CN1300635A - Process for removing CO2 and H2S from biological gas - Google Patents
Process for removing CO2 and H2S from biological gas Download PDFInfo
- Publication number
- CN1300635A CN1300635A CN00134330A CN00134330A CN1300635A CN 1300635 A CN1300635 A CN 1300635A CN 00134330 A CN00134330 A CN 00134330A CN 00134330 A CN00134330 A CN 00134330A CN 1300635 A CN1300635 A CN 1300635A
- Authority
- CN
- China
- Prior art keywords
- absorption tower
- desorber
- biogas
- absorption
- rich solution
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000010521 absorption reaction Methods 0.000 claims abstract description 61
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 238000003795 desorption Methods 0.000 claims abstract description 4
- 238000007599 discharging Methods 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 239000000243 solution Substances 0.000 claims description 45
- 230000002745 absorbent Effects 0.000 claims description 14
- 239000002250 absorbent Substances 0.000 claims description 14
- 230000008929 regeneration Effects 0.000 claims description 14
- 238000011069 regeneration method Methods 0.000 claims description 14
- 239000012535 impurity Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 claims description 6
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 6
- 229920000768 polyamine Polymers 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 241000282326 Felis catus Species 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 239000012264 purified product Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000007797 corrosion Effects 0.000 abstract description 2
- 238000005260 corrosion Methods 0.000 abstract description 2
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 7
- 238000011084 recovery Methods 0.000 description 5
- 235000019628 coolness Nutrition 0.000 description 4
- 230000008595 infiltration Effects 0.000 description 3
- 238000001764 infiltration Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XNWFRZJHXBZDAG-UHFFFAOYSA-N 2-METHOXYETHANOL Chemical compound COCCO XNWFRZJHXBZDAG-UHFFFAOYSA-N 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
A purified process for removing CD2 and H2S from biologic gas includes such steps as countercurrent contacting between the biologic gas and regenerated poor liquid in absorption tower, absorbing CO2 and H2S by poor liquid to purity said biologic gas and making poor liquid become rich liquid, delivering said rich liquid to desorption tower, heating it by boiler to release CO2 and H2S, exhausting them from tower top, discharging the regenerated poor liquid from tower bottom, and returning the absorption tower for cyclic use of the poor liquid. Its advantages are high absorption performance and purifying effect, less corrosion, low cost and less energy consumption.
Description
The present invention relates to CO in the biogas that anaerobic processes such as garbage loading embeading biogas (LFG) and sewage, mud, ight soil, straw produce
2, H
2The process for purifying of S.
At present, for CO in the biogas such as landfill biogas
2, H
2The purification of S abroad has and adopts embrane method to separate.Membrane separation process is under certain pressure condition, utilizes variety classes gas to have different infiltration rates to realize the purpose of its separation in the organic polymer film.For biogas, N wherein
2, CH
4Be difficult for infiltration, and CO
2, H
2Easily infiltration, thus realize CH
4With CO
2Separation.The advantage of this technology is: take up an area of and lack, shutting down is easy; Be not subjected to contain in the unstripped gas O
2The influence of amount, and remove CO
2In time, also dewater.But also there is following shortcoming in this technology: a) strict to the preliminary treatment of biogas, otherwise film is easy to be polluted and lost efficacy; B) service life of film limited, the renewal cost costliness of film makes production cost improve; C) film separates needs to carry out under elevated pressures, and needs the multistage pressurization, makes capital construction and operating cost improve; D) film separates CH
4The rate of recovery lower, only 70%.There is employing MEA (MEA) solution to be used for the CO that takes off of biogas as absorbent both at home and abroad
2Process for purifying is though this technology can be removed CO in the biogas effectively
2, H
2S, but this technology has following weak point: the one, the MEA solvent-oil ratio is big, purifies the cost height; The 2nd, absorption liquid has certain corrosivity, so process equipment need be used resistant material, technology investment is increased considerably.Still there is not to adopt the polyamines absorption liquid that contains absorbent MDEA (N methyl glycol amine) to be used for biogas CO both at home and abroad
2, H
2The absorption cleaning technology of S.
