CN117839391A - Zero-carbon-emission low-temperature methanol washing desulfurization system and method - Google Patents
Zero-carbon-emission low-temperature methanol washing desulfurization system and method Download PDFInfo
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- CN117839391A CN117839391A CN202410103450.7A CN202410103450A CN117839391A CN 117839391 A CN117839391 A CN 117839391A CN 202410103450 A CN202410103450 A CN 202410103450A CN 117839391 A CN117839391 A CN 117839391A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 246
- 238000005406 washing Methods 0.000 title claims abstract description 69
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 23
- 230000023556 desulfurization Effects 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 14
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 61
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 61
- 239000011593 sulfur Substances 0.000 claims abstract description 61
- 238000011084 recovery Methods 0.000 claims abstract description 46
- 230000008929 regeneration Effects 0.000 claims abstract description 44
- 238000011069 regeneration method Methods 0.000 claims abstract description 44
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 17
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000002994 raw material Substances 0.000 claims description 24
- 239000003507 refrigerant Substances 0.000 claims description 14
- 230000003009 desulfurizing effect Effects 0.000 claims description 10
- 238000005201 scrubbing Methods 0.000 claims description 7
- 239000002253 acid Substances 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 230000006837 decompression Effects 0.000 claims description 3
- QFHYHYSMAHUARD-UHFFFAOYSA-N [S].CO Chemical compound [S].CO QFHYHYSMAHUARD-UHFFFAOYSA-N 0.000 claims description 2
- 238000005507 spraying Methods 0.000 claims description 2
- 238000004891 communication Methods 0.000 claims 12
- 238000007701 flash-distillation Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 abstract description 7
- 239000000126 substance Substances 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 94
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- -1 S and the like Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000011278 co-treatment Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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- Gas Separation By Absorption (AREA)
Abstract
The invention provides a zero-carbon-emission low-temperature methanol washing desulfurization system and a zero-carbon-emission low-temperature methanol washing desulfurization method. The zero-carbon-emission low-temperature methanol washing desulfurization system comprises: the device comprises a washing tower, a medium-pressure flash tower, a heat regeneration tower, a methanol-water separation tower, a liquid separating tank, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a fifth heat exchanger, a circulating gas compressor and a sulfur recovery tail gas compressor; the outlet at the top of the thermal regeneration tower is communicated with the inlet of the sulfur recovery system through a fifth heat exchanger, and the gas outlet of the sulfur recovery system is communicated with a raw gas pipeline. The zero-carbon-emission low-temperature methanol washing desulfurization system combines the low-temperature methanol washing system with the sulfur recovery system, compresses tail gas of the sulfur recovery system back to raw gas of low-temperature methanol washing, and realizes zero emission of carbon and zero emission of sulfur-containing substances. The invention relates to a zero-carbon-emission low-temperature methanol washing desulfurization system which is suitable for CO in feed gas 2 The content is lower, and the purification requirement is a low-temperature methanol washing system only needing desulfurization.
Description
Technical Field
The invention relates to a gas purification technology in the field of coal chemical industry, in particular to a zero-carbon-emission low-temperature methanol washing desulfurization system and method.
Background
The raw material gas of the coal chemical plant often contains CO 2 、H 2 S, etc., which are required to be removed by a low temperature methanol scrubbing process to obtain a clean synthesis gas meeting downstream requirements. The low-temperature methanol washing and purifying method is a physical absorption method, and uses methanol to carry out CO treatment under the low-temperature condition (-70 to minus 30 ℃) 2 、H 2 The physical characteristics of high solubility and high selectivity of acid gas such as S and the like, and methanol is used as a solvent to remove the acid gas from raw material gas, and the method has the advantages of strong absorption capacity, high purification degree, good selectivity and the like, and is widely applied to modern large-scale coal chemical equipment.
