CN106474870B - A kind of sour gas re-absorption technique of mating coal water slurry gasification - Google Patents
A kind of sour gas re-absorption technique of mating coal water slurry gasification Download PDFInfo
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- CN106474870B CN106474870B CN201610986891.1A CN201610986891A CN106474870B CN 106474870 B CN106474870 B CN 106474870B CN 201610986891 A CN201610986891 A CN 201610986891A CN 106474870 B CN106474870 B CN 106474870B
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- 238000000034 method Methods 0.000 title claims abstract description 43
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 239000003245 coal Substances 0.000 title claims abstract description 16
- 238000002309 gasification Methods 0.000 title claims abstract description 16
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 13
- 239000002002 slurry Substances 0.000 title claims abstract description 12
- 230000013011 mating Effects 0.000 title claims abstract description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 222
- 238000004064 recycling Methods 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims description 98
- 230000008569 process Effects 0.000 claims description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 12
- 238000011144 upstream manufacturing Methods 0.000 claims description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 5
- 238000011143 downstream manufacturing Methods 0.000 claims description 4
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 238000007701 flash-distillation Methods 0.000 claims 1
- 230000005540 biological transmission Effects 0.000 abstract 1
- 239000002253 acid Substances 0.000 description 8
- 230000008929 regeneration Effects 0.000 description 6
- 238000011069 regeneration method Methods 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 239000006096 absorbing agent Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003250 coal slurry Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- CUZMQPZYCDIHQL-VCTVXEGHSA-L calcium;(2s)-1-[(2s)-3-[(2r)-2-(cyclohexanecarbonylamino)propanoyl]sulfanyl-2-methylpropanoyl]pyrrolidine-2-carboxylate Chemical group [Ca+2].N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1.N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1 CUZMQPZYCDIHQL-VCTVXEGHSA-L 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000012453 solvate Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 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
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing 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
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention relates to a kind of sour gas of mating coal water slurry gasification to reabsorb technique, it is characterised in that includes the following steps：Rich CO2The CO of methanol reabsorber2Mesolow flash zone carries out vacuum flashing, the CO isolated2Product pneumatic transmission is to gas ejector, the rich CO isolated2Methanol enters CO2Low pressure flash section, the semi lean solution isolated are divided into two strands, and first strand enters tail gas and reabsorb section, and second strand enters quasi- lean solution and generate section vacuum flashing, and obtained quasi- lean solution is sent out；Rich H2S methanol enters tail gas re-absorption section vacuum flashing and air lift, the gas phase parsed are absorbed again by first strand of half poor methanol, and tail gas is sent out, and the rich methanol extracted out from collecting tank enters N2Stripping section air lift；Rich methanol after air lift is pumped to subsequent handling through the charging of hot recycling tower, and gas phase enters tail gas re-absorption section from gas cap is risen between section, washed by first strand of half poor methanol.
Description
Technical field
The present invention relates to acid gas removal technique, the sour gas for referring specifically to a kind of mating coal water slurry gasification reabsorbs work
Skill.
Background technique
Based on the current resources situation of the few oily lack of gas of the more coals in China, quickly sent out by the chemical industry of raw material of coal in recent years
Exhibition, coal are obtained with H by high-temperature gasification2It is production C1 chemical industry and its derivative produce with CO crude synthesis gas as main component
The Suitable base of product.Water coal slurry pressurized gasification technology is due to conveying continuous-stable, carbon conversion with coal wide adaptation range, coal slurry
Rate is high, pressurized gasification is saved the features such as gas downstream compression energy consumption and equipment investment are few and is widely applied.Using coal gasification
It is removed in the crude synthesis gas of technique production and contains H2、CO、CO2Outside, there are also a small amount of H2S、COS、NH3, the microcomponents such as HCN, wherein
H2It is the unstripped gas of the chemical products such as synthesizing methanol, synthesis ammonia, sour gas CO2And H2S is usually the poisonous substance of synthetic catalyst,
So must be removed before synthesis procedure, to meet the requirement of downstream production and processing.
