CN106390686B - A kind of purification method of unstripped gas - Google Patents
A kind of purification method of unstripped gas Download PDFInfo
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- CN106390686B CN106390686B CN201611062867.5A CN201611062867A CN106390686B CN 106390686 B CN106390686 B CN 106390686B CN 201611062867 A CN201611062867 A CN 201611062867A CN 106390686 B CN106390686 B CN 106390686B
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- unstripped gas
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- gas
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- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000000746 purification Methods 0.000 title claims abstract description 10
- 239000002904 solvent Substances 0.000 claims abstract description 70
- 238000010521 absorption reaction Methods 0.000 claims abstract description 44
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000010828 elution Methods 0.000 claims abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical group OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 91
- 238000006243 chemical reaction Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000003599 detergent Substances 0.000 claims description 3
- 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 2
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 2
- 229920006395 saturated elastomer Polymers 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims 1
- 239000012535 impurity Substances 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 63
- 239000002994 raw material Substances 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000005261 decarburization Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000009469 supplementation Effects 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
- B01D2252/2021—Methanol
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention relates to a kind of purification methods of unstripped gas, it is characterised in that includes the following steps: that the first unstripped gas enters in the first absorption tower from bottom；First lean solvent, the first half lean solvents and the second half lean solvents enter the first absorption tower from top, the CO in the first unstripped gas2And H2The impurity compositions such as S are washed out；Tower top on first absorption tower obtains the first purified gas；The first richness CO is extracted out from the middle and lower part on first absorption tower2Solvent is divided into two strands, and first strand enters in the stripping tower from top；Second strand is sent out-of-bounds；Second unstripped gas enters second absorption tower from bottom, and the second lean solvent enters second absorption tower from top, elutes the sour gas in the second unstripped gas；Second gang of richness CO is extracted out from the middle and lower part of second absorption tower2Solvent；Purified gas discharge after elution, enters from the bottom of stripping tower, to first burst of richness CO2Solvent carries out air lift；Purified gas discharge after air lift obtains the first half lean solvents in the bottom of stripping tower.
Description
Technical field
The present invention relates to a kind of method for gas purification applied to coal chemical technology, refer specifically to a kind of to purify two kinds simultaneously
The method of unstripped gas.
Background technique
Low-temp methanol, which is washed, is, be widely used in using coal (petroleum coke) or residual oil as raw material produce synthesis ammonia, town gas,
In the device of industrial hydrogen, synthesizing methanol or other C-1 chemistry product, the sour gas in product is removed.Its process is to use low-temp methanol
The sour gas in gaseous mixture is absorbed, usually CO2And H2S, then make methanol and sour gas point through decompression desorption, air lift, heating regeneration
It opens, achievees the purpose that separation and recovery.Methanol reduces the absorbability of sour gas as the temperature rises.To improve methanol pair
The absorbability of sour gas reduces solvent internal circulating load, it is necessary to the absorption process of washing device for methanol be maintained to operate at low temperature.Methanol
The low-temperature heat source of cleaning device, first is that cooling capacity is supplemented to system by ice maker, second is that by CO in solution2Refrigeration by adsorption maintains.
With the raising required low temperature washing device for methanol, it is often necessary to while the desulfurization and decarburization of conversion gas is handled, especially
Desulfurization and decarburization while being plurality of raw materials gas, there is presently no relevant technologies.
Summary of the invention
The technical problem to be solved by the present invention is to for the prior art status provide it is a kind of can simultaneously desulfurization and decarburization and
The raw material gas purifying method of two kinds of unstripped gas can be purified simultaneously.
