CN202823321U - Slurry bed reaction and separation device - Google Patents
Slurry bed reaction and separation device Download PDFInfo
- Publication number
- CN202823321U CN202823321U CN 201220538103 CN201220538103U CN202823321U CN 202823321 U CN202823321 U CN 202823321U CN 201220538103 CN201220538103 CN 201220538103 CN 201220538103 U CN201220538103 U CN 201220538103U CN 202823321 U CN202823321 U CN 202823321U
- Authority
- CN
- China
- Prior art keywords
- bed reactor
- phase separation
- paste state
- state bed
- communicated
- 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 - Lifetime
Links
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a slurry bed reaction and separation device which comprises a slurry bed reactor (2), a multiphase separating tank (4), a settling tank (8) and a filtering component (12), wherein the upper part of the slurry bed reactor (2) is communicated with the multiphase separating tank (4) by a down-pipe (5); the bottom of the multiphase separating tank (4) is communicated with the slurry bed reactor (2) by a return pipe (6); the multiphase separating tank (4) arranged on the top of the return pipe is communicated with the settling tank (8); the upper part of the settling tank (8) is communicated with the filtering component (12); a slurry outlet of the filtering component (12) is communicated with the lower part of the settling tank (8) by a pipeline; and a liquid discharge hole (17) of the filtering component (12) is a liquid product outlet. Compared with the prior art, the slurry bed reactor has the characteristics of being reasonable in structure, high in separation efficiency and capable of continuously and stably running for a long period.
Description
Technical field
The utility model relates to a kind of gas-liquid-solid phase reaction separation equipment, more particularly, relate to a kind of paste state bed reactor and follow-up liquid solid particle continuous separate from equipment.
Background technology
Paste state bed reactor is a kind of gas-liquid commonly used (slurry) haptoreaction equipment, has high liquid storage amount.For the very large catalytic reaction process of reaction heat, use paste state bed reactor can effectively remove reaction heat, the isothermal operation of realization response device guarantees the normal operation of reactor, therefore is widely used in chemical process.
In paste state bed reactor, in order to eliminate the impact of diffusion, generally adopt tens microns even more fine grain catalyst, but also brought liquid reaction product to separate this difficult problem with catalyst granules thereupon.How effectively to realize liquid-solid separation, become the key technology in using the slurry reactor process.
The liquid-solid separation of paste state bed reactor catalyst slurry is generally carried out outside reactor, and the slurries that contain catalyst must use specific pump to carry, and the catalyst of separating still need to send back in the reactor with the slurries form.This process is easy to cause the breakage of catalyst granules, thereby the long-time continuous operation of reactor is brought problem.
Filtering technique is the common method of obtaining high separating efficiency.Press liquid form, filtration is divided into dead-end filtration and cross-flow filtration, compares traditional dead-end filtration, and the cross-flow filtration filter cake is difficult for piling up, and filter cycle is long, is the emphasis of studying at present.
US6068760, WO02/097007A2 all disclose and have adopted sedimentation techniques to realize the method for liquid-solid separation in paste state bed reactor, reacted slurries are drawn reactor, behind a sedimentation pipe, slurries enter settling tank and carry out sedimentation, supernatant liquor is discharged as product, and the thick slurry Returning reactor circulation of a large amount of catalyst granules is contained in lower floor.
The disclosed separation method of EP1405664A1 is that reacted slurries are directly introduced settling tank, sedimentation is provided with baffle plate in filling with, and height of baffle plate is higher than liquid level in the settling tank, therefore after slurry stream is crossed the slit of baffle plate and tank base, the clear liquid rising flows out above settling tank, and contains the underflow of particle in the outlet Returning reactor main body of settling tank bottom.
CN1600412A discloses a kind of liquid-solid separation system, and one or more layers equipment for separating liquid from solid as in the reactor, is realized the purpose of Separation of Solid and Liquid by filtration.Taken so a large amount of space reactors, and solid-liquid separation unit energy and the quality transmission of reaction, poor effect have been affected in the reactor body zone.