In the acid gas removal technique using methanol as lyosoption, lean solution semi lean solution acid gas removal technique is obtained
Relatively broad application.In the re-absorption process of lean solution semi lean solution acid gas removal process, a part absorbs CO2's
Rich methanol discharges the part CO dissolved in rich methanol by vacuum flashing2Afterwards, semi lean solution is generated, directly as the benefit of poor methanol
It fills lyosoption and is returned to the CO for absorbing process2Absorber portion, another part absorbs CO2And H2The rich methanol of S is dodged by decompression
It steams, the regeneration of nitrogen air lift and hot recycling realization methanol solvate, send after regenerated poor methanol tax is cold to acid gas removal and absorb
Duan Zuowei lyosoption.Lean solution semi lean solution acid gas removal process reduces thermal regeneration system load and outer to a certain extent
The consumption of portion's cooling capacity, but since semi lean solution is to CO2The re-absorption ability of gas is limited, to guarantee assimilation effect, needs in process
A large amount of semi lean solution is in CO2It absorbs and is recycled between process and re-absorption process, thereby result in gas absorber portion load and significantly increase, draw
It plays equipment investment to increase, causes the increase of power consumption, and limit the enlargement of device, simultaneously lean solution semi lean solution is acid
Thermal regeneration system energy consumption and the external cooling capacity consumption of gas removal have the space further decreased.
Summary of the invention
The technical problem to be solved by the present invention is to the statuses for the prior art to provide a kind of significant decrease sour gas
Removing means energy consumption, while the sour gas for reducing the mating coal water slurry gasification of equipment investment reabsorbs technique.
The present invention solves technical solution used by above-mentioned technical problem：The sour gas of the mating coal water slurry gasification is inhaled again
Knock off skill, it is characterised in that include the following steps：
The temperature that flash process is sent from upstream is -24 DEG C~-36 DEG C, pressure is 1.75MPaG~2.00MPaG, CO2It rubs
The rich CO that your content is 31%~36%2Methanol is entered the CO of reabsorber by top2Mesolow flash zone carries out vacuum flashing,
Control flashing pressure is 0.5MPaG~0.7MPaG；
From CO2The CO sent out at the top of mesolow flash zone2- 38 DEG C~-49 DEG C of product gas temperature, pressure 0.5MPaG~
0.7MPaG send the working gas to gas ejector as injector；
From CO2The rich CO that the bottom of mesolow flash zone is sent out2Methanol, CO2Molar content is 26%~31%, is flow to certainly
The CO of reabsorber2Low pressure flash section；Control CO2Low pressure flash section operating pressure is 0.05MPaG~0.12MPaG；
From CO2CO is sent out at the top of low pressure flash section2Product gas, is exported with gas ejector and is sent out by -59 DEG C~-65 DEG C of temperature
CO2After product gas mixing, send to downstream process；
From CO2CO in the semi lean solution that low pressure flash section bottom is sent out2Molar content is 17%~23%, is divided into two strands, wherein
First strand of semi lean solution reabsorbs section as washing methanol from the tail gas that top enters reabsorber, and second strand of semi lean solution is through half poor first
Alcohol heat exchanger recycling cooling capacity exchanges heat to after -44 DEG C~-48 DEG C, and the quasi- lean solution for entering reabsorber from top generates section；
Under the swabbing action of gas ejector, the quasi- lean solution of reabsorber is maintained to generate the operating pressure of section in 0.07MPaA
The micro-vacuum state of~0.1MPaA；
Half poor methanol vacuum flashing again in tower of section is generated into quasi- lean solution, the temperature flashed off is -61 DEG C~-65
DEG C gas extracted out by gas ejector after send to out-of-bounds；CO is sent out by the bottom that quasi- lean solution generates section2Content is 9%~12%
Quasi- lean solution, through quasi- lean pump pressurization after send to gas absorb process；
The rich H that the temperature that flash process is sent from upstream is -20 DEG C~-25 DEG C, pressure is 1.7MPaG~2.0MPaG2S
Methanol, the tail gas for entering reabsorber from middle part reabsorb vacuum flashing in section, while by from reabsorber reabsorber
N2The gas air lift of stripping section, the air lift pressure that control tail gas reabsorbs section is 0.07MPaG~0.20MPaG；In reabsorber
Tail gas reabsorbs section, rich H2CO in S methanol2And a small amount of H2S is constantly parsed, and rich methanol temperature constantly reduces, the gas phase parsed
In H2S gas is absorbed in uphill process by first strand of half poor methanol again；
The rich H that the upstream flash process is sent2S methanol and the upstream flash process send rich CO2The molar flow of methanol
Measure ratio 1:1.2~1:3；
From the tail gas of reabsorber reabsorb section at the top of send out -60 DEG C~-65 DEG C of exhaust temperature, pressure 0.07MPaG~
0.20MPaG is sent to finishing operations processing.
