CA1169207A - Method for defibrating waste paper and dispersing contaminants - Google Patents
Method for defibrating waste paper and dispersing contaminantsInfo
- Publication number
- CA1169207A CA1169207A CA000389221A CA389221A CA1169207A CA 1169207 A CA1169207 A CA 1169207A CA 000389221 A CA000389221 A CA 000389221A CA 389221 A CA389221 A CA 389221A CA 1169207 A CA1169207 A CA 1169207A
- Authority
- CA
- Canada
- Prior art keywords
- steam
- stock
- mixing tube
- waste paper
- slurry
- 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
Links
Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
- D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
- D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
- D21B1/30—Defibrating by other means
- D21B1/32—Defibrating by other means of waste paper
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/64—Paper recycling
Abstract
METHOD FOR DEFIBRATING WASTE PAPER
AND DISPERSING CONTAMINANTS
Abstract of the Disclosure A method for defibrating waste paper and dis-persing contained asphalt and wax contaminants within the fibers, The waste paper is initially pulped with water and the resulting stock is then contacted with a high pressure stream of steam having a velocity in the range of 1200 to 1600 ft./sec. The mixture of steam and stock is passed through a mixing tube under highly turbulent conditions to defibrate the waste paper and disperse any asphalt, waxes, and other contaminants throughout the separated fibers. The resulting stock can be used in papermaking processes, particularly for the production of paperboard products.
AND DISPERSING CONTAMINANTS
Abstract of the Disclosure A method for defibrating waste paper and dis-persing contained asphalt and wax contaminants within the fibers, The waste paper is initially pulped with water and the resulting stock is then contacted with a high pressure stream of steam having a velocity in the range of 1200 to 1600 ft./sec. The mixture of steam and stock is passed through a mixing tube under highly turbulent conditions to defibrate the waste paper and disperse any asphalt, waxes, and other contaminants throughout the separated fibers. The resulting stock can be used in papermaking processes, particularly for the production of paperboard products.
Description
~ ~92(~
METllOD FOR DEFIBRATING WASTE PA~ER
AND DISPEP~SI~G CONT~'~INANTS
Background of the Dnvention Was-te paper, commonly referred to as secondary fiber, is of~en used in the manufacture of paper and paperboard products. At present, the paperboard industry is the primary user of the recovered secondary fiber, and is moving toward the use of liner and corrugated media composed of all secondary fiber.
lOThe secondary fiber frequently contains asphaltic materials, as well as waxes, and if the asphalt and waxes are not fully dispersed, they will appear as surface deposits which can result in a build-up on the press rolls cf the paper machine and downgrade the finished board. .-15In a typical secondary fiber pulping system, the waste paper is introduced into a pulper and agitated with water to provide a stock having a solids content in i the range of about 1% to 5%. After filtering tfnrough centrifuge cleaners and screens, the stock has tradition-ally been passed through an asphalt dispersion system in which the stock is thickened to a consistency of about 10% to 12% and then fed through a press where additional water is removed to raise the solids content to a range of 30% to 35%. The thickened stock is then introduced into a pre-heater where the stock is agitated and heated to a temperature of 250F to 325F to melt the asphalt and waxes. The stock is then blown into a cyclone or blowtank. At this point, water is added from the paper-board machine in order to decrease thesolids content to a value of 4% to 5%. From the cyclone the stock is flowed to a stock chest and is pumped to the refiners immediately ahead o~ the papermaking machine.
In the conventional asphalt dispersion system substantial capital equipment has been required to thicken the stock to a solids content of about 30% to :1 1692~
35~, heat and defibrate the stock, and then return the stock to its approximate original consistency. Not only did the conventional system require substantial capital investment for equipment, but the energy costs were extremely high and considerable floor space was re~uired for the equipment.
A variety of steam contact devices have been used in th~ past for heating liquids. Basic to all steam con-tact devices is the introduction of steam into the cold liquid u-tilizing a number of different device configura-tions, none of which are capable of heating a fibrous stock defibrating the fibers, and dispersing~he contaminants with a single piece of equipment.
Summary of the Invention __ ... ..
The invention is directed to an im~roved method of defibrating secondary fiber and dispersing any asphalt, waxes, and other contam;nants, within the separated fiber.