The low-temperature methanol is eluted and absorbed to remove the acid medium CO in the raw material gas 2 、H 2 S, COS in the regeneration process of the obtained rich methanol, CO can be obtained by low-pressure desorption 2 CO obtained by stripping product gas with nitrogen gas 2 And N 2 The mixture is discharged as tail gas; and the H-enriched product is obtained after thermal regeneration 2 S, COS as feed to the sulfur recovery process. Methanol-rich low pressure desorption of CO 2 At the time, the temperature of the solution is due to CO 2 The desorption absorbs heat and the temperature is reduced, so that the system obtains low temperature of about-70 ℃ to ensure the purification index and CO 2 The sulfur content in the product gas and the tail gas meets the environmental protection emission standard.
After the upstream and downstream processes are optimized, the methanol washing feed gas is unconverted feed gas, CO 2 Lower content and no need for removal. The low-temperature methanol washing only needs to remove sulfur, and has a small amount of CO 2 Dissolved in methanol. Dissolving CO in methanol 2 Less, low pressure flash and stripping are no longer considered and simplified flow design is required.
At present, main components and contents in tail gas of a sulfur recovery system are shown in table 1, so that the tail gas cannot be directly discharged, and the tail gas is required to be matched with low-temperature methanol washing to realize zero discharge.
TABLE 1 Main Components and content in the Sulfur recovery System exhaust gas
Disclosure of Invention
The invention aims to solve the problems that the conventional low-temperature methanol washing and sulfur recovery system is unreasonable in configuration, so that the flow is complex and the tail gas cannot reach the emission standard, and provides a zero-carbon-emission low-temperature methanol washing desulfurization system which is used for optimally designing a low-temperature methanol washing system and has no tail gas emission; and then the low-temperature methanol washing system is combined with the sulfur recovery system, and tail gas of the sulfur recovery system is compressed back to the raw material gas fed into the low-temperature methanol washing, so that zero emission of carbon and zero emission of sulfur-containing substances are realized.
In order to achieve the above purpose, the invention adopts the following technical scheme: a zero carbon emission low temperature methanol wash desulfurization system comprising: a washing tower C-01, a medium-pressure flash tower C-02, a heat regeneration tower C-03, a methanol-water separation tower C-04, a liquid separating tank V-01, a first heat exchanger E-01, a second heat exchanger E-02, a third heat exchanger E-03, a fourth heat exchanger E-04, a fifth heat exchanger E-05, a circulating gas compressor K-01 and a sulfur recovery tail gas compressor K-02, and a matched sulfur recovery system;
the feed gas pipeline is communicated with an inlet of the liquid separating tank V-01 through a first heat exchanger E-01; the bottom outlet of the liquid separating tank V-01 is communicated with the methanol-water separation tower C-04 through a fourth heat exchanger E-04, and the top outlet of the liquid separating tank V-01 is communicated with the lower section of the washing tower C-01; the top outlet of the washing tower C-01 is communicated with the outside of the boundary region through a first heat exchanger E-01; the bottom outlet of the washing tower C-01 is communicated with the inlet of the middle-pressure flash tower C-02, the top gas outlet of the middle-pressure flash tower C-02 is communicated with a raw gas pipeline through a circulating gas compressor K-01, the bottom outlet of the middle-pressure flash tower C-02 is communicated with the inlet of the upper section of the heat regeneration tower C-03 through a third heat exchanger E-03, and the bottom outlet of the heat regeneration tower C-03 is communicated with the inlet of the upper section of the washing tower C-01 through the third heat exchanger E-03 and a second heat exchanger E-02 in sequence; the bottom outlet of the thermal regeneration tower C-03 is communicated with the top inlet of the methanol-water separation tower C-04 through a fourth heat exchanger E-04; the outlet at the top of the thermal regeneration tower C-03 is communicated with the inlet of the sulfur recovery system through a fifth heat exchanger E-05, and the tail gas outlet of the sulfur recovery system is communicated with the inlet pipeline of the circulating gas compressor through a sulfur recovery tail gas compressor.
