CN106390686A - Raw material gas purification method - Google Patents
Raw material gas purification method Download PDFInfo
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- CN106390686A CN106390686A CN201611062867.5A CN201611062867A CN106390686A CN 106390686 A CN106390686 A CN 106390686A CN 201611062867 A CN201611062867 A CN 201611062867A CN 106390686 A CN106390686 A CN 106390686A
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- solvent
- unstripped gas
- absorption tower
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- rich
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- 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
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- 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 invention relates to a raw material gas purification method, which is characterized by comprising the following steps that first raw material gas enters a first absorption tower from the bottom; a first lean solvent, a first semi-lean solvent and a second semi-lean solvent enter the first absorption tower from the upper part; impurity ingredients such as CO2 and H2S in the first raw material gas are washed out; first purification gas is obtained on the tower top of the first absorption tower; a first CO2-rich solvent extracted out from the middle-lower part of the first absorption tower is divided into two strands; the first strand enters a gas extraction tower from the top; the second strand is sent to the outside; the second raw material gas enters the second absorption tower from the bottom; the second lean solvent enters the second absorption tower from the top; acid gas in the second raw material gas is eluted; the second strand of CO2-rich solvent is extracted out from the middle-lower part of the second absorption tower; the eluted purification gas is exhausted and enters the gas extraction tower from the bottom; the gas extraction is performed on the first strand of CO2-rich solvent; the purification gas after the gas extraction is exhausted out; the first semi-lean solvent is obtained from the bottom of the gas extraction tower.
Description
Technical field
The present invention relates to a kind of method for gas purification being applied to coal chemical technology, refer specifically to one kind and can purify two kinds simultaneously
The method of unstripped gas.
Background technology
Low-temp methanol is washed is, be widely used in coal (petroleum coke) or residual oil be raw material production synthesis ammonia, town gas,
Sour gas in the device of industrial hydrogen, synthesizing methanol or other C-1 chemistry product, in removing product.Its process is to use low-temp methanol
Absorb the sour gas in gaseous mixture, usually CO2And H2S, then make methanol and acid edema caused by disorder of QI through decompression desorbing, air stripping, thermal regeneration
Open, reach the purpose of separation and recovery.Methanol reduces with the rising of temperature to the absorbability of sour gas.For improving methanol pair
The absorbability of sour gas, reduces solvent circulating load it is necessary to maintain the absorption process of washing device for methanol to operate at low temperature.Methanol
The low-temperature heat source of cleaning device, one is to supplement cold by ice maker to system, and two is by CO in solution2Refrigeration by adsorption is maintaining.
Improve it is often necessary to process the desulfurization and decarburization of conversion gas simultaneously with require to low temperature washing device for methanol, especially
It is desulfurization and decarburization while plurality of raw materials gas, there is presently no the technology of correlation.
Content of the invention
The technical problem to be solved be present situation for prior art provide one kind can simultaneously desulfurization and decarburization and
The raw material gas purifying method of two kinds of unstripped gas can be purified simultaneously.
The present invention solves the technical scheme that adopted of above-mentioned technical problem：The purification method of this unstripped gas, its feature exists
In comprising the steps：
First unstripped gas enters in the first absorption tower from bottom；First lean solvent, the first half lean solvents from stripping tower
Enter described first absorption tower with from the second half lean solvents out-of-bounds from top, and described first lean solvent, the first half lean
The discharge position that enters of solvent and the second half lean solvents is arranged from top to bottom successively；
First unstripped gas flows in described first absorption tower from bottom to top, with detergent counter current contacting, the first unstripped gas
In CO2And H2The impurity compositions such as S are washed out；Tower top on described first absorption tower obtains the first purified gas；From the described first suction
The middle and lower part receiving tower extracts the first rich CO out2Solvent；
Described first rich CO2Solvent is divided into two strands, wherein first gang rich CO2Solvent enters in described stripping tower from top；The
Two gangs of rich CO2Solvent send out-of-bounds；
Second unstripped gas from bottom enter second absorption tower, the second lean solvent from top enter described second absorption tower, two
Person's counter current contacting in second absorption tower, the sour gas in eluting second unstripped gas；Extract the from the middle and lower part of second absorption tower out
Two gangs of rich CO2Solvent；Purified gas after eluting are discharged from the top of second absorption tower, enter from the bottom of described stripping tower, right
Described first gang rich CO2Solvent carries out air stripping；
The second purified gas after air stripping are discharged from the top of described stripping tower, obtain described the in the bottom of described stripping tower
Half lean solvent.
