mixer for transfer to the moving material, to a volatile releasing and material carbonizing temperature in the range 450°F. - 600°F;
f. venting volatiles from said vent in said another region;
g. and discharging a friable particulate char from said further downstream zone.
a. continuously feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending mixer shafts;
b. progressively compressing the material fed into said one end of the mixer by advancing the material continuously through material conveying and compressing elements on the shafts which leave a reduced volume of space in the barrel for the material to the extent of forming a moving barrel-filling mass of material functioning as a first vapor block in a first region of said barrel, and utilizing the work energy imparted to the material required to squeeze out entrapped air in the material to raise the temperature of the material;
c. venting air squeezed out;
d. continuing to advance the material downstream from said first vapor block and in a further downstream mixer zone advancing it through mixing and material conveying elements on said shafts which decompress the material in another region having a vent to provide a traveling mass which does not so fill the barrel as to be forced out the vent in said another region;
e. in said further downstream zone progressively compressing the material downstream from said another region in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as another vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically, without applying any material external heat to the mixer for transfer to the moving material, to a volatile releasing and material carbonizing temperature in the range 450°F. - 600°F;
f. venting volatiles from said vent in said another region;
g. and discharging a friable particulate char from said further downstream zone.
19. A method of continuously carbonizing a mixture of primarily organic waste material which principally includes paper, garbage, and a minor proportion of synthetic plastic material, and reducing it to a useful combustible char product comprising the steps of:
a. continuouly feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region;
e. and discharging the carbonized product as a burnable char from said downstream region.
a. continuouly feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region;
e. and discharging the carbonized product as a burnable char from said downstream region.
20. A method of continuously carbonizing a mixture of comminuted primarily organic waste material comprising the steps of:
a. continuouly feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region;
e. and discharging the carbonized product.
a. continuouly feeding a stream of the comminuted waste material with a substantial organic materials content, into one end of a continuous mixer having an axially extending elongate barrel, housing axially extending, co-rotating mixer shafts;
b. contacting the material with material advancing elements on said shafts to advance the material fed into said one end of the mixer continuously through a first mixer region;
c. in a downstream mixer region progressively compressing the material in the substantial absence of air by passing it through material conveying and compressing elements on said shafts which leave a relatively reduced volume of space in the barrel for the material to the extent of forming a mass of moving material filling the barrel and functioning as a vapor block, while working the material against itself to create heat in the material which raises the temperature of the material adiabatically to a volatile releasing and material carbonizing temperature, without applying any material external heat to the mixer for transfer to the moving material;
d. venting volatiles from said downstream region;
e. and discharging the carbonized product.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US291,131 | 1988-12-28 | ||
| US07/291,131 US4908104A (en) | 1988-12-28 | 1988-12-28 | Method of continuously carbonizing a mixture of primarily organic waste material |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1333376C true CA1333376C (en) | 1994-12-06 |
Family
ID=23118993
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000613928A Expired - Fee Related CA1333376C (en) | 1988-12-28 | 1989-09-28 | Method of continuously carbonizing a mixture of primarily organic waste material |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US4908104A (en) |
| CA (1) | CA1333376C (en) |
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| SE8801377D0 (en) * | 1988-04-14 | 1988-04-14 | Productcontrol Ltd | PROCESSING OF ORGANIC MATERIAL |
| US6623602B1 (en) | 1998-11-06 | 2003-09-23 | G. Thomas Bissell | Method for reclaiming volatile products and non-volatile residue |
| US6273923B1 (en) * | 1999-01-25 | 2001-08-14 | Kenaf Biocatalytic Services, Llc | Catalytic vacuum distillation process |
| US7963048B2 (en) * | 2005-05-23 | 2011-06-21 | Pollard Levi A | Dual path kiln |
| US20060280669A1 (en) * | 2005-06-10 | 2006-12-14 | Jones Fred L | Waste conversion process |
| EP1947240B1 (en) * | 2005-10-06 | 2016-09-14 | Daio Paper Corporation | Regenerated particle aggregate, process for producing regenerated particle aggregate, regenerated-particle-aggregate-containing paper containing regenerated particle aggregate as internal additive, and coated printing paper coated with regenerated particle aggregate |
| CA2539012C (en) * | 2006-03-10 | 2013-07-09 | John Flottvik | Closed retort charcoal reactor system |
| US9045693B2 (en) | 2006-12-26 | 2015-06-02 | Nucor Corporation | Pyrolyzer furnace apparatus and method for operation thereof |
| BRPI0720677A2 (en) * | 2006-12-26 | 2014-03-18 | Nucor Corp | APPARATUS AND METHOD FOR PRODUCING COAL. |
| GB2450704A (en) * | 2007-07-03 | 2009-01-07 | Mars Inc | Screw extruder with a fluid inlet and a method of extruding |
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| ES2621287T3 (en) * | 2009-03-17 | 2017-07-03 | T.D.E. Recovery Technologies Ltd. | A pyrolytic reactor |
| US8328993B2 (en) * | 2009-05-18 | 2012-12-11 | Greenlight Energy Solutions, Llc | Pyrolysis reactor for processing municipal wastes |
| US8201501B2 (en) | 2009-09-04 | 2012-06-19 | Tinsley Douglas M | Dual path kiln improvement |
| US8795476B2 (en) * | 2010-09-24 | 2014-08-05 | John Flottvik | Charcoal reactor system |
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| CN112805084A (en) * | 2018-08-03 | 2021-05-14 | 美国能源系统网控股有限公司 | Biomass treatment apparatus, system, and method |
| JP6729906B1 (en) * | 2019-10-24 | 2020-07-29 | 柴田 勝美 | Heat treatment equipment |
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- 1988-12-28 US US07/291,131 patent/US4908104A/en not_active Expired - Lifetime
-
1989
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Also Published As
| Publication number | Publication date |
|---|---|
| US4908104A (en) | 1990-03-13 |
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