Further, the raw material gas pipeline is communicated with a first heat exchanger E-01 heat medium inlet, and a first heat exchanger E-01 heat medium outlet is communicated with a liquid separating tank V-01 inlet.
Further, the top outlet of the washing tower C-01 is communicated with the refrigerant inlet of the first heat exchanger E-01, and the refrigerant outlet of the first heat exchanger E-01 is communicated with the outside of the boundary region.
Further, the bottom outlet of the medium-pressure flash tower C-02 is communicated with the refrigerant inlet of the third heat exchanger E-03, and the refrigerant outlet of the third heat exchanger E-03 is communicated with the upper inlet of the heat regeneration tower C-03.
Further, the bottom outlet of the heat regeneration tower C-03 is communicated with the third heat exchanger E-03 heat medium inlet through a pump P-01, the third heat exchanger E-03 heat medium outlet is communicated with the second heat exchanger E-02 heat medium inlet, and the second heat exchanger E-02 heat medium outlet is communicated with the upper inlet of the washing tower C-01.
Further, the bottom outlet of the heat regeneration tower C-03 is communicated with the heat medium inlet of the fourth heat exchanger E-04 through a pump P-01, and the heat medium outlet of the fourth heat exchanger E-04 is communicated with the top inlet of the methanol-water separation tower C-04.
Further, the bottom outlet of the liquid separating tank V-01 is communicated with the refrigerant inlet of the fourth heat exchanger E-04, and the refrigerant outlet of the fourth heat exchanger E-04 is communicated with the methanol-water separation tower C-04.
Further, the bottom outlet of the thermal regeneration tower C-03 is communicated with a raw material gas pipeline.
Further, the top outlet of the heat regeneration tower C-03 is communicated with the inlet of a fifth heat exchanger E-05 heat medium, and the outlet of the fifth heat exchanger E-05 heat medium is communicated with the inlet of the sulfur recovery system.
Further, the sulfur recovery system is a system capable of converting sulfide into sulfur or sulfuric acid products and discharging tail gas.
Further, the tail gas outlet of the sulfur recovery system is communicated with the inlet pipeline of the circulating gas compressor K-01 through the sulfur recovery tail gas compressor K-02, and the outlet of the circulating gas compressor K-01 is communicated with the raw material gas pipeline.
Further, the top outlet of the methanol-water separation tower C-04 is communicated with a thermal regeneration tower C-03.
Further, the zero-carbon-emission low-temperature methanol washing desulfurization system is suitable for CO in feed gas 2 The content is lower, and the purification requirement is a low-temperature methanol washing system only needing desulfurization.
The invention also discloses a sulfur eluting method for the low-temperature methanol with zero carbon emission, which comprises the following steps: the raw material gas fed into the low-temperature methanol washing is mixed with the circulating flash gas and sprayed with the anti-icing methanol. The raw material gas is cooled by a cooler E-01 and then enters a liquid separation tank V-01, and water and spray methanol in the raw material gas are separated; feeding the separated raw gas into a washing tower C-01, washing and desulfurizing by using low-temperature methanol, and sending the purified gas at the top of the washing tower C-01 out of a boundary region after heat exchange by a first heat exchanger E-01; the bottom of the washing tower C-01 contains sulfur and a small amount of CO 2 The methanol rich in (2) is decompressed and then is subjected to decompression flash evaporation in a medium-pressure flash tower C-02 to recover effective gas; the rich methanol at the bottom of the medium-pressure flash tower C-02 is subjected to heat exchange (heating) by a third heat exchanger E-03 and then enters a thermal regeneration tower C-03 for regeneration, and lean methanol at the bottom of the thermal regeneration tower C-03 is sent to the top of a washing tower C-01 after being boosted and cooled; the regenerated acid gas at the top of the thermal regeneration tower C-03 is cooled by a fifth heat exchanger and sent to a sulfur recovery system;
the tail gas of the sulfur recovery system is compressed to the pressure equivalent to that of flash gas of a low-temperature methanol washing medium-pressure flash tower C-02 by a sulfur recovery tail gas compressor K-02, and is compressed by a recycle gas compressor K-01 together with flash gas of the medium-pressure flash tower C-02 and then returns to the feed gas.
