CN101116804B - Integrated reacting and separating device - Google Patents
Integrated reacting and separating device Download PDFInfo
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- CN101116804B CN101116804B CN2006100890386A CN200610089038A CN101116804B CN 101116804 B CN101116804 B CN 101116804B CN 2006100890386 A CN2006100890386 A CN 2006100890386A CN 200610089038 A CN200610089038 A CN 200610089038A CN 101116804 B CN101116804 B CN 101116804B
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Abstract
The present invention provides an integral reaction-separation equipment, mainly comprising a ring pipe and a separation component, wherein a circular reaction circuit is formed by the ring pipe and the separation component. The equipment is compact in structure, integrates catalytic reaction with catalyst separation and material heat transfer, especially can guarantee the high efficiency separation and the recycling use of fine particles such as nanometer or micron catalyst with reacting materials, and has good material mixing and heat transferring effects, which is suitable for strong heat absorbing or releasing solid-liquid, solid-liquid-liquid and partial gas-liquid-solid multiphase reaction system.
Description
Technical field
The present invention relates to a kind of chemical industry equipment, more specifically to the integration apparatus of a kind of catalytic reaction, product and catalyst separation and material heat exchange formation.
Background technology
At the petrochemical industry production field, have many chemical reaction processes not only to use solid catalyst, and in reaction time, is with strong heat release.In order to make reaction system avoid focus to produce and to keep temperature even, the mode of operation that adopts catalyst to float on a liquid can obtain comparatively satisfied effect.Because the heat transfer coefficient of liquid is bigger, the suspension mode of operation of catalyst in liquid is easy to reclaim heat; The catalyst grain size that this mode is used is less, therefore needn't can there be significant catalyst utilization rate of inner surface problem to catalyst granulation processing yet, helps the application of high activated catalyst, particularly need the frequent occasion of changing and regenerating for catalyst, it is comparatively convenient to operate.Slurries in the reactor can mix and stir by circulating of fluid, and the solid catalyst particulate is fully suspended, and have strengthened heat transfer and mass transfer.This mode of operation has been widely used in courses of reaction such as hydrogenation, oxidation, chlorination and polymerization.But one of greatest difficulty that this mode of operation faced is the separation problem of solid catalyst and liquid, and particularly very hour difficulty is even more serious for catalyst granules.In fact, for most catalytic reaction process, on the one hand catalyst granules need recycle, and catalyst granules and reactant liquor are separated fully with the safety of guaranteeing the subsequent operation step and the quality of the product that obtained.
Traditional paste state bed reactor adopts alr mode that catalyst is suspended more, and commercial plant for subparticle, because of the not high enough meeting of the less turbulence of slurries is sticked catalyst on reactor wall, has influenced the heat exchange effect owing to be subjected to the restriction of power of agitator; In addition, material exists big back-mixing in this class reactor, and to the reaction system that requires the raw material multiple feed or require very some occasions of high conversion, single paste state bed reactor is difficult to meet the demands.The general industry operating process is that catalytic reaction and catalyst separation are provided with separately, but this causes apparatus system comparatively huge.
In field of olefin polymerisation, annular-pipe reactor has obtained using widely.This class reactor has that the unit volume heat transfer area is big, Flow of Goods and Materials and troubled water is good, the device efficiency advantages of higher.Patent US6239235, US4121029, EP0891990 and WO2004024782 to annular-pipe reactor the application in olefinic polymerization carried out comparatively detailed description.
Although trickle catalyst granules is directly used in course of reaction many advantages are arranged, it is fully separated from reactant liquor, be the comparatively work of difficulty always.
US5534149 has proposed in the hydrogenation process of anthraquinone manufacturing hydrogen peroxide, contains the Pd/carbon catalyst of precious metal palladium and the separation method of reactant liquor.What this method adopted is the film resolution element, and the supporter of film is to be made by charcoal, pottery or metal material, and the aperture is 5-100 μ m; Film is to be made by the mixture of Alpha-alumina, zirconia, silica, and the aperture is 1-10 μ m; And film is carried out the periodicity backwash with working solution that does not contain catalyst or solvent.This method adopts the filter type of end sealing, and this mode of operation very easily causes the concentration polarization on film surface, and film pollutes also easily generation.