More pa~ticularl~, the stock of secondary fiber, after pulping and passing throu~h suitable filters, is ed to the inlet of a stock processing unit where it is passed into contact with a stream of high pressure steam having a velocity in the ranye of 1,200 ft/sec. to 1,600 ft~/sec.
The mixture of steam and stock is passed through a mixing tube under highly turbulent conditions which not only de~ibrates~ the secondary fiber, but also provides a com-pIate dispersion of the asphaltic materials, waxes and other contaminants through the sepaxated fibers.
With the present inventionr tne secondary ~ibex is heated, defibrated and the contaminants are dispersed through use of a single piece of equipment.
B~ use of the invention, a substantial reduction in capital investment is achieved over the conventional ; secondary fiber treatment processes. Due to the reduc-tion in capital equipment, the maintenance and manpower costs are also substantially reduced.
The system of the invention also reduces energy costs ànd provides a considerable space saving 1~ ~920~
over conventional systems, in that the space requir~~
ments are only about l/lOth of that required for the prior asphalt dispersion systems.
Lower grade waste paper cannot normally be used - 5 in the manufacture of paperboard for food containers, due to the offensive odor, bacteria and inadequa-te dispersion of other contaminants, However, the use of the high pressure steam serves to sterilize ~he stock and at the same time deodorize the stock, thereby enabl-ing the stock treated by the system o~ the invention to be used in food board and food containers.
Because of the improved dispersion of waxes, asphalt, and other contaminants, lower grades of waste paper can be used in the manufacture of paperboard and other products, ~hereby reducing the ovexall material cost for the papermaking process~
Other~objects and advantages will appear in the course of the following description.
Descri;ption of- the Drawihgs-The drawings illustrate the best mode presently contemplated of carrying out the invention.
In the dra~ings:
Fig. 1 is a schematic representation of a secondary stock system utilizing the method of the invention;
Fig. 2 is a longitudinal section of the stock processing unit; and Fig. 3 is a section taken along line 3-3 of Fig. 2.
Description of the Preferred Embodiment Fig. 1 illustrates a secondary stock system incorporating the present invention. ~he waste paper or secondary fiber is introduced into the pulper l and agitated with water to provide secondary stock having a solids content in the range of about 1.0% to 5~ by ~ ~920~
weight. The stock is pumped from the pulper 1 through lin~ 2 by pump 3 to a cyclone, indicated generally by 4 r where both light and heavy oreign materials are removed ~rom the stock.
Line 2 includes a conventional consistency regulator 5 which senses ~he consistency o~ the pulp passing through line 2 and automatically regulates the amount of water which is being introduced through line 6 to the pulper 1 to provide the desired solids content.
The st~ck being discharged from the cyclone 4 passes through barrier screen 7 where additional large-si~e contaminants are removed and is then discharged through line 8 to stock chest 9. The stock is pumped through line 10 from stock chest 9 by pump 11 and is introduced to the stock processing unit, indicated genarally by 12, where the stock is con~acted by a high pressure, high velocity stream o~ steam which acts to separate the ~ibers and fully disperse ~he waxes, asphalt and other contaminants.
The stock is discharged from the processing unit 12 through llne 13 to stock chest 14 and then is pumped through line 15 by pump 16 to the refiner 17.
A consistency regulator 18, similar to reguLator 5, is mounted in line 15 and senses the consistency of the stock and programs the addition o~ water through line 19, i~ necessary, to provide the desired stock consis- -tency.
In the event there is a stoppage ofthe paper-making machine, in which case the stock cannot be dis-charged rom the refiner 17 to the papermaking machine,a by-pass line 20 is connected between line 13 and stock chest 9. A li~uid level control 21 in stock chest 14, senses the level of the stock and controls valves 22 and 23 in lines 13 and 20, respectively, to thereby return the stock to the stock chest 9 in the event the li~uid level in stock chest 14 reaches a pre-set value.
20~
The processing unit 12 includes an outer hous-ing 24 having an inlet 25 connected to line lO for the introduction of stock into stock chamber 26. In addi-tion, housing 2~ is provided with a steam inlet 17 which is connected by line 28 to a source of steam under pressure, and the steam inlet 27 communicates with a steam chamber 29.