In view of the problems referred to above that exist, the purpose of this invention is to provide polyamines solution that a kind of employing contains absorbent MDEA and be CO in the biogas of absorption liquid
2, H
2The physical-chemical process for purifying of S makes effective ingredient CH in the biogas
4Can access more efficiently utilization, it is low to reach its investment and operating cost, CH
4The high purpose of the rate of recovery.
For realizing purpose of the present invention, take following technical measures:
CO in the biogas
2, H
2The process for purifying of S comprises absorption tower 1, desorber 8, reboiler 10, heat exchanger 5, cooler 2,3,6, separator 4,7, rich solution medial launder 13, absorbent storage tank 9, pump 11,12 etc.
1 bottom enters the absorption tower to biogas from the absorption tower, enters the absorption tower by the regeneration lean solution of desorber 8 from top, absorption tower, biogas and regeneration lean solution counter current contacting, CO in the biogas in the absorption tower
2, H
2Impurity such as S are absorbed by liquid absorption; Purified gas comes out from the top, absorption tower, and through cooler 3 coolings, separator 4 separates, and separating back gas becomes purified product gas, and condensate stream is to rich solution medial launder 13; Absorb CO
2, H
2Rich solution behind the impurity such as S comes out from the bottom, absorption tower, enters rich solution medial launder 13, comes out to enter heat exchanger 5 through pump 12 pressurizations from the rich solution medial launder, comes the lean solution heat exchange with desorber in heat exchanger, enters desorber 8 tops after heat exchanger comes out, and sprays into desorber; At the bottom of the tower of desorber, adopt reboiler 10 heating, make the CO in the rich solution
2Deng the impurity desorb, (contain CO from the cat head discharge
2, H
2S tail gas), contain CO
2Tail gas separate the back discharging or recycle through cooler 6 cooling, separator 7, the condensate stream of separation arrives rich solution medial launder 13; Regeneration lean solution after the desorb is come out from desorber 8 bottoms, and through pump 11 pressurizations, the rich solution heat exchange that enters heat exchanger 5 and absorption tower enters condenser 2 coolings again, enters the absorption tower from top, absorption tower again and recycles; Absorbent MDEA by absorbent storage tank 9 sends into pump 11.
Above-mentioned CO
2, H
2The absorption of S can be carried out in normal pressure or compression system.
Above-mentioned regeneration lean solution concentration is the polyamines aqueous solution that contains MDEA30%～50%.
Absorb 55 ℃～90 ℃ of temperature in the above-mentioned absorption tower, gas liquid ratio 40～60 under the normal pressure: 1, and pressurization gas liquid ratio down can reach 100～160: 1.
Desorption temperature is 90 ℃～110 ℃ in the above-mentioned desorber.
The polyamines solution that this process using contains absorbent MDEA is made absorption liquid, is a kind of chemical absorbent with Physical Absorption performance, can effectively remove CO in the biogas
2, H
2Impurity such as S reach the purpose of effective purification.The major advantage of this method is: a) have Physical Absorption and chemical absorbing characteristic concurrently, CO
2Solubility is big therein; B) have a narrow range of temperature between absorption and the regeneration, absorption reaction heat is less, and side reaction is few, and the regeneration hear rate is little; C) stability of solution is good, is difficult for degraded, so solvent-oil ratio is few; D) solution corrosion is little, and equipment can be selected carbon steel for use; E) absorption liquid concentration is higher, so the solution internal circulating load is little, and energy consumption is low; F) absorption liquid steam forces down, and the solvent evaporates loss is few; G) degree of purification height, CO in the purified gas
2Content≤2% (normal pressure absorption) add depress can＜0.2%, so this method has small investment, operating cost is low, the characteristics of less energy consumption.
Introduce technology contents of the present invention in detail below in conjunction with drawings and Examples.
Fig. 1 is CO in the biogas
2, H
2S process for purifying flow chart.
Among the figure, CO in the biogas
2, H
2The process for purifying of S comprises absorption tower 1, desorber 8, reboiler 10, heat exchanger 5, cooler 2,3,6, separator 4,7, rich solution medial launder 13, absorbent storage tank 9, pump 11,12 etc.