US2005/0027021 discloses a kind of liquid-solid separation system, realize liquid-solid separation by the filter element that vertical placement is set outside reactor, what play main filtration is the filter cake that is deposited on the filter element, regulates the thickness of filter cake by regulating the slurries flowing velocity.But because being design, element space size of living in determined, come controlled filter speed so that adjustable range is very limited by the outside slurry flow rate of regulating element merely, and fine grained easily stops up screen pipe and do not have effective back-flushing method to make filter process be difficult to realize serialization.
US2005/0000861 discloses a kind of filter element that can be placed on inside reactor and/or outside, this element is divided into coarse filtration district and fine filtering district, and the two is coaxial with vertically placement of footpath, block oarse-grained catalyst outside filtering area in coarse filtration district, top, Returning reactor recycles again again, carries out further isolated by filtration and can directly enter the fine filtering district that is located at below the coarse filtration district through the filtrate of coarse filtration.This solid separation method need to be by exterior power, and detailed back-flushing method is not provided, and is difficult to realize that liquid-solid continuous effective separates.
Utilize merely as can be known the method for filtering to be difficult to realize continued operation by above analysis, also can cause the catalyst solid abrasion of particles serious even realized continued operation, affect separative efficiency, also can make equipment complicated, investment and operating cost increase.
The utility model content
The purpose of this utility model provides a kind of slurry reactor and liquid-solid continuous separation equipment, is used for gas-liquid-solid phase reaction and Separation of Solid and Liquid process, can continued operation, and can discharge the catalyst granules of the fragmentation of wearing and tearing.
The slurry reactor that the utility model provides and separation equipment comprise paste state bed reactor 2, multi-phase separation tank 4, settling tank 8 and filter assemblies 12; Paste state bed reactor 2 tops are communicated with multi-phase separation tank 4 middle parts through down-pipe 5, the bottom of multi-phase separation tank 4 is communicated with paste state bed reactor through return duct 6, the top of multi-phase separation tank 4 is communicated with the paste state bed reactor top, multi-phase separation tank top is communicated with settling tank 8 middle parts, settling tank 8 tops are communicated with filter assemblies 12, the slurries outlet of filter assemblies 12 is communicated with settling tank 8 bottoms, and the clear liquid discharging opening 17 of filter assemblies 12 is the fluid product outlet.
The slurry reactor that the utility model provides and the beneficial effect of separation equipment are:
The slurry reactor that the utility model provides and separation equipment in slurry reactor district outer setting multi-phase separation tank, settling tank, filter assemblies, and the blowback system that is used for filter medium regeneration, simple in structure, separative efficiency is high, filter medium is easy to regeneration, and is practical.Can realize that solid catalyst particle separates with the continuous high-efficient of liquid form product, can also make because of the broken solid catalyst particle of wearing and tearing and discharge continuously reaction system, convenient and flexible operation.
Description of drawings
The slurry reactor that accompanying drawing provides for the utility model and the structural representation of separation equipment.
Among the figure, the 1-gas distributor; The 2-paste state bed reactor; The 3-exhaust outlet; 4-multi-phase separation tank; The 5-down-pipe; The 6-return duct; The 8-settling tank; The outlet of 11-concentrated slurry; The 12-filter assemblies; The 13-filter medium; The 15-pump; The 17-liquid outlet opening; 18-blowback entrance; 19-slurries charge door; 7,9,10,14,16-pipeline.
The specific embodiment
Below specify slurry reactor that the utility model provides and the specific embodiment of separation equipment, in this manual, involved term " top " refers to the top part of this container; " top " refers to 70% ~ 100% part of container total height from the bottom to top, " middle part " refers to 30% ~ 70% part of container total height from the bottom to top, " bottom " refers to 0 ~ 30% part of container total height from the bottom to top, and " bottom " refers to this container lowermost end part.