Located between the steam chamber 29 and the stock chamber 26 is a nozzle 30, and a conical plug 31 is spaced from the inner surface of nozzle 30 and defines a tapered annular passage 32 therebetween.
The position of the plug 31 can be adjusted axially to vary the cross-sectional area of the passage 32 and thus vary the amount of steam being delivered through the unit. To provide the adjustment for plug 31, a stem 33 is connected to the plug and extends through a suitable packing 34 in the end of the housing 24. The outer end of the stem is connected to a conven-tional diaphragm-type pressure actuator 35. A tempera-ture sensor 36 is located downstream of the processingunit 12 and senses the temperature of the stock being discharged from the unit~ If the temperature falls beneath a pre-set value, the sensor will operate the actuator 35 to thereby move the stem 33 to the left, as shown in Fig. 2, to increase the cross-sectional area of the passage 32 and increase the amount of steam being delivered to the unit. Conversely, if the tem-perature of the stock rises above a pre-set limit, the sensor will operate the actuator 35 to decrease the cross-sectional area o~ passage 32 and reduce the supply of steam.
Mounted within the housing is a mixing tube 37, and the upstream end of the mixing tube is spaced from the discharye of the nozzle 30.
The spacing between the upstream end of the mixing tube 37 and the nozzle 30 can be varied to con-20~
trol the velocity of stock flowing into the mixing tube 37. In this regard, a stud 33 is threadedly con-nected to the mixing tube 37 and extends outwardly through a slot 39 in housing 24 an~ is attached to a bar 40 which is mounted for slidiny movement on the outer surface of the housing. One end of a yoke 41 is connected to the outer end of the stud 38, while the opp~site end of the yoke is threaded and is received within the opening in a lug 42 on the outer surface of housing 24. Lock nuts 43 are engaged with the threaded end portion of the yoke 41 and are located on either side of the lug 42. By loosening the lock nuts 43, the yoke 41 can be moved axially of the housing to corres-pondingly move the mixing tube 37. This adjustment pro-vides a variation in the spacing between the upstream end of the mixing tube 37 and the nozzle 30 to regulate the~velocity of stock entering the unit.
The stock entering the housing 24 through inlet 25 has a consistency in the range of 1% to 5~ solids~
a temperature in the range of 100F to 135F, and a velocity o~ about 5 to 10 ft./sec. The steam entering the housing through the inlet 27 is at a pressure in excess of 20 psig and generally in the range of 50 to 100 psig. At the discharge end of the noz~le 30, the steam has a velocity in the range of 1200 to 1600 ft./
sec. and preferably in the range of about 1400 to 1500 ft,/sec.
The high pressure steam blasts against and into - the stock which is flowing from the stock chamber 26 into the bore of the mixing tube 37, and creates trem-endous turbulence within the mixing tube 37. This results in separation of the fibers in the stock, as well as heating the stock, so that the stock being dis-charged from the mixing tube has a temperature generally in the range of 170~F to 230F. The steam also serves 1 lB9207 to melt any asphalt contained in the stock as well as other wax-type contaminants, and the high turbl~lence will completely disperse these liquified materials within the fibers. This eliminates the possibility of the asphalt being concentrated at the surface o~ the paper sheet subsequently formed in the papermaking process, and minimizes the build-up of asphalt on the press rolls of the paper machine.
The steam will completely condense within the mixing tube 37 and the stock being discharged from the mixing tube will have a consistency decrease in the range of 0.01% to 0.03~ solids and will have a velocity of about'l4 to 22 ft~/sec.
As the system of the invention does not work the fibrous material to the extent that it is worked in conventional processes, the ~uality and ~inish of the paper product produced with the theated secondary fiber is believed'to be superior to that of secondary fiber treated by conventianal processes.
The steam also serves the additional function of sterilizing and deodorizing the secondary fiber.
This enables the ~iber to be used for applications, such as food product containers, where in many cases secondary fiber has not been usable.
Due to the thorough dispersion of the asphalt, the paper mills can utilize lower', less expensive grades of secondary fiber.