1 bottom enters the absorption tower to the biogas that transports through air blast from refuse landfill from the absorption tower, column bottom temperature～90 ℃, regeneration lean solution by desorber 8 enters the absorption tower from top, absorption tower, 55 ℃～60 ℃ of tower top temperatures, regeneration lean solution concentration is the polyamines aqueous solution that contains MDEA30%～50%, biogas and regeneration lean solution counter current contacting, CO in the biogas in the absorption tower
2, H
2Impurity such as S are absorbed by liquid absorption, and absorb 55 ℃～90 ℃ of temperature, gas liquid ratio 40～60: 1; Purified gas comes out from the top, absorption tower, and through cooler 3 coolings, separator 4 separates, and separating back gas becomes purified product gas, purified gas CH
4Content＞80%, CO
2Content＜2%, H
2S＜20mg/m
3, CH
4The rate of recovery＞95% purifies artifact gas and can be applicable to do motor vehicle fuel (pressurization) or make high quality gas fuel.Condensate stream is to rich solution medial launder 13; Absorb CO
2, H
2Rich solution behind the impurity such as S comes out from the bottom, absorption tower, enters rich solution medial launder 13, comes out to enter heat exchanger 5 through pump 12 pressurizations from the rich solution medial launder, comes the lean solution heat exchange with desorber in heat exchanger, enters desorber 8 tops after heat exchanger comes out, and sprays into desorber; Tower top temperature～90 ℃, column bottom temperature～110 ℃, 90 ℃～110 ℃ of desorption temperatures adopt reboiler 10 heating at the bottom of the tower of desorber, make the CO in the rich solution
2Deng the impurity desorb, (contain CO from the cat head discharge
2, H
2S tail gas), contain CO
2Tail gas separate the back discharging or recycle through cooler 6 cooling, separator 7, the condensate stream of separation arrives rich solution medial launder 13; Regeneration lean solution after the desorb is come out from desorber 8 bottoms, and through pump 11 pressurizations, the rich solution heat exchange that enters heat exchanger 5 and absorption tower enters condenser 2 coolings again, enters the absorption tower from top, absorption tower again and recycles; Absorbent MDEA by absorbent storage tank 9 sends into pump 11.
Embodiment one
Handle unstripped gas (LFG) amount 10,000 m
3/ d, unstripped gas form (%) and are: CH
450%～55%; CO
235%～45%; O
21～2.Absorption liquid concentration 30%～50%; Gas (unstripped gas) liquor ratio 50: 1.Purified gas CH
4Content＞80%, CO
2Content＜2%, H
2S＜20mg/m
3, CH
4The rate of recovery＞95%.
The absorption tower: tower top temperature～60 ℃, column bottom temperature～90 ℃, normal pressure absorbs (P=0.12Mpa absolute pressure) down;
Desorber: tower top temperature～90 ℃, column bottom temperature～110 ℃.
Embodiment two
Handle unstripped gas (LFG) amount 15000m
3/ d, unstripped gas form (%) and are: CH
450%～55%; CO
235%～45%; O
21～2.Absorption liquid concentration 30%～50%; Gas (unstripped gas) liquor ratio 150: 1.Purified gas CH
4Content＞80%, CO
2Content＜1%, H
2S＜20mg/m
3, CH
4The rate of recovery＞95%.
The absorption tower: tower top temperature～60 ℃, column bottom temperature～90 ℃ add and depress absorption (P=1.5Mpa absolute pressure);
Desorber: tower top temperature～90 ℃, column bottom temperature～110 ℃.
Claims (5)
1. CO in the biogas
2, H
2The process for purifying of S, it is characterized in that: comprise absorption tower (1), desorber (8), reboiler (10), heat exchanger (5), cooler (2), (3), (6), separator (4), (7), rich solution medial launder (13), absorbent storage tank (9), pump (11), (12) etc., (1) bottom enters the absorption tower to biogas from the absorption tower, the regeneration lean solution of being come by desorber (8) enters the absorption tower from top, absorption tower, biogas and regeneration lean solution counter current contacting, CO in the biogas in the absorption tower
2, H
2Impurity such as S are absorbed by liquid absorption; Purified gas comes out from the top, absorption tower, and through cooler (3) cooling, separator (4) separates, and separating back gas becomes purified product gas, and condensate stream is to rich solution medial launder (13); Absorb CO
2, H
2Rich solution behind the impurity such as S comes out from the bottom, absorption tower, enter rich solution medial launder (13), come out to enter heat exchanger (5), in heat exchanger, come the lean solution heat exchange with desorber through pump (12) pressurization from the rich solution medial launder, after heat exchanger comes out, enter desorber (8) top, spray into desorber; At the bottom of the tower of desorber, adopt reboiler (10) heating, make the impurity desorbs such as CO2 in the rich solution, discharge, contain CO from cat head
2Tail gas separate the back discharging or recycle through cooler (6) cooling, separator (7), the condensate stream of separation arrives rich solution medial launder (13); Regeneration lean solution after the desorb is come out from desorber (8) bottom, and through pump (11) pressurization, the rich solution heat exchange that enters heat exchanger (5) and absorption tower enters condenser (2) cooling again, and (1) top enters the absorption tower and recycles from the absorption tower again; The absorbent MDEA that is come by absorbent storage tank (9) sends into pump (11).
2. CO in the biogas according to claim 1
2, H
2The process for purifying of S is characterized in that: the interior CO in absorption tower (1)
2, H
2The absorption of S can be carried out in normal pressure or compression system.
3. CO in the biogas according to claim 1
2, H
2The process for purifying of S is characterized in that: regeneration lean solution concentration is the polyamines aqueous solution that contains MDEA30%～50%.
4. CO in the biogas according to claim 1
2, H
2The process for purifying of S is characterized in that: absorb 55 ℃～90 ℃ of temperature in absorption tower (1), gas liquid ratio 40～60 under the normal pressure: 1, and pressurization gas liquid ratio down can reach 100～160: 1.
5. CO in the biogas according to claim 1
2, H
2The process for purifying of S is characterized in that: 90 ℃～110 ℃ of the interior desorption temperatures of desorber (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001343300A CN1137753C (en) | 2000-12-19 | 2000-12-19 | Process for removing CO2 and H2S from biological gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001343300A CN1137753C (en) | 2000-12-19 | 2000-12-19 | Process for removing CO2 and H2S from biological gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1300635A true CN1300635A (en) | 2001-06-27 |
| CN1137753C CN1137753C (en) | 2004-02-11 |
Family
ID=4596163
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB001343300A Expired - Lifetime CN1137753C (en) | 2000-12-19 | 2000-12-19 | Process for removing CO2 and H2S from biological gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1137753C (en) |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101856579A (en) * | 2010-06-02 | 2010-10-13 | 清华大学 | Novel energy-saving CO2 trapping process of improved potassium carbonate |
| CN101108988B (en) * | 2007-08-10 | 2011-03-23 | 辽宁凯田再生能源环保有限公司 | Biogas cleaning equipment and purifying technique thereof |
| CN102059037A (en) * | 2010-11-22 | 2011-05-18 | 重庆欣雨压力容器制造有限责任公司 | Process for purifying carbon dioxide from tail gas of natural gas |
| CN101612512B (en) * | 2008-06-25 | 2011-05-25 | 苏庆泉 | Carbon dioxide separating system and separating method |
| CN102242059A (en) * | 2011-04-25 | 2011-11-16 | 青岛天人环境股份有限公司 | Device and method for preparing automobile fuel gas by utilizing organic wastes |
| CN101659889B (en) * | 2008-08-25 | 2012-09-26 | 来铁路 | Methane purifying comprehensive utilization technology |
| CN102802766A (en) * | 2009-06-19 | 2012-11-28 | 国际壳牌研究有限公司 | Process For The Removal Of Carbon Dioxide And/or Hydrogen Sulphide From A Gas |
| CN102933284A (en) * | 2010-04-20 | 2013-02-13 | 巴布考克日立株式会社 | Exhaust gas treatment system provided with carbon dioxide chemisorption equipment |
| CN103113945A (en) * | 2013-02-01 | 2013-05-22 | 王仕华 | Marsh gas purification system and marsh gas purification method |
| CN106318500A (en) * | 2015-07-06 | 2017-01-11 | 中国石油化工股份有限公司 | Biological purifying process of unconventional gas |
| CN106669365A (en) * | 2016-12-15 | 2017-05-17 | 西安交通大学 | Thermal-electric co-driven CO2 capturing system adopting amine method |
| CN108348841A (en) * | 2015-08-28 | 2018-07-31 | 能源科技创新有限责任公司 | Method and apparatus for handling biogas |
| CN111013333A (en) * | 2019-12-24 | 2020-04-17 | 中国纺织科学研究院有限公司 | Method for treating hydrogen sulfide in waste gas generated in viscose fiber production |
| CN111372671A (en) * | 2017-11-30 | 2020-07-03 | 株式会社神户制钢所 | Gas processing method and gas processing apparatus |
| CN114011212A (en) * | 2021-10-30 | 2022-02-08 | 雅邦绿色过程与新材料研究院南京有限公司 | Energy-saving process for recovering high-concentration CO2 by coupling membrane/MDEA solution |
-
2000
- 2000-12-19 CN CNB001343300A patent/CN1137753C/en not_active Expired - Lifetime
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101108988B (en) * | 2007-08-10 | 2011-03-23 | 辽宁凯田再生能源环保有限公司 | Biogas cleaning equipment and purifying technique thereof |
| CN101612512B (en) * | 2008-06-25 | 2011-05-25 | 苏庆泉 | Carbon dioxide separating system and separating method |
| CN101659889B (en) * | 2008-08-25 | 2012-09-26 | 来铁路 | Methane purifying comprehensive utilization technology |
| CN102802766A (en) * | 2009-06-19 | 2012-11-28 | 国际壳牌研究有限公司 | Process For The Removal Of Carbon Dioxide And/or Hydrogen Sulphide From A Gas |
| CN102933284A (en) * | 2010-04-20 | 2013-02-13 | 巴布考克日立株式会社 | Exhaust gas treatment system provided with carbon dioxide chemisorption equipment |
| CN101856579A (en) * | 2010-06-02 | 2010-10-13 | 清华大学 | Novel energy-saving CO2 trapping process of improved potassium carbonate |
| CN102059037A (en) * | 2010-11-22 | 2011-05-18 | 重庆欣雨压力容器制造有限责任公司 | Process for purifying carbon dioxide from tail gas of natural gas |
| CN102242059A (en) * | 2011-04-25 | 2011-11-16 | 青岛天人环境股份有限公司 | Device and method for preparing automobile fuel gas by utilizing organic wastes |
| CN103113945A (en) * | 2013-02-01 | 2013-05-22 | 王仕华 | Marsh gas purification system and marsh gas purification method |
| CN103113945B (en) * | 2013-02-01 | 2015-04-08 | 王仕华 | Marsh gas purification system and marsh gas purification method |
| CN106318500A (en) * | 2015-07-06 | 2017-01-11 | 中国石油化工股份有限公司 | Biological purifying process of unconventional gas |
| CN108348841A (en) * | 2015-08-28 | 2018-07-31 | 能源科技创新有限责任公司 | Method and apparatus for handling biogas |
| CN108348841B (en) * | 2015-08-28 | 2022-01-04 | 能源科技创新有限责任公司 | Method and device for treating biogas |
| CN106669365A (en) * | 2016-12-15 | 2017-05-17 | 西安交通大学 | Thermal-electric co-driven CO2 capturing system adopting amine method |
| CN111372671A (en) * | 2017-11-30 | 2020-07-03 | 株式会社神户制钢所 | Gas processing method and gas processing apparatus |
| US11331625B2 (en) | 2017-11-30 | 2022-05-17 | Kobe Steel, Ltd. | Gas treatment method and gas treatment apparatus |
| CN111013333A (en) * | 2019-12-24 | 2020-04-17 | 中国纺织科学研究院有限公司 | Method for treating hydrogen sulfide in waste gas generated in viscose fiber production |
| CN111013333B (en) * | 2019-12-24 | 2022-07-29 | 中国纺织科学研究院有限公司 | Method for treating hydrogen sulfide in waste gas generated in viscose fiber production |
| CN114011212A (en) * | 2021-10-30 | 2022-02-08 | 雅邦绿色过程与新材料研究院南京有限公司 | Energy-saving process for recovering high-concentration CO2 by coupling membrane/MDEA solution |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1137753C (en) | 2004-02-11 |
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