EP0571762 is identical with the reaction system of US5534149, what adopt is pottery or polyolefin micro-filtration membrane, and Pd/carbon catalyst is separated with reactant liquor in the mode of cross-flow, membrane material is an Alpha-alumina, the aperture is 0.1-3 μ m, and the strainability that this mode of operation shows filter element descends gradually, and this is because the pollution of metal sintering pipe and film is inevitable, it is not enough only depending on recoil, also needs regularly filter element to be regenerated.
As can be seen, above-mentioned prior art all is a filtration problem of only having considered catalyst, not with consersion unit, filter plant with move hot equipment and do integrated consideration.
CN1394672A relates to a kind of catalyst membrane separation method of heterogeneous suspension nano catalysis reaction, catalyst separation process and catalytic reaction process are combined, send in the inorganic film tube that average pore size is 2～200 nanometers and constantly be circulated between reactor and the inorganic film tube with the material in the pump continuous drawing reactor, utilize the screening principle of inoranic membrane, the constantly saturating filmed passing tube of liquid-phase product is separated, and the suspended state catalyst is trapped in to return in the reactor again in the film pipe and with recycle stock and recycles.Consersion unit is not coupled into integration apparatus with separating in this method, and flow process is longer.
CN2576324Y relates to Unitary suspend bed inorganic membrane reactor.This reactor is that the inoranic membrane separation assembly that several inorganic film tubes and film pipe bracing frame are formed is arranged in the reactor with certain arrangement mode, and an end of film pipe seals by shrouding, and the other end communicates with filtrate exit pipe.The film pipe is chosen pottery, metal material or their composite material film.The film pipe has vertically fixing in still according to the structure of support, multiple arrangement mode such as vertically rotate or horizontally rotate.This integrated mode is when film pipe and support go wrong, and whole device need stop and keep in repair, and is difficult to timely discovery in addition during the film tracheal rupture.
Summary of the invention
At the some shortcomings that existing procedure and device exist, the purpose of this invention is to provide that a kind of to collect catalytic reaction, catalyst separation and material heat exchange be one, be particularly suitable for the integrated reacting and separating device of finely grained catalyst.
Integrated reacting and separating device provided by the invention, it is characterized in that this equipment comprises endless tube 1 and separation assembly 2, endless tube 1 forms a closed circuit with separation assembly 2, circulating pump 3 is set on the endless tube 1, provide energy that reaction mass is circulated in the loop of endless tube 1 and separation assembly 2 formation, wherein endless tube 1 is provided with raw material and adds that inlet 4, catalyst add inlet 5, material unloads outlet 6, heat-exchange system 7, and the top of endless tube 1 is provided with liquid and collects balancer 8 and balance flue 9; Constitute by screen pipe 10 and housing 11 in the separation assembly 2, the screen pipe number is determined by the needed filter area of separation process, the setting of screen pipe makes reaction mass carry out Separation of Solid and Liquid in the mode of cross-flow, reaction mass is isolated product therein, product is discharged by outlet 12, the slurries of carrying after dense continue to circulate in endless tube, and separation assembly 2 is provided with backwashing system 13, and screen pipe 10 is carried out back flush to recover filtration flux.
Integrated reacting and separating device provided by the invention, reaction, heat transfer, mixing of materials and catalyst separation are carried out in an equipment, easy to operate, flow process is simple, compact conformation, is specially adapted to the gas-liquid-solid heterogeneous reaction of solid-liquid, solid-liquid-liquid and part of strong neither endothermic nor exothermic.This equipment has good mixing of materials and heat exchange effect, and reaction efficiency height, finely grained catalyst are difficult for sticking wall, and with the separative efficiency height of reaction mass.
Integrated reacting and separating device provided by the invention can be used for the Ammoximation reaction of ketone or the Ammoximation reaction of aldehyde, for example is used for the reaction of the amidoxime production cyclohexanone oxime of cyclohexanone.
Description of drawings
Fig. 1 is the schematic diagram of the integrated reacting and separating device that is made of one group of endless tube and separation assembly.Among the figure, 1-endless tube, 2-separation assembly, 3-circulating pump, 4-raw material add that inlet, 5-catalyst add inlet, the 6-material unloads outlet, 7-heat-exchange system, and 8-liquid is collected balancer, 9-balanced gas pipe, 10-screen pipe, 11-housing, the outlet of 12-product, 13-backwashing system.