The SysterQ of the invention eliminates substan-tial capital equipment which was necessary in prior systems of secondary fiber treatment. More particularly, the capital expenditure required ~or the defibrator-asphalt dispersion system of the invention is only about 4% to 14% of that of conventional asphalt disper-sion systems. Due to the reduction in amount of capita' equipment required, maintenance, power demand and man-power requirements are reduced and great operating savings are achieved.
METllOD FOR DEFIBRATING WASTE PA~ER
AND DISPEP~SI~G CONT~'~INANTS
Background of the Dnvention Was-te paper, commonly referred to as secondary fiber, is of~en used in the manufacture of paper and paperboard products. At present, the paperboard industry is the primary user of the recovered secondary fiber, and is moving toward the use of liner and corrugated media composed of all secondary fiber.
lOThe secondary fiber frequently contains asphaltic materials, as well as waxes, and if the asphalt and waxes are not fully dispersed, they will appear as surface deposits which can result in a build-up on the press rolls cf the paper machine and downgrade the finished board. .-15In a typical secondary fiber pulping system, the waste paper is introduced into a pulper and agitated with water to provide a stock having a solids content in i the range of about 1% to 5%. After filtering tfnrough centrifuge cleaners and screens, the stock has tradition-ally been passed through an asphalt dispersion system in which the stock is thickened to a consistency of about 10% to 12% and then fed through a press where additional water is removed to raise the solids content to a range of 30% to 35%. The thickened stock is then introduced into a pre-heater where the stock is agitated and heated to a temperature of 250F to 325F to melt the asphalt and waxes. The stock is then blown into a cyclone or blowtank. At this point, water is added from the paper-board machine in order to decrease thesolids content to a value of 4% to 5%. From the cyclone the stock is flowed to a stock chest and is pumped to the refiners immediately ahead o~ the papermaking machine.
In the conventional asphalt dispersion system substantial capital equipment has been required to thicken the stock to a solids content of about 30% to :1 1692~
35~, heat and defibrate the stock, and then return the stock to its approximate original consistency. Not only did the conventional system require substantial capital investment for equipment, but the energy costs were extremely high and considerable floor space was re~uired for the equipment.
A variety of steam contact devices have been used in th~ past for heating liquids. Basic to all steam con-tact devices is the introduction of steam into the cold liquid u-tilizing a number of different device configura-tions, none of which are capable of heating a fibrous stock defibrating the fibers, and dispersing~he contaminants with a single piece of equipment.
Summary of the Invention __ ... ..
The invention is directed to an im~roved method of defibrating secondary fiber and dispersing any asphalt, waxes, and other contam;nants, within the separated fiber.
More pa~ticularl~, the stock of secondary fiber, after pulping and passing throu~h suitable filters, is ed to the inlet of a stock processing unit where it is passed into contact with a stream of high pressure steam having a velocity in the ranye of 1,200 ft/sec. to 1,600 ft~/sec.
The mixture of steam and stock is passed through a mixing tube under highly turbulent conditions which not only de~ibrates~ the secondary fiber, but also provides a com-pIate dispersion of the asphaltic materials, waxes and other contaminants through the sepaxated fibers.
With the present inventionr tne secondary ~ibex is heated, defibrated and the contaminants are dispersed through use of a single piece of equipment.
B~ use of the invention, a substantial reduction in capital investment is achieved over the conventional ; secondary fiber treatment processes. Due to the reduc-tion in capital equipment, the maintenance and manpower costs are also substantially reduced.
The system of the invention also reduces energy costs ànd provides a considerable space saving 1~ ~920~
over conventional systems, in that the space requir~~
ments are only about l/lOth of that required for the prior asphalt dispersion systems.
Lower grade waste paper cannot normally be used - 5 in the manufacture of paperboard for food containers, due to the offensive odor, bacteria and inadequa-te dispersion of other contaminants, However, the use of the high pressure steam serves to sterilize ~he stock and at the same time deodorize the stock, thereby enabl-ing the stock treated by the system o~ the invention to be used in food board and food containers.
Because of the improved dispersion of waxes, asphalt, and other contaminants, lower grades of waste paper can be used in the manufacture of paperboard and other products, ~hereby reducing the ovexall material cost for the papermaking process~
Other~objects and advantages will appear in the course of the following description.
Descri;ption of- the Drawihgs-The drawings illustrate the best mode presently contemplated of carrying out the invention.