Further, the zero-carbon-emission low-temperature methanol sulfur eluting method is suitable for CO in the feed gas 2 The content is lower, and the purification requirement is a low-temperature methanol washing system only needing desulfurization.
According to the zero-carbon-emission low-temperature methanol washing desulfurization system and method, the low-temperature methanol washing system and the sulfur recovery system are combined, tail gas of the sulfur recovery system is pressed back into raw gas of low-temperature methanol washing, and zero emission of carbon and zero emission of sulfur-containing substances are realized. In particular, the present invention has the following advantages over the prior art:
1) When there is a hydrogen source outside the system, low CO 2 The concentration of raw gas (such as unconverted gas) is only required to be desulfurized, CO 2 The zero-carbon emission low-temperature methanol washing and desulfurizing system is only provided with a desulfurizing tower (a washing tower C-01), and sulfur in the raw material gas is removed by using low-temperature methanol; no longer is provided with low-voltage flashSteaming and stripping, namely removing heat and regenerating after medium-pressure flash evaporation and heat exchange of the rich methanol, reducing the flow, saving the investment and facilitating the operation; CO after supplementing hydrogen with purified gas 2 Becomes the raw material for the subsequent reaction.
2) The zero-carbon-emission low-temperature methanol washing desulfurization system has no exhaust gas, realizes zero emission of carbon, and simultaneously has no emission of sulfide-containing gas.
3) The tail gas of the sulfur recovery system is compressed back into the raw gas for low-temperature methanol washing, and the tail gas of the sulfur recovery system is not discharged outside the boundary region, so that zero emission of sulfide is realized.
Drawings
FIG. 1 is a flow chart of a zero carbon rejection low temperature methanol wash desulfurization system.
Detailed Description
The invention is further illustrated by the following examples:
example 1
The embodiment discloses a zero-carbon-emission low-temperature methanol washing and desulfurizing system, which is applicable to a low-temperature methanol washing system with only raw material gas desulfurization.
Specifically, a flow chart of the zero-carbon-emission low-temperature methanol washing desulfurization system is shown in fig. 1, and comprises the following steps: the system comprises a washing tower C-01, a medium-pressure flash tower C-02, a heat regeneration tower C-03, a methanol-water separation tower C-04, a sulfur recovery system, a liquid separating tank V-01, a first heat exchanger E-01, a second heat exchanger E-02, a third heat exchanger E-03, a fourth heat exchanger E-04, a fifth heat exchanger E-05, a circulating gas compressor K-01 and a sulfur recovery tail gas compressor K-02, and a matched sulfur recovery system;
the feed gas pipeline is communicated with a first heat exchanger E-01 heat medium inlet, and a first heat exchanger E-01 heat medium outlet is communicated with a liquid separating tank V-01 inlet; the bottom outlet of the liquid separating tank V-01 is communicated with the refrigerant inlet of the fourth heat exchanger E-04, and the refrigerant outlet of the fourth heat exchanger E-04 is communicated with the methanol-water separation tower C-04. The top outlet of the liquid separating tank V-01 is communicated with the lower section of the washing tower C-01; the top outlet of the washing tower C-01 is communicated with the refrigerant inlet of the first heat exchanger E-01, and the refrigerant outlet of the E-01 is communicated with the outside of the boundary region; the bottom outlet of the washing tower C-01 is communicated with the inlet of the medium-pressure flash tower C-02, the top gas outlet of the medium-pressure flash tower C-02 is communicated with a raw gas pipeline through a circulating gas compressor K-01, the bottom outlet of the medium-pressure flash tower C-02 is communicated with the refrigerant inlet of a third heat exchanger E-03, the refrigerant outlet of the third heat exchanger E-03 