H is contained in preferably described first unstripped gas and described second unstripped gas2：75%～15%, CO：75%～0.1%,
CO2：50%～2%, H2S：1%～0.0001%；Water content be saturated water content at temperature and pressure；Described first
The temperature of unstripped gas and described second unstripped gas is 50～-35 DEG C, and pressure is 2～8.5MPaG.
The ratio of described first lean solvent and described first unstripped gas is 0.1～10kg：1Nm3.
The ratio of described the first half lean solvents and the second half lean solvents and described first unstripped gas is respectively 0.1～10kg：
1Nm3With 0.01～10kg：1Nm3.
Described first gang rich CO2The ratio of solvent and described second unstripped gas is 0.01～10kg：1Nm3.
The ratio of described second rich co2 solvent and described second unstripped gas is 0.1～10kg：1Nm3.
The ratio of described second lean solvent and described second unstripped gas is 0.1～10kg：1Nm3.；
The reaction condition of described stripping tower is 0.2～8.5MPaG, 10～-70 DEG C.
The inner chamber on described first absorption tower is divided into upper, middle and lower segment by the first catch box and the second catch box, and described
The discharge position that enters of one lean solvent, the first half lean solvents and the second half lean solvents is located at epimere；Described first rich CO2The extraction of solvent
Position is located at the bottom in stage casing；
The inner chamber of described second absorption tower is divided into upper, middle and lower segment by the 3rd catch box and the 4th catch box, and described
Two rich CO2Withdrawn position be located at stage casing bottom.
Described solvent can be methanol, MDEA solvent or NHD solvent；Preferably methanol.
Compared with prior art, raw material gas purifying method provided by the present invention can purify two kinds of raw materials simultaneously, and second
Can be as the air stripping source of the gas of the lyosoption of the first unstripped gas, to rich CO after raw material gas purifying2Solvent is regenerated, half obtaining
Lean solvent can increase in the second purified gas as the cleaning solvent (or cleaning solvent of the second unstripped gas) of the first unstripped gas simultaneously
CO2Content, energy conservation and consumption reduction effects are notable, and can greatly reduce the operational load of the follow-up parsing of rich solvent and regenerative system,
Reduce the consumption of lean solvent and half lean solvent, thus reducing the energy consumption of solvent regeneration system further.
It is used in combination disclosure is particularly well suited to purifying as conversion gas purification generation hydrogen and non-shifting gas and generating fuel gas.
Brief description
Fig. 1 is embodiment of the present invention schematic flow sheet.
Specific embodiment
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
As shown in figure 1, the inner chamber on the first absorption tower 1 used in the method for this unstripped gas passes through the first catch box 11 He
Second catch box 12 is divided into upper, middle and lower segment, the first poor methanol, the first half poor methanols and the second half poor methanols enter discharge position
Positioned at epimere；First rich CO2The withdrawn position of methanol is located at the bottom in stage casing；The inner chamber of second absorption tower passes through the 3rd catch box
21 and the 4th catch box 22 be divided into upper, middle and lower segment, the second rich CO2Withdrawn position be located at stage casing bottom.
Supporting for the present embodiment multiple stage gasification furnace is worked, that is, the upstream of this device is provided with multiple stage gasification furnace output and slightly synthesizes
Gas, a portion through CO converting means, by most CO by with H2There is transformationreation in O, generate CO2And H2, obtain
Conversion gas first unstripped gas；Another part crude synthesis gas do not pass through CO converting means, and merely through in recovery crude synthesis gas
After heat and gas-water separation, enter this device 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 obtaining after first raw material gas purifying
Purified gas consist of H2：98.9%, N2：0.39%, CO：0.6%, AR：0.14%, CH4：0.12%, flow about 24.3 ten thousand Nm3/
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 obtaining after second raw material gas purifying
Purified gas consist of 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 generate electricity for IGCC as fuel gas and use.