In the dra~ings:
Fig. 1 is a schematic representation of a secondary stock system utilizing the method of the invention;
Fig. 2 is a longitudinal section of the stock processing unit; and Fig. 3 is a section taken along line 3-3 of Fig. 2.
Description of the Preferred Embodiment Fig. 1 illustrates a secondary stock system incorporating the present invention. ~he waste paper or secondary fiber is introduced into the pulper l and agitated with water to provide secondary stock having a solids content in the range of about 1.0% to 5~ by ~ ~920~
weight. The stock is pumped from the pulper 1 through lin~ 2 by pump 3 to a cyclone, indicated generally by 4 r where both light and heavy oreign materials are removed ~rom the stock.
Line 2 includes a conventional consistency regulator 5 which senses ~he consistency o~ the pulp passing through line 2 and automatically regulates the amount of water which is being introduced through line 6 to the pulper 1 to provide the desired solids content.
The st~ck being discharged from the cyclone 4 passes through barrier screen 7 where additional large-si~e contaminants are removed and is then discharged through line 8 to stock chest 9. The stock is pumped through line 10 from stock chest 9 by pump 11 and is introduced to the stock processing unit, indicated genarally by 12, where the stock is con~acted by a high pressure, high velocity stream o~ steam which acts to separate the ~ibers and fully disperse ~he waxes, asphalt and other contaminants.
The stock is discharged from the processing unit 12 through llne 13 to stock chest 14 and then is pumped through line 15 by pump 16 to the refiner 17.
A consistency regulator 18, similar to reguLator 5, is mounted in line 15 and senses the consistency of the stock and programs the addition o~ water through line 19, i~ necessary, to provide the desired stock consis- -tency.
In the event there is a stoppage ofthe paper-making machine, in which case the stock cannot be dis-charged rom the refiner 17 to the papermaking machine,a by-pass line 20 is connected between line 13 and stock chest 9. A li~uid level control 21 in stock chest 14, senses the level of the stock and controls valves 22 and 23 in lines 13 and 20, respectively, to thereby return the stock to the stock chest 9 in the event the li~uid level in stock chest 14 reaches a pre-set value.
20~
The processing unit 12 includes an outer hous-ing 24 having an inlet 25 connected to line lO for the introduction of stock into stock chamber 26. In addi-tion, housing 2~ is provided with a steam inlet 17 which is connected by line 28 to a source of steam under pressure, and the steam inlet 27 communicates with a steam chamber 29.
Located between the steam chamber 29 and the stock chamber 26 is a nozzle 30, and a conical plug 31 is spaced from the inner surface of nozzle 30 and defines a tapered annular passage 32 therebetween.
The position of the plug 31 can be adjusted axially to vary the cross-sectional area of the passage 32 and thus vary the amount of steam being delivered through the unit. To provide the adjustment for plug 31, a stem 33 is connected to the plug and extends through a suitable packing 34 in the end of the housing 24. The outer end of the stem is connected to a conven-tional diaphragm-type pressure actuator 35. A tempera-ture sensor 36 is located downstream of the processingunit 12 and senses the temperature of the stock being discharged from the unit~ If the temperature falls beneath a pre-set value, the sensor will operate the actuator 35 to thereby move the stem 33 to the left, as shown in Fig. 2, to increase the cross-sectional area of the passage 32 and increase the amount of steam being delivered to the unit. Conversely, if the tem-perature of the stock rises above a pre-set limit, the sensor will operate the actuator 35 to decrease the cross-sectional area o~ passage 32 and reduce the supply of steam.
Mounted within the housing is a mixing tube 37, and the upstream end of the mixing tube is spaced from the discharye of the nozzle 30.
The spacing between the upstream end of the mixing tube 37 and the nozzle 30 can be varied to con-20~
trol the velocity of stock flowing into the mixing tube 37. In this regard, a stud 33 is threadedly con-nected to the mixing tube 37 and extends outwardly through a slot 39 in housing 24 an~ is attached to a bar 40 which is mounted for slidiny movement on the outer surface of the housing. One end of a yoke 41 is connected to the outer end of the stud 38, while the opp~site end of the yoke is threaded and is received within the opening in a lug 42 on the outer surface of housing 24. Lock nuts 43 are engaged with the threaded end portion of the yoke 41 and are located on either side of the lug 42. By loosening the lock nuts 43, the yoke 41 can be moved axially of the housing to corres-pondingly move the mixing tube 37. This adjustment pro-vides a variation in the spacing between the upstream end of the mixing tube 37 and the nozzle 30 to regulate the~velocity of stock entering the unit.