The slurry reactor that the utility model provides and separation equipment comprise paste state bed reactor 2, multi-phase separation tank 4, settling tank 8 and filter assemblies 12; Paste state bed reactor 2 tops are communicated with through down-pipe 5 multi-phase separation tanks 4 middle parts, the bottom of multi-phase separation tank 4 is communicated with paste state bed reactor through return duct 6, the top of multi-phase separation tank 4 is communicated with the paste state bed reactor top, multi-phase separation tank top is communicated with settling tank 8 middle parts, settling tank 8 tops are communicated with filter assemblies 12, the slurries outlet of filter assemblies 12 is communicated with settling tank 8 bottoms, and the clear liquid discharging opening 17 of filter assemblies 12 is the fluid product outlet.
In the slurry reactor and separation equipment that the utility model provides, the top of described multi-phase separation tank 4 is communicated with through pipeline with the top of described paste state bed reactor.
In the slurry reactor and separation equipment that the utility model provides, can in down-pipe and return duct, not deposit for guaranteeing solid particle.Preferred down-pipe and return duct are and are obliquely installed, with the angle of level reference all greater than the angle of repose of solid particle.
The caliber of described down-pipe 5 is 0.5 ~ 6:1 with the ratio of the caliber of return duct 6, preferred 1 ~ 5:1, more preferably 1.5 ~ 3:1.Preferentially select larger-diameter down-pipe 5, being convenient to thicker particle relies on gravitational settling slowly to flow to the bottom of multi-phase separation tank 4 along the lower wall of down-pipe herein, bubble can gather and float herein simultaneously, make major part can return paste state bed reactor 2, play the effect of preliminary gas-liquid separation, elimination bubble.
In the slurry reactor and separation equipment that the utility model provides, the bottom of described paste state bed reactor 2 is provided with gas distributor 1, and vapor-phase reactant enters in the paste state bed reactor through gas distributor 1, and the top of described paste state bed reactor is provided with exhaust outlet 3.
Described multi-phase separation tank 4 bottoms are communicated with paste state bed reactor middle part or bottom through return duct 6, are provided with slurries charge door 19 on the described return duct.
In the slurry reactor and separation equipment that the utility model provides, described multi-phase separation tank can be for one or more.When multi-phase separation tank when being a plurality of, a plurality of multi-phase separation tanks can be arranged in around the level paste state bed reactor, so that the pressure between balance paste state bed reactor and the multi-phase separation tank.In use, because the initial gross separation of gas-liquid-solid three-phase can be realized in settlement action multi-phase separation tank inside, described multi-phase separation tank inside can be divided into gas enrichment region, reduction paste liquid zone and thickened pulp liquid zone from the top to the bottom.Preferably, in order to realize the better separating effect of gas-liquid-solid three-phase in the multi-phase separation tank, the cross-sectional area of multi-phase separation tank is 0.1 ~ 10:1 with the ratio of the cross-sectional area of paste state bed reactor, preferred 0.3 ~ 5:1, more preferably 0.6 ~ 3:1.When a plurality of multi-phase separation tank was arranged, the cross-sectional area of described multi-phase separation tank was a plurality of multi-phase separation tank cross-sectional area sums.
In the slurry reactor and separation equipment that the utility model provides, described multi-phase separation tank middle part is communicated with settling tank 8 middle parts; Described settling tank 8 tops are communicated with the multi-phase separation tank top; The bottom of described settling tank 8 is provided with concentrated slurry outlet 11.In use, because settlement action, described settling tank 8 inside are gas enrichment region, reduction paste liquid zone and thickened pulp liquid zone partly from the top on earth.The gas at settling tank 8 tops can enter the multi-phase separation tank through pipeline, discharges through the exhaust outlet at paste state bed reactor top again.
The concentrated slurry outlet 11 of described settling tank bottom is in order to discharge the high concentration slurries behind sedimentation concentration.Described concentrated slurry outlet 11 and slurries charge door 19 are used for processing more neatly catalyst granules.Replenish the slurries that are mixed with fresh solid particle catalyst by slurries charge door 19.Simultaneously, when the catalyst granules in the reactor because drawing small and during in the enrichment of the bottom of settling tank 8, can export 11 by concentrated slurry and discharge.
In the slurry reactor and separation equipment that the utility model provides, described filter assemblies 12 inside arrange filter medium, and the filter assemblies inner space is divided into slurries district and filtrate district, and described filter medium can or be filter for screen pipe.
Described settling tank 8 tops are connected with described filter assemblies 12, the clear liquid after the sedimentation in the settling tank is introduced in the filter assemblies filtered, and further remove solid granule, obtain liquid-phase product.Simultaneously, the slurries district of described filter assemblies 12 is connected with settling tank 8 bottoms, and the slurries after concentrated are sent back in the settling tank 8.In filter assemblies 12, the liquid in slurries district passes filter medium and enters the filtrate district, and the filtrate district is communicated with fluid product discharging opening 17, with after filtering clear liquid send as product as liquid.
Described filtrate district also is connected with for the blowback lines 18 and the valve that filter medium are carried out backwash, with the switching between controlled filter and the backwash.On the connecting line of settling tank and filter assemblies slush pump can also be set, to increase the slurries mobilization dynamic.
In the slurry reactor and separation equipment that the utility model provides, described filter medium is selected from the filtering material of sintered metal mesh micropore filter material, sintering metal powder micropore filter material, metal micro-holes membrane material, sintered metal fiber poromerics, micropore ceramics material, ceramic membrane materials or other type.The utility model is to the not restriction of material of filter medium.
The slurry reactor that the utility model provides and the application process of separation equipment, unstripped gas enters paste state bed reactor after being distributed by gas distributor, with the slurries mixing afterreaction in the paste state bed reactor, upwards flow simultaneously, the slurries that then are mingled with the part minute bubbles flow in the multi-phase separation tank through down-pipe; In the paste state bed reactor, be gas enrichment space on the aperture position of down-pipe, be used for the gas that the unreacted gas of enrichment and reaction generate.In the multi-phase separation tank, be mingled with alveolate slurries and rely on the preliminary sedimentation of Action of Gravity Field, the space is gas enrichment region, reduction paste liquid zone and thickened pulp liquid zone partly from the top on earth in the multi-phase separation tank; Wherein the gas enrichment region is connected with the gas enrichment space of paste state bed reactor.Sustainable participation reacts the catalyst of larger particles in the paste state bed reactor along with the slurries main body is returned through return duct after the enrichment of multi-phase separation tank.A small amount of broken subparticle can rise along with slurries are slow and the final settling tank 8 that flows into.In this process, owing to containing a large amount of bubbles in the paste state bed reactor, its internal density is reduced, thereby formed a density contrast with the slurries in the multi-phase separation tank, cause slurries between paste state bed reactor and multi-phase separation tank, to circulate, thereby guaranteed the continuous displacement of concentrated slurry in the multi-phase separation tank, guaranteed simultaneously carrying out continuously of multi-phase separation process.
In settling tank, the slurries that contain a small amount of broken subparticle can further sedimentation, in settling tank from the top on earth part be gas enrichment region, reduction paste liquid zone and thickened pulp liquid zone.Wherein the gas enrichment region is connected with the top of multi-phase separation tank; The slurries of reduction paste liquid zone are introduced in the filter assemblies through pump and are carried out isolated by filtration, and the concentrated slurry after filtering in the filter assemblies returns the bottom thickened pulp liquid zone enrichment of settling tank through pipeline, and finally discharge through the concentrated slurry outlet.
In filter assemblies, slurries from settling tank axially flow downward along filter assemblies, wherein a part of liquid passes through filter medium under the promotion of filter medium both sides pressure reduction, and finally draws as product, and the micro-solid particle then flows back to the settling tank bottom with slurries.Carry out filtering medium layer both sides pressure reduction thickening and rise along with filter cake with reaction, when pressure reduction is higher than setting value, backwashing system is started working, this moment, the liquid outlet opening late gate was closed, valve opening on the blowback lines, liquid outlet opening and recoil pipeline are communicated with, the backwash medium is the back flush filtering medium layer under the reverse differential pressure that adds promotes, the reverse differential pressure that removes with filter cake constantly reduces, when being lower than another setting value, flushing process finishes, the valve closing on this moment blowback lines, and system returns to normal operating state.Wherein said backwash medium can be the product clear liquid, also can be distillate, the preferred product clear liquid.
The applicable gas, liquid, solid phase reaction of the method that the utility model provides also need to be isolated the chemical reaction process of solid particle from slurries, such as synthetic (Fischer-Tropsch) process of the hydrocarbon oil hydrogenation, certain embodiments and the Fischer-Tropsch that adopt suspension bed or oar state bed reactor.
Specify the continuous separation method that paste state bed reactor that the utility model provides is used for Fischer-Tropsch building-up process liquid and solid particle below in conjunction with accompanying drawing, but therefore the utility model is not restricted.
As shown in drawings: the reactant synthesis gas enters in the paste state bed reactor with wherein slurries through gas distributor 1 from the bottom of paste state bed reactor 2 and mixes, contact with catalyst granules in the slurries, and carrying out chemical reaction, product and unnecessary reactant rise to the top of paste state bed reactor 2 with catalyst granules; Unreacted reactant gas separates with slurries herein with gaseous product, discharges from the gas vent 3 at top, and catalyst granules then enters in the multi-phase separation tank 4 through down-pipe 5 with the form of liquid with slurries.In multi-phase separation tank 4, gas-liquid-solid three-phase is sedimentation in the tank because density does not coexist, part is gas enrichment region, reduction paste liquid zone and thickened pulp liquid zone on earth from the top, the gas of enrichment is sent into paste state bed reactor 4 top gas enrichment spaces through pipeline 7, the slurries of thickened pulp liquid zone flow downward and return paste state bed reactor 2 through return duct 6, the dilution slurries that contain micro-minute bubbles and crushed particles then can be introduced into and carry out secondary settlement in the settling tank 8, realize further gas-liquid-solid three-phase separation.In the settling tank 8, the gas of enrichment is introduced multi-phase separation tank 4 through pipeline 9, the slurries that are rich in solid particle are discharged by concentrated slurry outlet 11, the slurries that contain micro-broken solid particle flow through filter assemblies 12 by pipeline 14 from top to bottom through pump 15, under tubular filtering medium 13 inside and outside differential pressures promote, liquid can radially pass filter medium, and finally draws as the product clear liquid.Solid particle then is arrested on the filter medium inwall, because the souring of liquid flow, part filter cake on the filter medium inwall constantly comes off and flows downward with slurries and turns back in the settling tank 8 through pipeline 16, the filter cake of part difficult drop-off can be trapped on the inwall of filter medium, along with constantly thickening of filter cake, pressure reduction between filter medium is inside and outside rises, and when pressure reduction was higher than 0.35MPa, backwashing system was started working.Under the promotion that adds reverse differential pressure, also radially ecto-entad is by filter medium in the filtrate district of backwash medium introducing filter assemblies, and the filter cake that is attached on the filter medium inwall is sprung back in the slurries, and returns settling tank 8 along with slurries flow downward.When the pressure reduction inside and outside the filter medium was lower than 0.1MPa, flushing process finished, and system returns to normal operating state.
The following examples are further described the method that the utility model provides, but therefore do not limit the utility model.
Embodiment
The multi-phase separation tank that adopts in force and the Area Ratio of reactor are 1:1, down-pipe 5 is 2:1 with the diameter ratio of return duct 6, and the placement angle of down-pipe and return duct and level reference is 45 degree, filter medium is the sintered porous metal chimney filter, its external diameter is 50mm, long is 1000mm, and average pore size is 2 μ m.The particle size range of the catalyst that adopts is 20～100 μ m, and synthesis gas enters bed by reactor bottom with the form of bubbling in this process, under operating condition, generates liquid hydrocarbon.Unreacted synthesis gas separates with slurries fully with gas products after slurries rise to reactor head, and is discharged by exhaust outlet; The part slurries are introduced the multi-phase separation tank through down-pipe, and the slurries that contain damaged catalyst granules enter settling tank.In settling tank, the slurries that are rich in broken solid particle can be got rid of by discharge gate 11, after the slurries that contain micro-broken solid particle can be introduced filter assemblies and filter by pump, finally draw as product.A small amount of solid particle then is delayed on the filter medium tube wall and forms filter cake, because the souring of liquid flow, the part filter cake on the inner pipe wall constantly comes off and gets back to tedge with downward liquid flow.The filter cake of part difficult drop-off can be stayed on the chimney filter inwall, along with constantly thickening of filter cake, when the pressure reduction between the inner and outer pipes surpassed 0.35MPa, the backwash medium was introduced outer tube, the filter cake that is attached on the inner tubal wall is washed in the slurries, and returns tedge along with slurries flow downward.This process continues several seconds, and when the pressure reduction between inner and outer pipes was lower than 0.1MPa, system returned to normal operating state.In this process, the slurry solid content that is drained into settling tank by the multi-phase separation tank is 900 μ g/ml, and solid content is less than 3 μ g/ml in the liquid form product after filtering, and the maximum gauge of particle is 2 μ m.Separative efficiency is more than 99%.
Wherein solid content adopts weight method to measure in the slurries.
Separative efficiency is calculated by following formula:
η=（S
m-S
f）/S
m
Wherein: S
mSolid content in the=raw material (slurries before filtering); S
fSolid content in the=product (cleaner liquid).
Claims (12)
1. a slurry reactor and separation equipment is characterized in that, comprise paste state bed reactor (2), multi-phase separation tank (4), settling tank (8) and filter assemblies (12); Paste state bed reactor (2) top is communicated with multi-phase separation tank (4) middle part through down-pipe (5), the bottom of multi-phase separation tank (4) is communicated with paste state bed reactor through return duct (6), the top of multi-phase separation tank (4) is communicated with the paste state bed reactor top, multi-phase separation tank top is communicated with settling tank (8) middle part, settling tank (8) top is communicated with filter assemblies (12), the slurries outlet of filter assemblies (12) is communicated with settling tank (8) bottom, and the clear liquid discharging opening (17) of filter assemblies (12) is the fluid product outlet.
2. according to the equipment of claim 1, the top of described multi-phase separation tank (4) is communicated with through pipeline with the top of described paste state bed reactor (2).
3. according to the equipment of claim 1, it is characterized in that, described down-pipe (5) and return duct (6) are and are obliquely installed, with the angle of the level reference angle of repose greater than solid particle.
4. according to the equipment of claim 1, it is characterized in that, the ratio of the caliber of the caliber of described down-pipe (5) and return duct (6) is 0.5 ~ 6:1.
5. according to the equipment of claim 4, it is characterized in that, the ratio of the caliber of the caliber of described down-pipe (5) and return duct (6) is 1 ~ 5:1.
6. according to the equipment of claim 5, it is characterized in that, the ratio of the caliber of the caliber of described down-pipe (5) and return duct (6) is 1.5 ~ 3:1.
7. according to the equipment of claim 1, it is characterized in that, described multi-phase separation tank (4) is 0.1 ~ 10:1 with the ratio of the sectional area of paste state bed reactor (2).
8. according to the equipment of claim 7, it is characterized in that, described multi-phase separation tank (4) is 0.3 ~ 5:1 with the ratio of the sectional area of paste state bed reactor (2).
9. according to the equipment of claim 8, it is characterized in that, described multi-phase separation tank (4) is 0.6 ~ 3:1 with the ratio of the sectional area of paste state bed reactor (2).
10. according to the equipment of claim 1, it is characterized in that, the bottom of described paste state bed reactor (2) arranges gas distributor (1).
11. the equipment according to claim 1 is characterized in that, the top of described paste state bed reactor (2) arranges exhaust outlet (3).