Concretely comprise the following steps：
Temperature is -20 DEG C, pressure is the first unstripped gas 437825Nm of 5.63MPaG3/ h, enters the first absorption from bottom
In tower 1；Temperature be -50 DEG C the first poor methanol, temperature be -36 DEG C of the first half poor methanols from stripping tower 3 and temperature be -
58 DEG C enter the first absorption tower 1 from the second half poor methanols out-of-bounds from epimere, the first poor methanol, the first half poor methanols and the
The discharge position that enters of 2 half poor methanols is arranged from top to bottom successively；
First unstripped gas flows in the first absorption tower 1 from bottom to top, 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 from the first absorption tower 1
The first rich CO is extracted in portion out2Methanol；
First rich CO2Methanol is divided into two strands, wherein first gang rich CO2Methanol enters in described stripping tower 3 from top；Second
The rich CO of stock2Methanol send out-of-bounds；First gang of rich CO2Methanol and second gang of rich CO2The molar flow of methanol is than for 0.3.
Temperature is -22 DEG C, pressure is the second unstripped gas 467184Nm of 5.85MPaG3/ h enters second absorption tower from bottom
2, the second poor methanol enters second absorption tower 2, both counter current contacting in second absorption tower 2, eluting second unstripped gas from top
In sour gas；Extract the second rich CO from the middle and lower part of second absorption tower 2 out2Methanol；Purified gas after eluting are from second absorption tower 2
Top discharge, enter the bottom of stripping tower 3, to from first gang of the first absorption tower rich CO2Methanol carries out air stripping；
The second purified gas after air stripping, CO therein2Content by enter before stripping tower≤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 rich CO2The ratio of methanol and the second unstripped gas is 0.03kg/Nm3；First gang of rich CO2Methanol and second strand
Rich CO2The molar flow of methanol is than for 0.3；
The ratio of the second unstripped gas and the second poor methanol is 0.68kg/1Nm3；
The reaction condition of stripping tower 3 is 2.2MPaG, -25 DEG C.
In old process, under the treatment scale that this is implemented, for requiring supplementation with a large amount of N in the fuel gas of IGCC Plant2Or
CO2, to fill into CO2As a example gas, the CO that about requires supplementation with2Tolerance is 36139Nm3/ h, due to needing pressure match, to CO2Pressurization
To 2.2MPaG, the compression power consumption that need to increase is 4763kW.The quantity of circulating water needing is 433t/h.Device needs to arrange CO simultaneously2
Compressor, also increases the investment cost of device.
And the second purified gas in the present embodiment can use directly as fuel gas, it is 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 notable.
Claims (4)
1. a kind of purification method of unstripped gas is it is characterised in that comprise the steps：
First unstripped gas enters in the first absorption tower (1) from bottom；First lean solvent, the first half lean molten from stripping tower (3)
Agent and enter described first absorption tower (1) from top from the second half lean solvents out-of-bounds, and described first lean solvent, first
The discharge position that enters of half lean solvent and the second half lean solvents is arranged from top to bottom successively；
First unstripped gas flows in described first absorption tower (1) from bottom to top, and detergent counter current contacting, in the first unstripped gas
CO2And H2S is washed out；Obtain the first purified gas in the tower top of described first absorption tower (1)；From described first absorption tower (1)
Middle and lower part extracts the first rich CO out2Solvent；
Described first rich CO2Solvent is divided into two strands, wherein first gang rich CO2Solvent enters in described stripping tower (3) from top；The
Two gangs of rich CO2Solvent send out-of-bounds；
Second unstripped gas enters second absorption tower (2) from bottom, and the second lean solvent enters described second absorption tower (2) from top,
Both counter current contacting, the sour gas in eluting second unstripped gas in second absorption tower (2)；Under from second absorption tower (2)
Second gang of rich CO is extracted in portion out2Solvent；Purified gas after eluting are discharged from the top of second absorption tower (2), enter described stripping tower
(3) bottom, to first gang of rich CO from described first absorption tower (1)2Solvent carries out air stripping；
The second purified gas after air stripping are discharged from the top of described stripping tower (3), obtain described in the bottom of described stripping tower (3)
The first half lean solvents.