The stock entering the housing 24 through inlet 25 has a consistency in the range of 1% to 5~ solids~
a temperature in the range of 100F to 135F, and a velocity o~ about 5 to 10 ft./sec. The steam entering the housing through the inlet 27 is at a pressure in excess of 20 psig and generally in the range of 50 to 100 psig. At the discharge end of the noz~le 30, the steam has a velocity in the range of 1200 to 1600 ft./
sec. and preferably in the range of about 1400 to 1500 ft,/sec.
The high pressure steam blasts against and into - the stock which is flowing from the stock chamber 26 into the bore of the mixing tube 37, and creates trem-endous turbulence within the mixing tube 37. This results in separation of the fibers in the stock, as well as heating the stock, so that the stock being dis-charged from the mixing tube has a temperature generally in the range of 170~F to 230F. The steam also serves 1 lB9207 to melt any asphalt contained in the stock as well as other wax-type contaminants, and the high turbl~lence will completely disperse these liquified materials within the fibers. This eliminates the possibility of the asphalt being concentrated at the surface o~ the paper sheet subsequently formed in the papermaking process, and minimizes the build-up of asphalt on the press rolls of the paper machine.
The steam will completely condense within the mixing tube 37 and the stock being discharged from the mixing tube will have a consistency decrease in the range of 0.01% to 0.03~ solids and will have a velocity of about'l4 to 22 ft~/sec.
As the system of the invention does not work the fibrous material to the extent that it is worked in conventional processes, the ~uality and ~inish of the paper product produced with the theated secondary fiber is believed'to be superior to that of secondary fiber treated by conventianal processes.
The steam also serves the additional function of sterilizing and deodorizing the secondary fiber.
This enables the ~iber to be used for applications, such as food product containers, where in many cases secondary fiber has not been usable.
Due to the thorough dispersion of the asphalt, the paper mills can utilize lower', less expensive grades of secondary fiber.
The SysterQ of the invention eliminates substan-tial capital equipment which was necessary in prior systems of secondary fiber treatment. More particularly, the capital expenditure required ~or the defibrator-asphalt dispersion system of the invention is only about 4% to 14% of that of conventional asphalt disper-sion systems. Due to the reduction in amount of capita' equipment required, maintenance, power demand and man-power requirements are reduced and great operating savings are achieved.
Claims (8)
1. A method of defibrating waste paper and dispersing contained contaminants within the dispersed fibers, comprising the steps of contacting an aqueous stock of waste paper having a fibrous solids content of 1% to 5% by weight with steam at a pressure in excess of 20 psig and at a velocity of 1,200 to 1,600 ft./sec. to provide a steam-stock mixture, and flowing the mixture through a mixing tube under highly turbul-ent conditions to thereby heat the stock, separate the fibers of the stock and disperse any contained contam-inants.
2. The method of claim 1, and including the step of flowing the stock into contact with the steam at a velocity of 14 to 22 ft./sec.
3. The method of claim 1, and including the step of sensing the temperature of the mixture down-stream of the mixing tube, and adjusting the rate of flow of said steam to provide a substantially uniform temperature for the mixture.
4. A method of defibrating waste paper and dispersing contained contaminants within the dispersed fibers, comprising the steps of passing steam at a pressure in excess of 20 psig through a nozzle in a housing to obtain a steam velocity in the range of 1,200 to 1,600 ft./sec., directing the steam into a mixing tube spaced axially of said nozzle, introducing an aqueous slurry of waste paper having a fibrous solids content of 1% to 5% by weight into the space in the hous-ing between said nozzle and said mixing tube, and sub-jecting the mixture of steam and slurry to highly turbulent conditions in said mixing tube to thereby
4. A method of defibrating waste paper and dispersing contained contaminants within the dispersed fibers, comprising the steps of passing steam at a pressure in excess of 20 psig through a nozzle in a housing to obtain a steam velocity in the range of 1,200 to 1,600 ft./sec., directing the steam into a mixing tube spaced axially of said nozzle, introducing an aqueous slurry of waste paper having a fibrous solids content of 1% to 5% by weight into the space in the hous-ing between said nozzle and said mixing tube, and sub-jecting the mixture of steam and slurry to highly turbulent conditions in said mixing tube to thereby
Claim 4 cont'd. . . . . .