To guarantee that sulfur content reaches discharge standard in tail gas, the tail gas is preferably controlled and described from reabsorber
CO2The molar flow of first strand of half poor methanol of low pressure flash section bottom is than 1:1.5~1:2；
From tail gas reabsorb section collecting tank extract out rich methanol, through reabsorber circulating pump be forced into 0.5MPaG~
0.7MPaG and through rich methanol heat exchanger recycling cooling capacity exchange heat to -35 DEG C~-45 DEG C after, send to the N of reabsorber2Stripping section into
Promoting the circulation of qi mentions；
The low-pressure nitrogen that temperature is -5 DEG C~-35 DEG C, pressure is 0.4MPaG~0.7MPaG enters N from bottom2Stripping section,
The molar flow ratio of the nitrogen and the rich methanol is 1:10~1:25；N2The air lift pressure of stripping section be 0.12MPaG~
0.25MPaG；Rich methanol after air lift is pumped to subsequent handling through the charging of hot recycling tower, and gas phase enters tail gas from rising gas cap between section
Section is reabsorbed, is washed by first strand of half poor methanol.
It is preferred that the molar flow ratio of first strand of half poor methanol and second strand of half poor methanol is 1:1~1:3.
Compared with prior art, present invention tool has the advantage that：
1, the feature high using coal water slurry gasification operating pressure, introduces gas ejector, utilizes rich CO2Methanol mesolow
Flash the CO generated2Product gas is as gas ejector working gas, after half poor methanol recycles cooling capacity, aspirates in gas ejector
Negative pressure state under flash again, greatly release the CO dissolved in half poor methanol2Gas generates quasi- lean solution.
2, opposite semi lean solution, CO in quasi- lean solution2Content is lower, and the quasi- lean solution of unit quantity is to CO2Just there is stronger absorption energy
Power, the increase of absorbability reduce regeneration poor methanol dosage, while also reducing thermal regeneration system energy consumption and absorbing the cold of process
Amount consumption.
3, since quasi- lean solution is to CO2Just there is stronger absorbability, under the premise of guaranteeing air lift clean-up effect, circulation
Quantity of methyl alcohol is greatly reduced, and reduces the power consumption and equipment investment of recycle methanol.
4, quasi- lean solution substitution semi lean solution significantly reduces gas absorber portion load, it is large-scale to be conducive to device as lyosoption
Change.
Detailed description of the invention
Fig. 1 is the process 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.
Involved noun explanation in the present invention：
Rich H2S methanol：Refer to and absorbs H2S and CO2Methanol solution
Rich CO2Methanol：Refer to and only absorbs CO2Methanol solution
Semi lean solution：Refer to rich CO2Methanol is pressed in, after low pressure flash, CO2Methanol solution of the content 17%~23%
Quasi- lean solution：Refer to semi lean solution after tiny structure flashes, CO2Methanol solution of the content 9%~12%
As shown in Figure 1, the reabsorber 1 in the present embodiment is divided into four sections from top to bottom, separated between section by end socket.Wherein
Upper section is CO2Mesolow flash zone 11, middle upper section are CO2Low pressure flash section 12；Middle and lower sections are divided into two parts by catch box, collection
Liquid case above section is known as tail gas and reabsorbs section 13, is partially known as N below catch box2Stripping section 14 is provided on collecting tank 16
The liter gas cap 17 of lower tower upper section is ascended into for the gas in lower tower lower section；Lean solution generates section 15 subject to lower section.
The temperature sent of flash process is pressed from upstream is -24 DEG C~-36 DEG C, pressure be 1.75MPaG~2.00MPaG,
CO2The rich CO that molar content is 31%~36%2Methanol enters the CO of reabsorber 1 from top2Mesolow flash zone 11 carries out
Vacuum flashing, control flashing pressure are 0.5MPaG~0.7MPaG.
From the CO of reabsorber 12The CO that the top of mesolow flash zone 11 is sent out2- 38 DEG C~-49 DEG C of product gas temperature, pressure
Power 0.5MPaG~0.7MPaG send the working gas to gas ejector 7 as injector.
From the CO of reabsorber 12The rich CO that the bottom of mesolow flash zone 11 is sent out2Methanol, CO2Molar content is 26%
~31%, it flow to the CO of reabsorber 1 certainly2Low pressure flash section 12 controls CO212 operating pressure 0.05MPaG of low pressure flash section~
0.12MPaG。
From the CO of reabsorber 12The CO sent out at the top of low pressure flash section 122- 59 DEG C~-65 DEG C of product gas temperature, with gas
The CO that the outlet of injector 7 is sent out2It send after product gas mixing to downstream process and recycles cooling capacity.
From the CO of reabsorber 12CO in the semi lean solution that 12 bottom of low pressure flash section is sent out2Molar content is 17%~23%,
It is divided into two strands, wherein first gang of semi lean solution a, which reabsorbs section 13 from the tail gas that top enters reabsorber 1, is used as washing methanol, the
Two gangs of semi lean solution b enter reabsorber 1 from top after half poor methanol heat exchanger 2 recycling cooling capacity exchanges heat to -44 DEG C~-48 DEG C
Quasi- lean solution generate section 15.
The molar flow ratio for controlling first strand of half poor methanol a and second strand of half poor methanol b is 1:2.
Under the swabbing action of gas ejector 7, the operating pressure for maintaining the quasi- lean solution of reabsorber 1 to generate section 15 exists
The micro-vacuum state of 0.07MPaA~0.1MPaA, into reabsorber 1 quasi- lean solution generate section 15 half poor methanol in tower again
Secondary vacuum flashing flashes off -61 DEG C~-65 DEG C of gas temperature, through being drawn for gas ejector 7, and comes from reabsorber 1CO2
The CO sent out at the top of mesolow flash zone2After product gas mixing, gas ejector 7 is sent out.
The CO in the quasi- lean solution that the bottom that quasi- lean solution generates section 15 is sent out2Content is 9%~12%, is added through quasi- lean pump 6
After pressure, send to absorption process as absorption methanol.
The CO sent out from gas ejector 72- 54 DEG C~-60 DEG C of product gas temperature, pressure 0.05MPaG~0.12MPaG,
With the CO from reabsorber 12The CO sent out at the top of low pressure flash section2After product gas mixing, send to downstream process and recycle cooling capacity.
From upstream press flash process temperature be -20 DEG C~-25 DEG C, the richness that pressure is 1.7MPaG~2.0MPaG
H2S methanol, the tail gas for entering reabsorber 1 from middle part reabsorb section 13, reabsorb in section 13 in the tail gas of reabsorber 1, rich
H2CO in S methanol2And a small amount of H2S is constantly parsed, and rich methanol temperature constantly reduces, H2S gas is come from uphill process
The CO of reabsorber 12First gang of semi lean solution a of low pressure flash section absorbs again.
The rich H that upstream flash process is sent2S methanol and upstream flash process send rich CO2The molar flow of methanol is than 1:
1.2~1:3；
- 60 DEG C~-65 DEG C of the exhaust temperature sent out at the top of section 13, pressure are reabsorbed from the tail gas of reabsorber 1
0.07MPaG~0.20MPaG is sent to finishing operations processing.
To guarantee that sulfur content reaches discharge standard in tail gas, controls the tail gas and the CO from reabsorber2It is low
Press the molar flow of first strand of half poor methanol of flash zone bottom than 1:1.5~1:2；
The rich methanol extracted out from collecting tank 16, is forced into 0.5MPaG~0.7MPaG through reabsorber circulating pump 3 and through richness
Heat exchange of methanol device 4 recycles cooling capacity and exchanges heat to after -35 DEG C~-45 DEG C, send to reabsorber 1N2Stripping section 14, temperature be -5 DEG C~-
35 DEG C, pressure be 0.4MPaG~0.7MPaG low-pressure nitrogen enter N from bottom2Stripping section 14 utilizes low-pressure nitrogen air lift, N2
The air lift pressure of stripping section 14 is 0.12MPaG~0.25MPaG；Rich solution after air lift is sent after the pressurization of 5 feed pump of hot recycling tower
To subsequent thermal step for regeneration, gas phase enters tail gas re-absorption section 13 from gas cap 17 is risen between section, is washed by first strand of half poor methanol.
The molar flow ratio of low-pressure nitrogen and the rich methanol of the collecting tank 16 extraction is 1:10~1:25.
Comparative example
By taking the device for producing hydrogen using coal water slurry gasification gas making as an example, into effective gas (H of acid gas removal plants2+
It CO) is 210000Nm3/ h reabsorbs technique to the sour gas of lean solution semi lean solution process and mating coal water slurry gasification under this benchmark
Major parameter, which compares, is shown in Table 1.
Table 1
As can be seen from Table 1, for the device for producing hydrogen based on coal water slurry gasification gas making, sour gas provided by the present embodiment
Technique is reabsorbed, poor methanol internal circulating load is only 83% of poor methanol internal circulating load in lean solution semi lean solution process, subsequent reduction hot recycling
Load 1020KW/h reduces external cooling capacity and consumes 340KW/h, and quasi- lean solution internal circulating load is only in lean solution semi lean solution process in embodiment
The 85% of half poor methanol internal circulating load, adding up power consumption reduces 384KW/h.