The schematic diagram of the integrated reacting and separating device that Fig. 2 constitutes for being connected by two groups of endless tubes and separation assembly.Among the figure, the same Fig. 1 of the mark of 1-13, the 14-raw material replenishes mouth, 15-catalyst make-up mouth, 16-products export.
Fig. 3 is endless tube and two separation assembly F in parallel
1, F
2The schematic diagram of the integrated reacting and separating device that constitutes.
When Fig. 4 is ceramic-film tube for screen pipe in the separation assembly, the input and output material schematic diagram of reaction mass.Among the figure, 20-slurry, 21-product clear liquid junction, 22-purified liquor outlet, 23-to be separated carries slurries outlet, 24-encapsulant, the 11-separation assembly housing after dense.
When Fig. 5 is the metal sintering pipe for screen pipe in the separation assembly, the input and output material schematic diagram of reaction mass.Same Fig. 4 of mark among the figure.
Fig. 6 is the profile of ceramic membrane separation assembly.Among the figure, 31-runner, 32-screen pipe.
Fig. 7 is the separation assembly profile that metal film pipe or metal sintering pipe constitute.Among the figure, 33-runner, 34-screen pipe thickness.
The specific embodiment
Integrated reacting and separating device provided by the invention, main catalytic reaction process takes place in endless tube 1, endless tube 1 comprises upper and lower horizontal segment and vertical section, upper and lower horizontal segment defines the zone that the horizontal reaction mass in upper and lower flows, every section is connected with adjacent segment by a level and smooth elbow or bend pipe, the diameter of endless tube 1 and length depend on (comprising the hop count of upper and lower horizontal segment and vertical section etc.) production capacity, reaction time of concrete reaction and to the requirement of productive rate, endless tube can be obtained by steel, titanium, nickel metal or the processing of other alloy.
Circulating pump 3 on the endless tube 1, provide energy that reaction mass is circulated in endless tube 1, circulating pump 3 can be arranged on the appropriate location of endless tube 1, and circulating pump is generally axial-flow pump, be built in the endless tube, make feed liquid circulation at a high speed in endless tube, improved heat transfer, mass transfer effect, and, under the effect of circulating pump, reaction mass is made the high speed shuttling movement, has guaranteed the violent turbulence of material, and has reduced solid catalyst particulate sticking on the reactor wall; Good mixing makes and forms in the endless tube than uniform catalyst concentration, and catalyst granules can sedimentation, is difficult for sticking wall, can keep the catalyst concn higher than general tank reactor.
On endless tube 1, be provided with raw material and add inlet 4, the said inlet 4 that adds can at endless tube diverse location place, can be provided with one or more raw materials and add inlet in the diverse location setting of endless tube; Be provided with material at the following horizontal segment of endless tube 1 and unload outlet 6, generally material is unloaded outlet 6 and be arranged on that catalyst adds before the inlet 5, the material fluid transfers the adjacent domain of the rearmost point that upwards flows in the endless tube, so that make fresh catalyst before passing through emission point for the first time, can in reactor, be detained the long as far as possible time.Catalyst adds inlet and 5 can be provided with separately, and catalyst also can add inlet 4 and reaction raw materials adds together from raw material certainly.
Said heat-exchange system 7 is preferably the form of chuck on endless tube 1, is example with the exothermic reaction, and endless tube and external jacket have constituted coaxial double pipe heat exchanger, and the reaction mass that the coolant fluid in external jacket flows through in chuck and the endless tube carries out exchange heat; Cooling agent flows and contacts with the surface round the endless tube outer surface at the annular space of chuck, shifts out the reaction heat in the endless tube.
The top of endless tube 1 is provided with liquid and collects balancer 8 and balance flue 9, the safety of system is collected and guaranteed to unnecessary liquid when liquid is collected 8 pairs of equipment enforcement of balancer backwash operation, and the balance that balanced gas pipe 9 comes to guarantee by gas pressure system pressure is set.
In the integrated reacting and separating device provided by the invention, endless tube 1 is not limit with the connected mode of separation assembly 2, normally constitute the integral body of going in ring, and seal, a continuous logistics corridor so just is provided with suitable encapsulant by the flange connection; Owing to there is not voidage, it is high that the efficient of the paste state bed reactor that the reaction efficiency of this equipment is more traditional is wanted.