heat the slurry, separate the fibers in the slurry and disperse any contained contaminants throughout the separated fibers.
heat the slurry, separate the fibers in the slurry and disperse any contained contaminants throughout the separated fibers.
5. The method of claim 4, and including the step of flowing the slurry into the housing at a veloc-ity of 5 to 10 ft./sec.
6. The method of claim 4, and including the step of maintaining the velocity of the mixture of steam and slurry at the downstream end of said mixing tube in the range of 14 to 22 ft./sec.
7. The method of claim 4, and including the step of adjusting the axial spacing between the nozzle and the mixing tube to establish the velocity of the slurry flowing to said space.
8. The method of claim 5, and including the step of maintaining the pressure of the steam entering said nozzle at a value of 50 to 100 psig.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US204,942 | 1980-11-07 | ||
| US06/204,942 US4312701A (en) | 1980-11-07 | 1980-11-07 | Method for defibrating waste paper and dispersing contaminants |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1169207A true CA1169207A (en) | 1984-06-19 |
Family
ID=22760112
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000389221A Expired CA1169207A (en) | 1980-11-07 | 1981-11-02 | Method for defibrating waste paper and dispersing contaminants |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US4312701A (en) |
| CA (1) | CA1169207A (en) |
Families Citing this family (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3241876A1 (en) * | 1982-11-12 | 1984-05-17 | J.M. Voith Gmbh, 7920 Heidenheim | DEVICE FOR FACTIONING FIBER SUSPENSION |
| US4872953A (en) * | 1986-12-18 | 1989-10-10 | Eze Products, Inc. | Apparatus for improving the quality of paper manufactured from recycled paper with a hydrokinetic amplifier |
| US4726880A (en) * | 1986-12-18 | 1988-02-23 | Eze Products, Inc. | Method and apparatus for improving the quality of paper manufactured from recycled paper with a hydrokinetic amplifier |
| DE3728890C1 (en) * | 1987-08-29 | 1988-07-14 | Escher Wyss Gmbh | Process for regulating the specific dispersion work |
| EP0315709A1 (en) * | 1987-11-10 | 1989-05-17 | Kimberly-Clark Corporation | Newsprint furnish and newsprint paper |
| DE3827336A1 (en) * | 1988-08-12 | 1990-02-15 | Escher Wyss Gmbh | METHOD FOR TREATING THE SHORT FIBER FRACTION AFTER SEPARATING THE LONG FIBER FRACTION FROM A SECONDARY FIBER MIXTURE, ESPECIALLY FOR THE PRODUCTION OF CARTON BOXES |
| US5059280A (en) * | 1989-07-31 | 1991-10-22 | Kimberly-Clark Corporation | Method for removing agglomerated particles after dry fiberizing wastepaper |
| ES2023626T3 (en) * | 1989-10-10 | 1994-07-01 | Nils Anders Lennart Wikdahl | METHOD AND DEVICE FOR THE PRODUCTION OF IMPROVED QUALITY CELLULOSE PULP. |
| US5743638A (en) * | 1996-07-30 | 1998-04-28 | Q-Jet, Dsi | Dual control mixing jet cooker |
| US6306248B1 (en) | 1997-11-20 | 2001-10-23 | The University Of Alabama In Huntsville | Method for transforming diverse pulp and paper products into a homogenous cellulosic feedstock |
| EP0927788A3 (en) * | 1997-12-22 | 2000-05-03 | Roediger Anlagenbau GmbH | Process and apparatus for separating heavy and light materials from a suspension |
| US6113738A (en) | 1998-03-16 | 2000-09-05 | Nalco Chemical Company | Use of additives to breakdown and stabilize wax during fiber recycle |
| CN1150055C (en) | 1998-03-16 | 2004-05-19 | 纳尔科化学公司 | Contaminant dispersants useful in recycling of treated containers |
| US6372085B1 (en) | 1998-12-18 | 2002-04-16 | Kimberly-Clark Worldwide, Inc. | Recovery of fibers from a fiber processing waste sludge |