The technical scheme of the invention to solve the technical problem is: the purification method of the unstripped gas, feature exist
In including the following steps:
First unstripped gas enters in the first absorption tower from bottom；First lean solvent, the first half lean solvents from stripping tower
Enter first absorption tower from top with from the second half lean solvents out-of-bounds, and first lean solvent, the first half poor
The feeding position of solvent and the second half lean solvents is successively arranged from top to bottom；
First unstripped gas flows from bottom to top in first absorption tower, with detergent counter current contacting, the first unstripped gas
In CO2And H2The impurity compositions such as S are washed out；Tower top on first absorption tower obtains the first purified gas；It is inhaled from described first
Extract the first richness CO out in the middle and lower part for receiving tower2Solvent；
The first richness CO2Solvent is divided into two strands, wherein first gang of richness CO2Solvent enters in the stripping tower from top；The
Two gangs of richness CO2Solvent is sent out-of-bounds；
Second unstripped gas enters second absorption tower from bottom, and the second lean solvent enters the second absorption tower from top, and two
Person's counter current contacting in second absorption tower elutes the sour gas in the second unstripped gas；From the middle and lower part of second absorption tower extraction the
Two gangs of richness CO2Solvent；Purified gas after elution is discharged from the top of second absorption tower, enters from the bottom of the stripping tower, right
First burst of richness CO2Solvent carries out air lift；
The second purified gas after air lift is discharged from the top of the stripping tower, obtains described the in the bottom of the stripping tower
Half lean solvent.
It is preferred that containing H in first unstripped gas and second unstripped gas2: 75%~15%, CO:75%~0.1%,
CO2: 50%~2%, H2S:1%~0.0001%；Water content for saturated water content at temperature and pressure；Described first
The temperature of unstripped gas and second unstripped gas is 50~-35 DEG C, and pressure is 2~8.5MPaG.
The ratio of first lean solvent and first unstripped gas is 0.1~10kg:1Nm3。
The ratio of the first half lean solvent and the second half lean solvents and first unstripped gas is respectively 0.1~10kg:
1Nm3With 0.01~10kg:1Nm3。
First burst of richness CO2The ratio of solvent and second unstripped gas is 0.01~10kg:1Nm3。
The ratio of the second rich co2 solvent and second unstripped gas is 0.1~10kg:1Nm3。
The ratio of second lean solvent and second unstripped gas is 0.1~10kg:1Nm3.；
The reaction condition of the stripping tower be 0.2~8.5MPaG, 10~-70 DEG C.
The inner cavity on first absorption tower is divided into upper, middle and lower segment by the first catch box and the second catch box, and described
The feeding position of one lean solvent, the first half lean solvents and the second half lean solvents is located at upper section；The first richness CO2The extraction of solvent
Position is located at the bottom in middle section；
The inner cavity of the second absorption tower is divided into upper, middle and lower segment by third catch box and the 4th catch box, and described
Two richness CO2Withdrawn position be located at the bottom in middle section.
The solvent can be methanol, MDEA solvent or NHD solvent；It is preferred that methanol.
Compared with prior art, raw material gas purifying method provided by the present invention can purify two kinds of raw materials, and second simultaneously
The air lift gas source that can be used as the lyosoption of the first unstripped gas after raw material gas purifying, to rich CO2Solvent is regenerated, half obtained
Lean solvent can be used as the cleaning solvent (or cleaning solvent of the second unstripped gas) of the first unstripped gas, while increase in the second purified gas
CO2Content, energy conservation and consumption reduction effects are significant, and can greatly reduce the operational load of rich solvent subsequent parsing and regenerative system,
The dosage for reducing lean solvent and half lean solvent, to further decrease the energy consumption of solvent regeneration system.
Disclosure is particularly well suited to generate fuel gas as conversion gas purification generation hydrogen and the purification of non-shifting gas to be used in combination.
Detailed description of the invention
Fig. 1 is flow diagram of the embodiment of the present invention.
Specific embodiment
The present invention will be described in further detail below with reference to the embodiments of the drawings.
As shown in Figure 1, the inner cavity on the first absorption tower 1 used in the method for the unstripped gas passes through 11 He of the first catch box
Second catch box 12 divides for upper, middle and lower segment, the feeding position of the first poor methanol, the first half poor methanols and the second half poor methanols
Positioned at upper section；First richness CO2The withdrawn position of methanol is located at the bottom in middle section；The inner cavity of second absorption tower passes through third catch box
21 and the 4th catch box 22 divide for upper, middle and lower segment, the second richness CO2Withdrawn position be located at the bottom in middle section.
By the mating more gasification furnaces work of the present embodiment, i.e. the upstream of the present apparatus is provided with more gasification furnace outputs and slightly synthesizes
Gas, a portion pass through CO converting means, by most CO by with H2Conversion reaction occurs for O, generates CO2And H2, obtain
The first unstripped gas of conversion gas；Another part crude synthesis gas does not pass through CO converting means, and merely through in recycling crude synthesis gas
After heat and gas-water separation, into present apparatus unit, this is the second unstripped gas in the present embodiment.
First unstripped gas, consisting of H2: 55.87%, N2: 0.22%, CO:0.34%, AR:0.08%, CH4:
0.07%, CO2: 42.96%, H2S:0.25%, NH3: 0.02%, H2O:0.18%；First obtained after first raw material gas purifying
Purified gas group becomes H2: 98.9%, N2: 0.39%, CO:0.6%, AR:0.14%, CH4: 0.12%, about 24.3 ten thousand Nm of flow3/
h；
Second unstripped gas, consisting of: H2: 47.14%, N2: 0.26%, CO:20.16%, AR:0.10%, CH4:
0.08%, CO2: 31.77%, H2S:0.28%, NH3: 0.01%, H2O:0.17%；Second obtained after second raw material gas purifying
Purified gas group becomes H2: 60.66%, N2: 0.33%, CO:25.94%, AR:0.13%, CH4: 0.10%, CO2: 13%.Flow
About 36.1 ten thousand Nm3/ h can be used as fuel gas and use for IGCC power generation.
Specific steps are as follows:
The first unstripped gas 437825Nm that temperature is -20 DEG C, pressure is 5.63MPaG3/ h enters first from bottom and absorbs
In tower 1；The first half poor methanols from stripping tower 3 and temperature that the first poor methanol that temperature is -50 DEG C, temperature are -36 DEG C are -
58 DEG C from the second half poor methanols out-of-bounds enter the first absorption tower 1 from upper section, the first poor methanol, the first half poor methanols and the
The feeding position of 2 half poor methanols is successively arranged from top to bottom；
First unstripped gas flows from bottom to top in the first absorption tower 1, and detergent counter current contacting, in the first unstripped gas
CO2And H2The impurity compositions such as S are washed out；Tower top on the first absorption tower 1 obtains the first purified gas；Under in the first absorption tower 1
Extract the first richness CO out in portion2Methanol；
First richness CO2Methanol is divided into two strands, wherein first gang of richness CO2Methanol enters in the stripping tower 3 from top；Second
Stock richness CO2Methanol is sent out-of-bounds；First gang of richness CO2Methanol and second gang of richness CO2The molar flow ratio of methanol is 0.3.
The second unstripped gas 467184Nm that temperature is -22 DEG C, pressure is 5.85MPaG3/ h enters second absorption tower from bottom
2, the second poor methanol enters second absorption tower 2 from top, and the two counter current contacting in second absorption tower 2 elutes the second unstripped gas
In sour gas；The second richness CO is extracted out from the middle and lower part of second absorption tower 22Methanol；Purified gas after elution is from second absorption tower 2
Top discharge, into the bottom of stripping tower 3, to first gang of richness CO from the first absorption tower2Methanol carries out air lift；
The second purified gas after air lift, CO therein2Content by before air inlet stripper≤5%, increase to >=13%, from gas
The top of stripper 3 is discharged, and obtains the first half poor methanols in the bottom of stripping tower 3.
In the present embodiment, the ratio of the first poor methanol and the first unstripped gas is 1.39kg/1Nm3。
The ratio of the first half poor methanols and the second half poor methanols and the first unstripped gas is respectively 1.6kg/1Nm3And 0.02kg/
1Nm3。
First gang of richness CO2The ratio of methanol and the second unstripped gas is 0.03kg/Nm3；First gang of richness CO2Methanol and second strand
Rich CO2The molar flow ratio of methanol is 0.3；
The ratio of second unstripped gas and the second poor methanol is 0.68kg/1Nm3；
The reaction condition of stripping tower 3 be 2.2MPaG, -25 DEG C.
In old process, under the treatment scale of this implementation, for requiring supplementation with a large amount of N in the fuel gas of IGCC Plant2Or
CO2, to fill into CO2For gas, the CO that about requires supplementation with2Tolerance is 36139Nm3/ h, due to needing pressure match, to CO2Pressurization
To 2.2MPaG, needing increased compression power consumption is 4763kW.The quantity of circulating water needed is 433t/h.Device needs that CO is arranged simultaneously2
Compressor also increases the investment cost of device.
And the second purified gas in the present embodiment can be used directly as fuel gas, be not required to supplement CO2；And annual operating cost
5% can be reduced, plant energy consumption reduces by 6%；Energy conservation and consumption reduction effects are significant.
Claims (3)
1. a kind of purification method of unstripped gas, it is characterised in that include the following steps:
First unstripped gas enters in the first absorption tower (1) from bottom；It is first lean solvent, the first half from stripping tower (3) poor molten
Agent and enter first absorption tower (1), and first lean solvent, first from top from the second half lean solvents out-of-bounds
The feeding position of half lean solvent and the second half lean solvents is successively arranged from top to bottom；
First unstripped gas is flowed from bottom to top in first absorption tower (1), and detergent counter current contacting, in the first unstripped gas
CO2And H2S is washed out；The first purified gas is obtained in the tower top of first absorption tower (1)；From first absorption tower (1)
Extract the first richness CO out in middle and lower part2Solvent；
The first richness CO2Solvent is divided into two strands, wherein first gang of richness CO2Solvent enters in the stripping tower (3) from top；The
Two gangs of richness CO2Solvent is sent out-of-bounds；
Second unstripped gas enters second absorption tower (2) from bottom, and the second lean solvent enters the second absorption tower (2) from top,
The two elutes the sour gas in the second unstripped gas in second absorption tower (2) interior counter current contacting；Under in second absorption tower (2)
Extract the second richness CO out in portion2Solvent；Purified gas after elution is discharged from the top of second absorption tower (2), into the stripping tower (3)
Bottom, to come from first absorption tower (1) first gang of richness CO2Solvent carries out air lift；
The second purified gas after air lift is discharged from the top of the stripping tower (3), obtains in the bottom of the stripping tower (3) described
The first half lean solvents;
Contain H in first unstripped gas and second unstripped gas2: 75% ~ 15%, CO:75% ~ 0.1%, CO2: 50% ~ 2%, H2S:1%
~0.0001%；Water content for saturated water content at temperature and pressure；First unstripped gas and second unstripped gas
Temperature be 50 ~ -35 DEG C, pressure be 2 ~ 8.5MPaG；
The ratio of first lean solvent and first unstripped gas is 0.1 ~ 10kg:1Nm3；
The ratio of the first half lean solvent and the second half lean solvents and first unstripped gas is 0.1 ~ 10kg:1Nm3With
0.01 ~ 10kg:1Nm3；
First burst of richness CO2The ratio of solvent and second unstripped gas is 0.01 ~ 10kg:1Nm3；
The ratio of second lean solvent and second unstripped gas is 0.1 ~ 10kg:1Nm3；
The second richness CO2The ratio of solvent and second unstripped gas is 0.1 ~ 10kg:1Nm3；
The reaction condition of the stripping tower (3) be 0.2 ~ 8.5MPaG, 10 ~ -70 DEG C.
2. the purification method of unstripped gas according to claim 1, it is characterised in that the inner cavity of first absorption tower (1) is logical
It crosses the first catch box (11) and the second catch box (12) is divided into upper, middle and lower segment, first lean solvent, the first half lean solvents
It is located at upper section with the feeding position of the second half lean solvents；The first richness CO2The withdrawn position of solvent is located at the bottom in middle section；
The inner cavity of the second absorption tower is divided into upper, middle and lower segment by third catch box (21) and the 4th catch box (22), institute
State the second richness CO2Withdrawn position be located at the bottom in middle section.
3. the purification method of unstripped gas according to claim 2, it is characterised in that the solvent is methanol, MDEA solvent
Or NHD solvent.
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| CN201611062867.5A CN106390686B (en) | 2016-11-28 | 2016-11-28 | A kind of purification method of unstripped gas |
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| CN100415346C (en) * | 2005-06-02 | 2008-09-03 | 中国寰球工程公司 | Method for purifying carbonyl gas through methanol in low temperature |
| WO2013022895A2 (en) * | 2011-08-08 | 2013-02-14 | Fluor Technologies Corporation | Methods and configurations for h2s concentration in acid gas removal |
| DE102012016643A1 (en) * | 2012-08-09 | 2014-02-13 | Linde Aktiengesellschaft | Process for the selective desulfurization of a synthesis gas |
| CN102806000B (en) * | 2012-09-05 | 2015-05-20 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step low-temperature methanol washing method |
| DE102015005203A1 (en) * | 2015-04-23 | 2016-10-27 | Linde Aktiengesellschaft | Process and apparatus for decomposing synthesis gases |
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