Integrated reacting and separating device provided by the invention, separation assembly 2 is made up of screen pipe 10 and housing 11, also has a certain amount of catalytic reaction to take place in separation assembly 2.Screen pipe is inorganic film tube or metal sintering pipe normally, and its radical depends on separation flux and total treating capacity.
Said inorganic film tube is selected from ceramic-film tube, metal film pipe, glass-film pipe or carbon film of molecular sieve pipe, and the aperture of film is from 4nm-50 μ m.The material of ceramic-film tube can be aluminium oxide, zirconia, titanium oxide or silica, and it is the 3-10mm runner that single ceramic-film tube has a plurality of diameters; The material of metal film pipe can be stainless steel, nickel metal, titanium or other alloy, is generally a runner.
Said metal sintering pipe is the porous metals pipe that metal dust (or metallic fiber) is made through high temperature sintering, and available stainless steel, other metal or alloy are made, and the aperture is from 0.5 μ m-200 μ m.
Product cross cleaner liquid constantly from the screen pipe surface through radially seeing through; enter and see through side; and the solid subparticle is blocked and is deposited on the surface of screen pipe; although swiftly flowing slurry makes that the sedimentary deposit on screen pipe surface is very thin, but can influence filtration flux, some superfine particulates also can stop up the micropore of screen pipe in addition; these all can cause the pollution of screen pipe; make filtration flux and selectivity descend, thereby reduce the production efficiency of filter, shorten the life-span of screen pipe.Therefore, backwashing system 13 is set, utilized cleaner liquid, solvent or reaction raw materials periodically to recoil and to make filtration flux maintain a comparatively stable scope.Recoil regularly guarantees to filter steady and continuous ground to be carried out, and the time of filter cycle and recoil is fast depended on parameters such as the concentration of concrete response characteristic and reaction temperature, pressure, slurry and internal circulating load.The film pollution condition that filtration flux also can't recover when recoiling fast for employing can adopt chemical method that screen pipe is thoroughly regenerated.
Said separation assembly can have a plurality of, and they are combined with endless tube with series, parallel or series-parallel system and are connected.Because equipment is behind the operation certain hour, the pollution of screen pipe can not be avoided fully in the separation assembly, and connected mode in parallel is convenient to switch between the separation assembly, has guaranteed the continuity of running, therefore preferred (referring to Fig. 3) or series-parallel mode in parallel.The choosing of encapsulant should consider its heat endurance, chemical compatibility and and membrane material between the matching of thermal coefficient of expansion, to avoid the leakage of material.
Said integrated reacting and separating device also can constitute (referring to Fig. 2) by two groups or more endless tube and separation assembly series connection.
The quick circulation under the effect of circulating pump of integrated reacting and separating device provided by the invention, reaction mass not only makes catalyst fully suspend and rapid mixing in liquid phase, and catalytic reaction takes place, and can prevent effectively that solid catalyst is at the screen pipe surface deposition; Screen pipe surface velocity requirement when higher circulation rate has also satisfied cross-flow filtration has weakened the concentration polarization phenomenon on screen pipe surface.
Below in conjunction with accompanying drawing 1-accompanying drawing 7 a kind of operating process of integrated reacting and separating device provided by the invention is described, but does not therefore limit content of the present invention.
Fig. 1 is the schematic diagram of the integrated reacting and separating device that is made of one group of endless tube and separation assembly.Reaction raw materials adds inlet 4 from raw material, catalyst adds inlet 5 from catalyst and adds the endless tube 1, make its forced circulation by circulating pump 3, flowing of reactant mixture should be kept sufficiently high speed to keep the suspension of solid, reaction mass is crossed separation assembly 2 along predetermined direction (for example the direction of arrow shown in the endless tube among the figure flows) the reaction mass slurry stream that flows, cross-flow filtration takes place in screen pipe 10, product is crossed cleaner liquid and is relied on the radially outflow of pressure differential from screen pipe 10, discharge through exporting 12, and the slurries of carrying after dense through chimney filter continue to recycle in endless tube 1, regenerate by 13 pairs of films of backpurge system.