2. the purification method of unstripped gas according to claim 1 is it is characterised in that described first unstripped gas and described second
H is contained in 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；The temperature of described first unstripped gas and described second unstripped gas is 50～-35
DEG C, pressure is 2～8.5MPaG；
The ratio of described first lean solvent and described first unstripped gas is 0.1～10kg：1Nm3.
The ratio of described the first half lean solvents and the second half lean solvents and described first unstripped gas is 0.1～10kg：1Nm3With
0.01～10kg：1Nm3.
Described first gang rich CO2The ratio of solvent and described second unstripped gas is 0.01～10kg：1Nm3.
The ratio of described second lean solvent and described second unstripped gas is 0.1～10kg：1Nm3.
The ratio of described second rich co2 solvent and described second unstripped gas is 0.1～10kg：1Nm3.
The reaction condition of described stripping tower 3 is 0.2～8.5MPaG, 10～-70 DEG C.
3. unstripped gas according to claim 1 and 2 purification method it is characterised in that described first absorption tower (1) interior
Chamber is passed through the first catch box (11) and the second catch box (12) and is divided into upper, middle and lower segment, described first lean solvent, the first half lean
The discharge position that enters of solvent and the second half lean solvents is located at epimere；Described first rich CO2The withdrawn position of solvent is located at the bottom in stage casing
Portion；
The inner chamber of described second absorption tower passes through the 3rd catch box (21) and the 4th catch box (22) is divided into upper, middle and lower segment, institute
State the second rich CO2Withdrawn position be located at stage casing bottom.
4. the purification method of unstripped gas according to claim 3 is it is characterised in that described solvent is methanol, MDEA solvent
Or NHD solvent.
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| Application Number | Priority Date | Filing Date | Title |
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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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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611062867.5A CN106390686B (en) | 2016-11-28 | 2016-11-28 | A kind of purification method of unstripped gas |
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| CN106390686A true CN106390686A (en) | 2017-02-15 |
| CN106390686B CN106390686B (en) | 2019-02-01 |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1872392A (en) * | 2005-06-02 | 2006-12-06 | 中国寰球工程公司 | Method for purifying carbonyl gas through methanol in low temperature |
| CN102806000A (en) * | 2012-09-05 | 2012-12-05 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN103571545A (en) * | 2012-08-09 | 2014-02-12 | 林德股份公司 | Method for selective desulphurisation of synthetic raw gas |
| CN103889546A (en) * | 2011-08-08 | 2014-06-25 | 氟石科技公司 | Methods and configurations for h2s concentration in acid gas removal |
| CN106065342A (en) * | 2015-04-23 | 2016-11-02 | 林德股份公司 | The method and apparatus of separating synthetic gas |
-
2016
- 2016-11-28 CN CN201611062867.5A patent/CN106390686B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1872392A (en) * | 2005-06-02 | 2006-12-06 | 中国寰球工程公司 | Method for purifying carbonyl gas through methanol in low temperature |
| CN103889546A (en) * | 2011-08-08 | 2014-06-25 | 氟石科技公司 | Methods and configurations for h2s concentration in acid gas removal |
| CN103571545A (en) * | 2012-08-09 | 2014-02-12 | 林德股份公司 | Method for selective desulphurisation of synthetic raw gas |
| CN102806000A (en) * | 2012-09-05 | 2012-12-05 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN106065342A (en) * | 2015-04-23 | 2016-11-02 | 林德股份公司 | The method and apparatus of separating synthetic gas |
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