| US7364642B2 (en) * | 2003-08-18 | 2008-04-29 | Kimberly-Clark Worldwide, Inc. | Recycling of latex-containing broke |
| US7967877B2 (en) * | 2003-11-13 | 2011-06-28 | Biomass Worldwide Group Limited | Biomass energy product and processing method |
| US20060112749A1 (en) * | 2003-11-13 | 2006-06-01 | Noll Anthony P | Soil amendment product and method of processing |
| US20050166812A1 (en) * | 2003-11-13 | 2005-08-04 | Horizon Fuel And Financial Management, Llp | MSW processing vessel |
| US7745208B2 (en) * | 2006-02-15 | 2010-06-29 | Noll Anthony P | Angled reaction vessel |
| US8728802B2 (en) * | 2006-02-15 | 2014-05-20 | Biomass Worldwide Group Limited | Angled reaction vessel |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3057769A (en) * | 1955-05-16 | 1962-10-09 | Waldorf Paper Prod Co | Method of preparing paper of uniform appearance |
| US3736223A (en) * | 1970-12-01 | 1973-05-29 | Black Clawson Co | Waste treatment and fiber reclamation system |
| US3741863A (en) * | 1971-08-27 | 1973-06-26 | Rust Eng Co | Method of recycling waste cellulosic materials |
-
1980
- 1980-11-07 US US06/204,942 patent/US4312701A/en not_active Expired - Lifetime
-
1981
- 1981-11-02 CA CA000389221A patent/CA1169207A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| US4312701A (en) | 1982-01-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA1169207A (en) | Method for defibrating waste paper and dispersing contaminants | |
| US3661328A (en) | Pulp refining system and process | |
| CA2093260A1 (en) | Method for producing a delignified papermaking fiber from recycled, high lignin content, waste paper and product thereof | |
| EP0060104B1 (en) | Drying wood pulp | |
| JPS6315396B2 (en) | ||
| WO2003066962A1 (en) | Method for preparing fibres contained in a pulp suspension | |
| FI62149B (en) | FOERFARANDE FOER FRAMSTAELLNING AV VARMSLIPMASSA | |
| AU667015B2 (en) | Papermaking process and apparatus for use therewith | |
| US3891497A (en) | Non-aqueous defiberizing process of waste paper in the presence of steam and a liquid nonmiscible in water, e.g., tetrachlorethylene | |
| AT510109B1 (en) | METHOD, SYSTEM AND REFINER FOR GRINDING CHOPPES OR CELLULOSE FIBERS | |
| US4559104A (en) | Apparatus for discharging material | |
| US3884755A (en) | Closed cycle paper sheet production | |
| CA1052156A (en) | Pulp | |
| EP2099968A1 (en) | Method of treating filtrate produced in thickening of paper fibre suspension | |
| US5458738A (en) | Clarifying suspended solids from liquid process streams | |
| EP1759057A1 (en) | Method for producing a paper web and paper-making machine | |
| US6053439A (en) | Reducing wax content and enhancing quality of recycled pulp from OCC and waste paper | |
| WO1997013026A1 (en) | Apparatus for dewatering/pressing in combination with washing of paper pulp | |
| NO178348B (en) | Method and apparatus for producing cellulose pulp with improved quality properties | |
| CA1303399C (en) | Method for regulating working pressure during production of mechanical pulp | |
| WO1999046442A1 (en) | Method and apparatus for treatment of fiber suspension containing minerals, such as coated broke, in paper production | |
| DE10219844C1 (en) | Hot dispersion of a paper fiber suspension, from used recycled paper, has a press to give a high-consistency suspension for heating, with measurements of heating energy consumption to control the press action | |
| Kruse | Recycling old corrugated containers as furnish for wet process hardboard | |
| EP0721526B1 (en) | Method and apparatus for dewatering of a fibre suspension | |
| US3007519A (en) | Cleaning systems for paper making machines |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |