CN201701861U - Purge gas treatment device - Google Patents
Purge gas treatment device Download PDFInfo
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- CN201701861U CN201701861U CN2010202198739U CN201020219873U CN201701861U CN 201701861 U CN201701861 U CN 201701861U CN 2010202198739 U CN2010202198739 U CN 2010202198739U CN 201020219873 U CN201020219873 U CN 201020219873U CN 201701861 U CN201701861 U CN 201701861U
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Abstract
The utility model provides a purge gas treatment device, which sequentially comprises a first membrane separation device, a carbon monoxide conversion device, a decarburization device, a purification separator, a purified gas adsorber and a second membrane separation device. The first membrane separation device is internally provided with at least one membrane separation assembly, one side of the membrane separation assembly without permeated gas is connected with the carbon monoxide conversion device; the carbon monoxide conversion device comprises at least one conversion tower, the discharge end of which is connected with the decarburization device; the decarburization device comprises at least one absorption tower the discharge end of which is connected with the purification separator, and the outlet of the purification separator is connected with the purified gas adsorber; and the second membrane separation device is connected with the discharge port of the purified gas absorber and is internally provided with at least one membrane separation assembly. Compared with the prior art, by the treatment device, the utility model effectively recovers hydrogen and carbon monoxide in methanol synthesized purge gas and finally prepares natural gas through progressive treatment processes, thereby fully utilizing light hydrocarbon gases, such as methane and the like in the purge gas.
Description
Technical field
The utility model relates to Coal Chemical Industry and petroleum gas chemical field, is specifically related to the treating apparatus of a kind of methyl alcohol or gas and synthetic ammonia purge.
Background technology
Methyl alcohol is of many uses, for example can be used for making multiple organic products such as formaldehyde, acetic acid, chloromethanes, first ammonia in fields such as fine chemistry industries, also is one of important source material of agricultural chemicals and medicine.In addition, methyl alcohol can be used as novel clean fuel after deep processing, adds in the gasoline to make methanol gasoline.
At present, well known to a person skilled in the art that a kind of common technology of preparation methyl alcohol is to make unstrpped gas after the coal gasification, it is H that these unstrpped gas a series of purifications of process and compression process obtain main matter
2+ CO+CO
2Gas, carry out synthetic reaction then and make methyl alcohol.Have a certain amount of tail gas and discharge in said process, promptly methanol synthetic discharged gas delayed, its main component is methane and hydrogen, also contains a spot of carbon monoxide, carbon dioxide, nitrogen and other light hydrocarbon gas.Herein, the off-gas of being mentioned is the off-gas that methanol technics well known to those skilled in the art produces.For the valuable gases in methanol synthetic discharged gas delayed is reclaimed, the methanol synthetic discharged gas delayed method of multiple processing is disclosed in the prior art, wherein Chang Yong two kinds of methods are pressure swing absorption process and membrane separating method.
See also Fig. 1, be pressure swing absorption process process chart of the prior art.The cardinal principle of transformation absorption is to utilize the difference of the adsorption capacity of different components on adsorbent in the gas medium, and adsorbent carries out the specific components in the selective absorption gas when pressure raises, and desorption obtains regeneration gas when pressure reduces.See also Fig. 1, pressure-swing absorption apparatus comprises pretreatment unit, pressure-swing absorption apparatus, refining plant successively, methanol synthetic discharged gas delayedly at first in pretreatment unit, remove wherein contained methyl alcohol through water scrubber and separator, enter pressure-swing absorption apparatus then, gases such as methane wherein and carbon dioxide are adsorbed, and hydrogen component is not adsorbed.Methanol synthetic discharged gas delayedly obtain high concentration hydrogen at the adsorption tower cat head, and then handle through refining plant and to obtain purified hydrogen by adsorbent bed; Methane that is adsorbed and carbon dioxide etc. are then discharged at the bottom of the absorption Tata as desorption gas by regenerative process, and the gas firing that acts as a fuel falls.Though this method has the advantage that hydrogen purity height, pressure drop are little, hydrogen recovery rate is high of preparation, lost most of CO, the CO in the off-gas
2Deng available gas, and a large amount of methane that contain in the off-gas and other light hydrocarbon gas are not fully used yet.
See also Fig. 2, be membrane separating method process chart of the prior art.The operation principle that film separates is to utilize high molecular polymer (as polyimides or polysulfones) film to select " filtrations " feeding gas and reach the purpose of gas separation.When two or more admixture of gas passed through thin polymer film, therefore each gas component had different speed owing to have different dissolving diffusion coefficients in polymer when permeating by membranous wall, and the comparatively faster gas of infiltration rate has H
2O, H
2, He, CO
2, be commonly called as " fast gas "; The relatively slow gas of infiltration rate has nitrogen, CO, methane and other light hydrocarbon gas, is commonly called as " gas slowly ".Like this, gas component is separated into the infiltration gas of low pressure and the non-infiltration gas of high pressure after separating through film.
When utilizing the film separating treatment methanol synthetic discharged gas delayed, the most H in the off-gas
2, CO
2, portion C O etc. obtain at the bottom of tower as low-pressure permeability gas, through returning system for methanol synthesis after the hydrogen gas compressor compression; And most CH
4, N
2, Ar and small part H2, CO
2Fall through the gas firing that in factory, acts as a fuel after the step-down as the non-infiltration gas of high pressure with portion C O etc., both lost pressure and also wasted hydro carbons.
The utility model content
Problem to be solved in the utility model is to provide a kind for the treatment of apparatus of synthesis purge gas, by this treating apparatus, can reclaim the H in methanol synthetic discharged gas delayed or the gas and synthetic ammonia purge
2With available gas such as CO, can make full use of the light hydrocarbon gas such as methane in the off-gas again.
In order to solve above technical problem, the utility model provides a kind for the treatment of apparatus of off-gas, and described off-gas comprises methanol synthetic discharged gas delayed and/or gas and synthetic ammonia purge, and described treating apparatus comprises successively:
First membrane separation device is provided with a membrane separation assemblies at least in described first membrane separation device, non-infiltration gas one side of described membrane separation assemblies is connected with carbon monoxide conversion device;
Described carbon monoxide conversion device comprises at least one conversion tower, and the discharge end of described conversion tower is connected with decarbonization device;
Described decarbonization device comprises at least one absorption tower, and the discharging opening on described absorption tower is connected with decontaminating separator;
The gaseous phase outlet of described purge gas separator is connected with the purified gas absorber;
Described treating apparatus also comprises second membrane separation device that is connected with the discharging opening of described purified gas absorber, in described second membrane separation device at least one membrane separation assemblies is set.
Preferably, described carbon monoxide conversion device comprises middle temperature transformation tower and high temperature shift tower.
Preferably, before described middle temperature transformation tower, also be provided with the hot water saturator.
Preferably, described decarbonization device also comprises the decontaminating separator that is connected with described absorption tower.
Preferably, the port of export of described decontaminating separator further is provided with active carbon filter.
Preferably, described decarbonization device also comprises CO
2Regenerator.
Preferably, described second membrane separation device comprises first section membrane separation assemblies and second section membrane separation assemblies.
Preferably, before described first section membrane separation assemblies, also further be provided with mechanical filter.Preferably, first membrane separation assemblies of described second membrane separation device the outlet of non-infiltration gas be connected with the raw material gas inlet of described second membrane separation assemblies.
The utility model provides a kind for the treatment of apparatus of off-gas, and described off-gas is methanol synthetic discharged gas delayed and/or gas and synthetic ammonia purge.The utility model hydrogen of earlier off-gas being purified out in first membrane separation device, and then through carbon monoxide conversion device carbon monoxide is converted to hydrogen and carbon dioxide successively, sending into decarbonization device again carries out carbonization treatment and gets rid of carbon dioxide, get rid of hydrogen through second membrane separation device again, make methane and lighter hydrocarbons content then and reach natural gas more than 92%.The utility model uses above-mentioned treating apparatus, effective recycling hydrogen and the carbon monoxide in methanol synthetic discharged gas delayed, and make natural gas at last by treatment process step by step, made full use of the light hydrocarbon gas such as methane in the off-gas.
Description of drawings
Fig. 1 is the methanol synthetic discharged gas delayed device schematic diagram of transformation adsorption treatment in the prior art;
Fig. 2 is the methanol synthetic discharged gas delayed device schematic diagram of film separating treatment in the prior art;
The off-gas treating apparatus schematic diagram that Fig. 3 provides for the utility model.
The specific embodiment
In order further to understand the utility model, below in conjunction with embodiment the utility model preferred embodiment is described, but should be appreciated that these describe just to further specifying feature and advantage of the present utility model, rather than to the restriction of the utility model claim.
Please refer to Fig. 3, off-gas treating apparatus schematic diagram provided by the invention, off-gas of the present invention is methanol purge gas and/or gas and synthetic ammonia purge, be preferably methanol synthetic discharged gas delayed, described treating apparatus comprises first membrane separation device 11 successively, in the present embodiment, in first membrane separation device 11, be provided with one section separating film module.For diffusion barrier, can use macromolecule micro-porous film well known to those skilled in the art, material can be acetic acid esters, polyimides, polysulfones, cellulose, glass fibre, polytetrafluoroethylene (PTFE), polyolefin etc.For the quantity of separating film module, also one or more can be set, to reach higher separating effect, to this present invention and without particular limitation.
Described first membrane separation device is connected with carbon monoxide conversion device 12, and described carbon monoxide conversion device comprises the carbon monodixe conversion tower, and in this carbon monodixe conversion tower, following transformationreation well known to those skilled in the art takes place carbon monoxide:
Through after the above-mentioned transformationreation, CO changes into CO
2And generation H
2For the carbon monodixe conversion tower, the present invention is also without particular limitation, can use conversion tower well known to those skilled in the art, for example middle temperature transformation tower or low-temperature conversion tower.In the present embodiment, set gradually middle temperature transformation tower 12a and low-temperature conversion tower 12b, make CO carry out middle temperature transformation earlier and generate CO
2, generate CO through low-temperature conversion again
2The middle temperature transformation temperature is preferably 300 ℃～500 ℃, and the low-temperature conversion temperature is preferably 180 ℃～260 ℃, more preferably 190 ℃～220 ℃.In the carbon monodixe conversion tower apparatus, also further being provided with hot water saturator 12c is used for carrying out humidification from film gas separated component, so that carry out the carbon monodixe conversion reaction, in carbon monoxide conversion device, also further be provided with the preheater (not shown) that is used for preheating.
Described carbon monoxide conversion device 12 is connected with decarbonization device 13, described decarbonization device 13 is used for absorbing carbon dioxide, decarbonization device can be provided with the pressure swing adsorption decarbonization device, and MDEA (N methyl diethanolamine) decarbonization device also can be set, and preferably uses the MDEA decarbonization device.After the conversion gas (treating decarburization gas stream) of discharging from carbon monoxide conversion device is admitted to decarbonization device, can enter from bottom, decarburization absorption tower, from bottom to top by decarburization absorption tower 13a; MDEA solution through regeneration enters from top, decarburization absorption tower, and from top to bottom by the decarburization absorption tower, the decarburization gas stream for the treatment of of reverse flow fully contacts in the decarburization absorption tower with MDEA solution, treats the CO in the decarburization gas stream
2Be absorbed and enter MDEA solution, unabsorbed other gas component is drawn from top, decarburization absorption tower.
Described decarbonization device 13 also comprises the decontaminating separator 13b that is connected with top, decarburization absorption tower, be used for removing the MDEA solution of the purified gas of discharging from the absorption tower (be absorbed carbon dioxide after gas stream), decontaminating separator can use decontaminating separator well known to those skilled in the art, the port of export of described decontaminating separator further is provided with clarifier absorber 13d, described purification absorber is preferably active carbon filter, its effect is in order to remove the water in the decarburization gas stream, preventing that water and carbon dioxide reaction from producing carbonic acid, thereby corrode second membrane separator.Gas through decarburization flows after the discharge of top, decarburization absorption tower, and the separating treatment through decontaminating separator enters the purification absorber again, further to remove MDEA solution and the moisture in the gas stream.
Be adsorbed with CO
2The MDEA rich solution discharge from decarburization absorption tower bottom through entering after the step-down and directly be sent to regenerator 13c top after the poor rich liquid heat exchanger heating and carry out hot reactivation, the regeneration gas that obtains enters the regeneration separators (not shown), CO after through cooling
2Can discharge from the regeneration separators top, the phegma of regeneration separators bottom returns the regenerator top; Draw lean solution from the regenerator bottom, can reenter the decarburization absorption tower after lean solution is boosted through cooling and absorb CO
2, MDEA absorption plant and operation all belong to prior art well known to those skilled in the art, repeat no more once more.
Described decarbonization device is connected with second membrane separation device 14, in the present embodiment, be provided with first section membrane separation assemblies 14a and second section membrane separation assemblies 14b in second membrane separation device, described first section membrane separation assemblies is used for that described the 3rd object gas stream is carried out film and separates; Described second section membrane separation assemblies is used for that the non-infiltration gas after described first section membrane separation assemblies separation is carried out film and separates, and the non-infiltration gas outlet of first membrane separation assemblies of described second membrane separation device is connected with the raw material gas inlet of second membrane separation assemblies.Mechanical filter device 14c can also be set before first section membrane separation assemblies, be used for removing the mist of the gas stream after the decarburization.
Form described the 4th object gas stream by the non-infiltration gas after described second section membrane separation assemblies separation; Infiltration gas after separating by described first section membrane separation assemblies with separates by described second section membrane separation assemblies after infiltration gas be compressed mixing and form second hydrogen-rich gas stream, be sent to methanol synthesizer then.The methane and the lighter hydrocarbons composition of the 4th object gas stream can reach more than 92%, can directly be sent to industry or civilian as natural gas, also can further compress as natural gas used for automobile CNG.
Below in conjunction with the methanol synthetic discharged gas delayed processing method specific embodiment of above-mentioned treating apparatus explanation the present invention.
Herein, all gas contents of mentioning are percent by volume.The off-gas composition of discharging from methanol synthesizer comprises hydrogen, carbon monoxide, carbon dioxide, methane, nitrogen and other lighter hydrocarbons, and wherein hydrogen content is preferably 40%～85%, is preferably 58%～63%; The content of carbon monoxide is 1%～10%, is preferably 6%～7.5%; The content of carbon dioxide is 1%～10%, more preferably 1.2%～1.8%; Methane and other lighter hydrocarbons and be 10%～60%, more preferably 30%～32%, surplus is N
2, gas such as steam, lighter hydrocarbons of the present invention are meant carbon number well known to those skilled in the art less than 4 hydro carbons, molecular formula is C
nH
m, wherein n and m are the positive integer greater than 2, and the n maximum is no more than 4.
Comprise that methanol synthetic discharged gas delayed 201 of above-mentioned gas composition at first enters water scrubber and washes, remove the small amount of methanol in the off-gas, the off-gas that leaves water scrubber carries a spot of liquid foam and enters and be preheating to 40 ℃～80 ℃ after gas-liquid separator removes the mist of deentrainment, preferably be preheating to 40 ℃～60 ℃, enter first membrane separation device then, contact with membrane separation assemblies in being arranged on first membrane separation device, pressure for off-gas is preferably 5MPa～27MPa.Off-gas after the preheating contacts with the membrane separation assemblies of first membrane separation device and obtains first hydrogen-rich gas stream 202 and first object gas stream 203.
First object gas stream preferably is pressurized to 4.0MPa～6.0MPa, be admitted to carbon monoxide conversion device as unstripped gas after preferably being pressurized to 4.5MPa～5.5MPa, in the saturator of carbon monoxide conversion device, first object gas stream is given gas humidification with circulation desalted water counter current contacting, in preheater, preferably be preheating to 300 ℃～400 ℃ then, more preferably be preheating to 340 ℃～380 ℃ and enter the middle temperature transformation tower, in the middle temperature transformation tower, carbon monoxide in first object gas stream and water react and generate carbon dioxide and hydrogen.The conversion gas of discharging in the middle temperature transformation tower is lowered the temperature successively with after first object gas stream, twice heat exchange of circulation desalted water, preferably is cooled to 180 ℃～230 ℃, enters the low conversion tower that becomes then and carries out low temperature shift reaction, so that reaction of carbon monoxide is complete.Second object gas stream 204 of discharging from the low-temperature conversion tower one by one with circulation desalted water and recirculated cooling water heat exchange, be cooled to 40 ℃, enter gas-liquid separator then and remove moisture.
Second object gas stream 204 of discharging from the low-temperature conversion tower enters decarbonization device, enters from bottom, decarburization absorption tower, from bottom to top by decarburization adsorption tower and MEDA solution counter current contacting, absorbs the carbon dioxide of second object gas in flowing by MDEA solution.The gas of discharging from decarburization absorption tower cat head flows by after the decontaminating separator purification, removes residual MDEA solution by active carbon adsorber again, obtains the 3rd object gas stream 205.
The 3rd object gas stream of discharging from decarbonization device enters into second membrane separation device, preferably be pressurized to 3MPa～5MPa and send into the mist that the mechanical filter removal is carried secretly then, preferably be preheating to 40 ℃～70 ℃ then, more preferably being preheating to 45 ℃～60 ℃ enters in first section membrane separation assemblies, separating the non-infiltration gas stream that obtains by first section membrane separation assemblies enters into second section membrane separation assemblies and separates and obtain the 4th object gas stream 206, methane and lighter hydrocarbons purity in the 4th object gas stream reach more than 92%, can also can further be compressed directly as civilian or industrial natural gas as natural gas used for automobile; The infiltration air pressure that the infiltration gas that obtains from first section membrane separation assemblies and second section membrane separation assemblies obtain contracts and mixes the back and form second hydrogen-rich gas stream, 207, the second hydrogen-rich gas streams and can be used as the methyl methanol syngas raw material.
Below with specific embodiment technical scheme of the present invention is described.
Embodiment:
Have the methanol synthetic discharged gas delayed of two bursts of identical components: H
2Be 60.0%, CH
4+ C
nH
mBe 31.45%, CO is 6.5%, CO
2Be 1.5%, N
2Be 0.5%, O
2Be 0.05%.
The pressure of two strands of off-gas is respectively 7.0MPa and 4.4MPa, and total flow is 44400Nm
3/ h, described off-gas 201 is introduced into water scrubber and washes, remove the methyl alcohol in the unstripped gas, the off-gas that leaves water scrubber has a spot of mist, be admitted to gas-liquid separator then and remove the mist of deentrainment, the off-gas that leaves gas-liquid separator is fed in first membrane separation device contact with separating film module and obtains first hydrogen-rich gas stream 202 and first object gas flows 203.Wherein, the flow of first hydrogen-rich gas stream 202 is 21757.27Nm
3/ h, pressure are 2.2MPa, and component is: H
2Be 93.002%, CH
4+ C
nH
mBe 3.858%, CO
2Be 1.443%, CO is 1.583%, N
2Be 0.077%, O2 is 0.036%; The flow of first object gas stream 203 is 22642.62Nm
3/ h, pressure are 4.9MPa, and component is: H
2Be 29.824%, CH
4+ C
nH
mBe 56.931%, CO
2Be 1.419%, CO is 10.877%, N
2Be 0.888%, O2 is 0.061%.
First object gas that comes out from first membrane separation device flows to the converting means into CO, enter the hot water saturator after earlier the first object gas stream being pressurized to 5.0MPa, in the hot water saturator and circulation desalted water counter current contacting humidification, enter preheater then, enter the middle temperature transformation tower after being preheating to 360 ℃, carbon monoxide and water react and generate carbon dioxide and hydrogen in the middle temperature transformation tower, therefrom conversion tower discharge conversion gas flows with first object gas successively, after twice heat exchange of circulation desalted water, cool to 210 ℃, enter the low-temperature conversion tower then, in the low-temperature conversion tower, conversion gas is proceeded low-temperature conversion, the conversion gas and the circulation desalted water of discharging from the low-temperature conversion tower carry out heat exchange, cool to 160 ℃, entering gas-liquid separator separates again goes out moisture and then the MDEA solution of follow-up decarburization workshop section is boiled again, after further being reduced to 100 ℃, temperature cools off through water cooler, temperature drops to 40 ℃, enter again gas-liquid separator with moisture from coming out, the flow that obtains second object gas stream, 204, the second object gas stream 204 is 25077.20Nm
3/ h, pressure are 4.62MPa, and component is: H
2Be 36.520%, CH
4+ C
nH
mBe 51.406%, CO
2Be 10.982%, CO is 0.120%, N
2Be 0.802%, H
2O is 0.170%.
Second object gas stream, the 204 MDEA decarbonization devices that enter in the decarbonization device, second object gas stream is entered by bottom, decarburization absorption tower, from bottom to top by the decarburization absorption tower, MDEA solution through regeneration enters from top, decarburization absorption tower, from top to bottom by the decarburization absorption tower, second object gas stream of reverse flow fully contacts in the decarburization absorption tower with MDEA solution, carbon dioxide in second object gas stream is absorbed and enters in the MDEA solution, unabsorbed other component is drawn from top, decarburization absorption tower in second object gas stream, enter decontaminating separator, gas component after the separation enters active carbon filter, and to remove the flow that MDEA obtains the 3rd object gas stream 205, the three object gas stream 205 be 22318.56Nm
3/ h, pressure are 4.57MPa, and component is: H
2Be 40.993%, CH
4+ C
nH
mBe 57.702%, CO
2Be 0.100%, CO is 0.135%, N
2Be 0.900%, H
2O is 0.170%.
The MDEA solution that is absorbed with carbon dioxide is discharged from the bottom, absorption tower, through entering the poor rich liquid heat exchanger heating after the step-down, enter regenerator then and carry out hot reactivation, regeneration gas is through the cooling of regeneration gas cooler, enter regeneration separators, the carbon dioxide high-altitude emptying that draw at the separator top; The lean solution of regenerator bottom through the poor rich liquid heat exchanger cooling after, again through the cooling of lean solution cooler, be circulated to top, decarburization absorption tower by the lean pump supercharging then and continue carbon dioxide in absorption second object gas stream.
The 3rd object gas flows to into second membrane separation device, at first enter mechanical filter, remove the mist of carrying secretly in the 3rd object gas stream, enter heater then and be warming up to 50 ℃, the 3rd object gas after the heating flows to into one section membrane separation assemblies, obtaining purity in infiltration gas one side of one section membrane separation assemblies is 92.099%, pressure is one section hydrogen of 0.9MPa, and the non-infiltration gas of one section membrane separation assemblies enters the two-segment film separation assembly, obtaining purity in infiltration gas one side of two-segment film separation assembly is 83.637%, pressure is two sections hydrogen of 0.3MPa, obtain second hydrogen rich gas gas stream 207 after these two sections hydrogen and one section hydrogen compressed mixed, flow is 9467.420Nm
3/ h, pressure are 2.5MPa, H
2Content is 90.034%, CH
4+ C
nH
mBe 9.331%, CO
2Be 0.165%, CO is 0.045%, N
2Be 0.187%, H
2O is 0.237%.
The flow that obtains the 4th object gas stream 206, the four object gas from non-infiltration gas one side of two-segment film separation assembly is 12836.721Nm
3/ h, pressure are 2.5MPa, H
2Content is 4.869%, CH
4+ C
nH
mBe 93.442%, CO
2Be 0.052%, CO is 0.201%, N
2Be 1.427%, H2O 0.009% meets national two class natural gas standards.
More than methanol synthetic discharged gas delayed processing method provided by the utility model and device are described in detail.Used specific case herein principle of the present utility model and embodiment are set forth, the explanation of above embodiment just is used for helping to understand method of the present utility model and core concept thereof.Should be understood that; for those skilled in the art; under the prerequisite that does not break away from the utility model principle, can also carry out some improvement and modification to the utility model, these improvement and modification also fall in the protection domain of the utility model claim.
Claims (9)
1. the treating apparatus of an off-gas, described off-gas comprises methanol purge gas and/or gas and synthetic ammonia purge, it is characterized in that, described treating apparatus comprises successively:
First membrane separation device is provided with a membrane separation assemblies at least in described first membrane separation device, non-infiltration gas one side of described membrane separation assemblies is connected with carbon monoxide conversion device;
Described carbon monoxide conversion device comprises at least one conversion tower, and the discharge end of described conversion tower is connected with decarbonization device;
Described decarbonization device comprises at least one absorption tower, and the discharging opening on described absorption tower is connected with decontaminating separator;
The gaseous phase outlet of described purge gas separator is connected with the purified gas absorber;
Described treating apparatus also comprises second membrane separation device that is connected with the discharging opening of described decontaminating separator, in described second membrane separation device at least one membrane separation assemblies is set.
2. treating apparatus according to claim 1 is characterized in that, described carbon monoxide conversion device comprises middle temperature transformation tower and high temperature shift tower.
3. treating apparatus according to claim 2 is characterized in that, also is provided with the hot water saturator before described middle temperature transformation tower.
4. treating apparatus according to claim 1 is characterized in that described decarbonization device also comprises the decontaminating separator that is connected with described absorption tower.
5. treating apparatus according to claim 4 is characterized in that the port of export of described decontaminating separator further is provided with active carbon filter.
6. treating apparatus according to claim 4 is characterized in that described decarbonization device also comprises CO
2Regenerator.
7. treating apparatus according to claim 1 is characterized in that, described second membrane separation device comprises first section membrane separation assemblies and second section membrane separation assemblies.
8. treating apparatus according to claim 7 is characterized in that, also further is provided with mechanical filter before described first section membrane separation assemblies.
9. treating apparatus according to claim 7 is characterized in that, the non-infiltration gas outlet of first membrane separation assemblies of described second membrane separation device is connected with the raw material gas inlet of second membrane separation assemblies.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202198739U CN201701861U (en) | 2010-06-08 | 2010-06-08 | Purge gas treatment device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202198739U CN201701861U (en) | 2010-06-08 | 2010-06-08 | Purge gas treatment device |
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| CN201701861U true CN201701861U (en) | 2011-01-12 |
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ID=43439006
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101850209A (en) * | 2010-06-08 | 2010-10-06 | 中煤能源黑龙江煤化工有限公司 | Vent gas treatment method and treatment device |
| CN105129731A (en) * | 2015-08-20 | 2015-12-09 | 神华集团有限责任公司 | Recycling device for hydrogen in methanol purge gas |
| CN108439332A (en) * | 2018-04-19 | 2018-08-24 | 贵州赤天化桐梓化工有限公司 | A kind of process of methanol-fueled CLC hydrogen retrieval UF membrane impermeable gas recycling |
-
2010
- 2010-06-08 CN CN2010202198739U patent/CN201701861U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101850209A (en) * | 2010-06-08 | 2010-10-06 | 中煤能源黑龙江煤化工有限公司 | Vent gas treatment method and treatment device |
| CN101850209B (en) * | 2010-06-08 | 2012-08-22 | 中煤能源黑龙江煤化工有限公司 | Vent gas treatment method and treatment device |
| CN105129731A (en) * | 2015-08-20 | 2015-12-09 | 神华集团有限责任公司 | Recycling device for hydrogen in methanol purge gas |
| CN108439332A (en) * | 2018-04-19 | 2018-08-24 | 贵州赤天化桐梓化工有限公司 | A kind of process of methanol-fueled CLC hydrogen retrieval UF membrane impermeable gas recycling |
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