12. the equipment according to claim 1 is characterized in that, is provided with slurries charge door (19) on the return duct (6) of described connection multi-phase separation tank (4) and paste state bed reactor (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220538103 CN202823321U (en) | 2012-10-19 | 2012-10-19 | Slurry bed reaction and separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220538103 CN202823321U (en) | 2012-10-19 | 2012-10-19 | Slurry bed reaction and separation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202823321U true CN202823321U (en) | 2013-03-27 |
Family
ID=47935121
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220538103 Expired - Lifetime CN202823321U (en) | 2012-10-19 | 2012-10-19 | Slurry bed reaction and separation device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202823321U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854859A (en) * | 2018-07-27 | 2018-11-23 | 中化蓝天霍尼韦尔新材料有限公司 | A kind of suspension liquid phase reaction unit and operation method |
| CN111905659A (en) * | 2020-08-24 | 2020-11-10 | 中国科学院青岛生物能源与过程研究所 | Method and device for extracting cleaning liquid from slurry bed |
| WO2021051426A1 (en) * | 2019-09-19 | 2021-03-25 | 中国科学院青岛生物能源与过程研究所 | Outer circulation slurry bed reactor |
-
2012
- 2012-10-19 CN CN 201220538103 patent/CN202823321U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854859A (en) * | 2018-07-27 | 2018-11-23 | 中化蓝天霍尼韦尔新材料有限公司 | A kind of suspension liquid phase reaction unit and operation method |
| CN108854859B (en) * | 2018-07-27 | 2023-08-18 | 中化蓝天霍尼韦尔新材料有限公司 | Suspension gas-liquid phase reaction device and operation method |
| WO2021051426A1 (en) * | 2019-09-19 | 2021-03-25 | 中国科学院青岛生物能源与过程研究所 | Outer circulation slurry bed reactor |
| CN111905659A (en) * | 2020-08-24 | 2020-11-10 | 中国科学院青岛生物能源与过程研究所 | Method and device for extracting cleaning liquid from slurry bed |
| CN111905659B (en) * | 2020-08-24 | 2022-04-19 | 中国科学院青岛生物能源与过程研究所 | Method and device for extracting cleaning liquid from slurry bed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN203018064U (en) | Slurry-bed loop reaction and separation equipment | |
| CN101314120B (en) | Slurry bed reactor and uses thereof | |
| CN101081357A (en) | Slurry bed circulatory flow reactor and uses thereof | |
| CN201529520U (en) | Descending pipe structure of slurry bed ring current reactor for preventing clogging | |
| CN202173844U (en) | Reaction, sedimentation and filtration integrated device | |
| CN102451651B (en) | Slurry bed loop reactor and application thereof | |
| CN101116803A (en) | Slurry -bed reaction unit and method of use thereof | |
| CN205569936U (en) | Thick liquid attitude bed ft synthesis catalyst solid -liquid separation equipment | |
| CN102703712A (en) | Combined filtration process for recovering noble metal catalyst from fischer-tropsch synthesis products | |
| CN101708876A (en) | Hydraulic jet magnetic resin adsorptive reactor | |
| CN202823321U (en) | Slurry bed reaction and separation device | |
| CN201529435U (en) | Filter inner component of slurry bed reactor | |
| CN209501042U (en) | A kind of filter device | |
| CN104888668B (en) | A kind of F- T synthesis and the device and method separated | |
| CN102049222B (en) | Application method of loop slurry reactor adopting novel filtration module | |
| CN102232008B (en) | Method and system for handling slurries of varying liquid rates and solids content | |
| CN201586518U (en) | Downtake structure of slurry bed circulation flow reactor | |
| CN201776135U (en) | Structure of descending pipe with magnetic field for slurry bed circulation flow reactor | |
| CN203018065U (en) | Slurry-bed loop reactor and continuous separation equipment | |
| CN201558690U (en) | Inner filtering component for slurry bed reactor | |
| CN204746286U (en) | Thick liquid attitude bed reactor's ft synthesis result piece -rate system | |
| CN217041447U (en) | Double-fixed-bed medium filter | |
| CN201890820U (en) | Solid-liquid separation integrated equipment | |
| CN104888667B (en) | The Fischer-Tropsch synthetic piece-rate system and method for a kind of paste state bed reactor | |
| CN204569519U (en) | Poly-repelling crude oil storage tank sewage purification machinery |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130327 |
|
| CX01 | Expiry of patent term |