The schematic diagram of the integrated reacting and separating device that Fig. 2 constitutes for being connected by two groups of endless tubes and separation assembly.Structural principle and Fig. 1 are basic identical, can operate under the same terms or different condition.Their difference is that the first reactor outlet clear liquid 12 introduces second reactor and continue reaction under the effect of pressure reduction, and raw material replenishes by 14 and adds, and catalyst can add by 14 or 15, and product is through 16 outflow reactors, and 13 is backpurge system.
The schematic diagram of Fig. 3 equipment that to be endless tube constitute with two separation assemblies in parallel.Its structure is basic identical with Fig. 1 with operation, and different is to adopt two components from assembly F
1And F
2Mode in parallel is operated.If when separation assembly needs chemical regeneration, can pass through F
1And F
2The mode of operation of switching.
Fig. 4 and Fig. 5 are respectively when screen pipe is ceramic-film tube and metal sintering pipe in the separation assembly, the input and output material schematic diagram of reaction mass, as we can see from the figure, slurry 20 to be separated enters screen pipe after distributing, under pressure differential promotes, cross-flow filtration, product clear liquid flow out and compile the back 21 from screen pipe and flow out from exporting 22, and the slurries of carrying after dense flow out and continue to turn round in equipment through exporting 23.Among the figure, adopt encapsulant 24 to seal to prevent that slurry from leaking to product clear liquid side.The 11st, the separation assembly shell.
Fig. 6 and Fig. 7 are respectively Fig. 4 and Fig. 5 generalized section at A-A and B-B place.19 separator tubes are housed in the separation assembly among Fig. 6, and every separator tube has a kind of situation of 19 passages, and 31 is runner among the figure, and 32 is screen pipe, and the number of tubes of separation assembly, number of active lanes and size are not subjected to above-mentioned restriction, can select as required; 19 pipes are arranged in the separation assembly among Fig. 7, and 33 is runner among the figure, and 34 is the thickness of screen pipe, and the number of tubes in the separation assembly, number of active lanes and size are not subjected to above-mentioned qualification, can require selected according to actual separation.
Claims (10)
1. one kind is used for solid-liquid, the integrated reacting and separating device of the heterogeneous reaction that solid-liquid-liquid and part are gas-liquid-solid, it is characterized in that this equipment comprises endless tube (1) and separation assembly (2), endless tube (1) forms a closed circuit with separation assembly (2), circulating pump (3) is set on the endless tube (1), provide energy to make reaction mass circulation in the loop of endless tube (1) and separation assembly (2) formation, wherein endless tube (1) is provided with raw material and adds inlet (4), solid catalyst adds inlet (5), material unloads outlet (6), heat-exchange system (7), the top of endless tube (1) is provided with liquid and collects balancer (8) and balance flue (9), endless tube length and heat exchange area visual response condition and decide; Separation assembly (2) is made of screen pipe (10) and housing (11), the screen pipe number is determined by the needed filter area of separation process, the setting of screen pipe (10) makes reaction mass carry out Separation of Solid and Liquid in the mode of cross-flow, reaction mass is isolated product therein, product is discharged by outlet (12), the slurries of carrying after dense continue to circulate in endless tube, separation assembly (2) is provided with backwashing system (13), screen pipe (10) is carried out back flush to recover filtration flux, the aperture that wherein said screen pipe (10) is selected from film is the inorganic film tube of 4nm-50 μ m, and perhaps being selected from the aperture is the metal sintering pipe of 0.5 μ m-200 μ m.
2. according to the equipment of claim 1, wherein said circulating pump (3) is an axial-flow pump.
3. according to the equipment of claim 1, wherein said raw material adds inlet (4) and is provided with one or more at the diverse location place of endless tube (1).
4. according to the equipment of claim 1, wherein said heat-exchange system (7) is the form of chuck, and cooling agent or heat donor fluid carry out heat exchange with reaction mass in chuck.
5. according to the equipment of claim 1, wherein said inorganic film tube is selected from ceramic-film tube, metal film pipe or carbon film of molecular sieve pipe.
6. according to the equipment of claim 5, wherein said ceramic-film tube, single have a runner that a plurality of diameters are 3-10mm.
7. according to the equipment of claim 5, wherein said metal film pipe is a runner.