Claims (2)
1. a kind of sour gas of mating coal water slurry gasification reabsorbs technique, it is characterised in that include the following steps：
The temperature come from upstream is -24 DEG C ~ -36 DEG C, pressure is 1.75MPaG~2.00MPaG, CO2Molar content is 31% ~ 36%
Rich CO2Methanol enters the CO of reabsorber (1) from top2Mesolow flash zone (11) carries out vacuum flashing, control flash distillation pressure
Power is 0.5MPaG~0.7MPaG；
The therefrom CO that the top of low pressure flash section (11) is sent out2- 38 DEG C ~ -49 DEG C of product gas temperature, 0.5 MPaG of pressure~
0.7MPaG send the working gas to gas ejector (7) as injector；
From CO2The rich CO that the bottom of mesolow flash zone (11) is sent out2Methanol, CO2Molar content is 26% ~ 31%, flow to and inhales again certainly
Receive the CO of tower (1)2Low pressure flash section (12)；Control CO2Low pressure flash section (12) operating pressure is 0.05 MPaG~0.12MPaG；
From CO2CO is sent out at the top of low pressure flash section2Product gas, is sent out with gas ejector (7) outlet by -59 DEG C ~ -65 DEG C of temperature
CO2After product gas mixing, send to downstream process；
From CO2CO in the semi lean solution that low pressure flash section (12) bottom is sent out2Molar content is 17% ~ 23%, is divided into two strands, wherein the
One semi lean solution (a) reabsorbs section (13) as washing methanol, second strand of semi lean solution from the tail gas that top enters reabsorber (1)
(b) after semi lean solution heat exchanger (2) recycling cooling capacity exchanges heat to -44 DEG C ~ -48 DEG C, the quasi- lean solution of reabsorber (1) is entered from top
It generates section (15)；
Under the swabbing action of gas ejector (7), maintain quasi- lean solution generate the operating pressure of section (15) 0.07MPaA ~
The micro-vacuum state of 0.1MPaA；
Semi lean solution vacuum flashing again in tower of section (15) is generated into quasi- lean solution, the temperature flashed off is -61 DEG C ~ -65 DEG C
Gas by gas ejector (7) extraction after sent to out-of-bounds, quasi- lean solution generate section (15) bottom send out CO2Content be 9% ~
12% quasi- lean solution is sent to gas as absorption methanol after quasi- lean pump (6) pressurization and absorbs process；
The rich H that the temperature that flash process is sent from upstream is -20 DEG C ~ -25 DEG C, pressure is the MPaG of 1.7 MPaG~2.02S methanol,
The tail gas for entering reabsorber (1) from middle part reabsorbs section (13) interior vacuum flashing, while being come from the N of reabsorber (1)2Gas
The gas air lift of section (14) is proposed, the air lift pressure that control tail gas reabsorbs section is 0.07 MPaG~0.20MPaG；In reabsorber
Tail gas reabsorbs section, rich H2CO in S methanol2And a small amount of H2S is constantly parsed, and rich methanol temperature constantly reduces, the gas phase parsed
In H2S gas is absorbed in uphill process by first strand of semi lean solution (a) again；
The rich H that upstream flash process is sent2S methanol and upstream flash process send rich CO2The molar flow of methanol is than 1:1.2~1:
3；
- 60 DEG C ~ -65 DEG C of the exhaust temperature sent out at the top of section, 0.07 MPaG~0.20 of pressure are reabsorbed from the tail gas of reabsorber
MPaG is sent to finishing operations processing；
The rich methanol that the collecting tank (16) for reabsorbing section (13) from tail gas is extracted out, is forced into 0.5 through reabsorber circulating pump (3)
The MPaG of MPaG~0.7 and through rich methanol heat exchanger (4) recycling cooling capacity exchange heat to -35 DEG C ~ -45 DEG C after, send to reabsorber (1)
N2Stripping section (14) carries out air lift；
The low-pressure nitrogen that temperature is -5 DEG C ~ -35 DEG C, pressure is the MPaG of 0.4 MPaG~0.7 enters N from bottom2Stripping section (14),
N2The air lift pressure of stripping section (14) is 0.12 MPaG~0.25MPaG；Rich methanol after air lift is through hot recycling tower feed pump (5)
It send to subsequent handling, gas phase is washed from gas cap (17) are risen between section into tail gas re-absorption section (13) by first strand of semi lean solution；
The molar flow ratio of first strand of semi lean solution (a) and second strand of semi lean solution (b) is 1:1~1:3.
2. a kind of sour gas of mating coal water slurry gasification according to claim 1 reabsorbs technique, it is characterised in that described
The molar flow ratio of low-pressure nitrogen and the rich methanol of the collecting tank (16) extraction is 1:10~1:25.
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