8. according to the equipment of claim 1, it is characterized in that adopting at least two group endless tubes and separation assembly to be in series.
9. according to the equipment of claim 1, it is characterized in that having multicomponent to connect with series, parallel or series-parallel mode from assembly.
10. according to the equipment of claim 1, it is characterized in that multicomponent connects with parallel way from assembly, handover operation.
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| CN2006100890386A CN101116804B (en) | 2006-07-31 | 2006-07-31 | Integrated reacting and separating device |
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|---|---|---|---|
| CN2006100890386A CN101116804B (en) | 2006-07-31 | 2006-07-31 | Integrated reacting and separating device |
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| CN101116804A CN101116804A (en) | 2008-02-06 |
| CN101116804B true CN101116804B (en) | 2010-06-23 |
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|---|---|---|---|---|
| CN101391196B (en) * | 2008-10-31 | 2011-09-14 | 神华集团有限责任公司 | Extraction method of heavy fraction of ft synthetic product from slurry bed reactor |
| CN102311326A (en) * | 2010-07-06 | 2012-01-11 | 东营远大化工有限公司 | Method for preparing cyclohexenyl cyclohexanone with high conversion rate |
| CN102151520A (en) * | 2010-12-21 | 2011-08-17 | 湘潭大学 | Gas-liquid-solid or liquid-solid heterogeneous catalytic reaction method |
| CN102773048B (en) * | 2011-05-09 | 2017-06-06 | 波利玛利欧洲股份公司 | Produce the Ammoximation reaction device of cyclohexanone oxime |
| CN103663624B (en) * | 2012-09-14 | 2015-12-16 | 浙江中凯瑞普环境工程股份有限公司 | A kind of process for purification of oil field reinjection water |
| CN103708426B (en) * | 2014-01-08 | 2015-07-29 | 石祖嘉 | Anthraquinone oxydol production apparatus |
| CN105108883B (en) * | 2015-08-31 | 2018-02-09 | 佛山市佛冠义齿有限公司 | A kind of filling forming method of ceramic product |
| CN108970409A (en) * | 2018-07-26 | 2018-12-11 | 河南省亚龙超硬材料有限公司 | It is a kind of for being classified the device of diadust |
| CN113082977B (en) * | 2021-04-06 | 2021-11-30 | 江苏舒源空调制造有限公司 | Efficient waste gas treatment system and process |
| CN115055135B (en) * | 2022-07-05 | 2023-10-24 | 福建福豆新材料有限公司 | Trimethyl boron preparation system |
| CN115231741B (en) * | 2022-08-27 | 2023-11-28 | 西南石油大学 | Shale gas fracturing flowback fluid oxidation separation synchronous treatment method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1041299C (en) * | 1991-10-16 | 1998-12-23 | 成都科技大学 | Integrated meutralizing and concentrating device for producing phospham |
| CN2393618Y (en) * | 1999-09-29 | 2000-08-30 | 中国石油化工集团公司 | Filtering apparatus |
| US6239235B1 (en) * | 1997-07-15 | 2001-05-29 | Phillips Petroleum Company | High solids slurry polymerization |
| CN2524819Y (en) * | 2001-12-24 | 2002-12-11 | 熊天渝 | Semi dry type fume desulfurizing and dust-removing integrated device with solid and gas recirculation |
| CN1108906C (en) * | 2000-06-30 | 2003-05-21 | 隋贤栋 | Gradient ceramic-film tube and its preparation |
-
2006
- 2006-07-31 CN CN2006100890386A patent/CN101116804B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1041299C (en) * | 1991-10-16 | 1998-12-23 | 成都科技大学 | Integrated meutralizing and concentrating device for producing phospham |
| US6239235B1 (en) * | 1997-07-15 | 2001-05-29 | Phillips Petroleum Company | High solids slurry polymerization |
| CN2393618Y (en) * | 1999-09-29 | 2000-08-30 | 中国石油化工集团公司 | Filtering apparatus |
| CN1108906C (en) * | 2000-06-30 | 2003-05-21 | 隋贤栋 | Gradient ceramic-film tube and its preparation |
| CN2524819Y (en) * | 2001-12-24 | 2002-12-11 | 熊天渝 | Semi dry type fume desulfurizing and dust-removing integrated device with solid and gas recirculation |
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