is communicated with the upper inlet of the heat regeneration tower C-03, the bottom outlet of the heat regeneration tower C-03 is communicated with the heat medium inlet of the third heat exchanger E-03 through a pump P-01, the heat medium outlet of the third heat exchanger E-03 is communicated with the heat medium inlet of a second heat exchanger E-02, and the heat medium outlet of the second heat exchanger E-02 is communicated with the upper inlet of the washing tower C-01. The bottom outlet of the heat regeneration tower C-03 is communicated with the heat medium inlet of the fourth heat exchanger E-04 through a pump P-01, and the heat medium outlet of the fourth heat exchanger E-04 is communicated with the top inlet of the methanol-water separation tower C-04. The top outlet of the methanol-water separation tower C-04 is communicated with the thermal regeneration tower C-03. And the bottom outlet of the thermal regeneration tower C-03 is communicated with a raw material gas pipeline. The top outlet of the thermal regeneration tower C-03 is communicated with the inlet of a fifth heat exchanger E-05 heat medium, the outlet of the fifth heat exchanger E-05 heat medium is communicated with the inlet of a sulfur recovery system, and the gas outlet of the sulfur recovery system is communicated with the inlet pipeline of a circulating gas compressor K-01 through a sulfur recovery tail gas compressor K-02; the outlet pipeline of the circulating gas compressor K-01 is communicated with the raw material pipeline.
The sulfur recovery system converts sulfide into sulfur or sulfuric acid products and discharges tail gas.
Example 2
The embodiment discloses a sulfur eluting method for low-temperature methanol with zero carbon emission, which adopts the system described in the embodiment 1 and comprises the following steps: mixing the unconverted raw material gas washed by low-temperature methanol with the circulating flash gas and spraying the anti-icing methanol. The raw material gas is cooled by a cooler E-01 and then enters a liquid separation tank V-01, and water and spray methanol in the raw material gas are separated; feeding the separated raw gas into a washing tower C-01, washing and desulfurizing by using low-temperature methanol, and sending the purified gas at the top of the washing tower C-01 out of a boundary region after heat exchange by a first heat exchanger E-01; the bottom of the washing tower C-01 contains sulfur and a small amount of CO 2 The methanol rich in (2) is decompressed and then is subjected to decompression flash evaporation in a medium-pressure flash tower C-02 to recover effective gas; the rich methanol at the bottom of the medium-pressure flash tower C-02 is subjected to heat exchange (heating) by a third heat exchanger E-03 and then enters a thermal regeneration tower C-03 for regeneration, and lean methanol at the bottom of the thermal regeneration tower C-03 is subjected to pressure boosting, cooling and washingThe top of the tower C-01; the regenerated acid gas at the top of the thermal regeneration tower C-03 is cooled by a fifth heat exchanger and sent to a sulfur recovery system;
and compressing the tail gas of the sulfur recovery system to the pressure equivalent to that of flash gas of the low-temperature methanol washing medium-pressure flash tower C-02 by a sulfur recovery tail gas compressor K-02, and compressing the tail gas and flash gas of the medium-pressure flash tower C-02 together by a circulating gas compressor K-01 to return to the raw gas.
The zero-carbon-emission low-temperature methanol sulfur-eluting method is suitable for CO in feed gas 2 The content is lower, and the purification requirement is a low-temperature methanol washing system only needing desulfurization.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (10)
1. A zero carbon emission low temperature methanol wash desulfurization system, comprising: the device comprises a washing tower, a medium-pressure flash tower, a heat regeneration tower, a methanol-water separation tower, a liquid separating tank, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a fifth heat exchanger, a circulating gas compressor and a sulfur recovery tail gas compressor;
the feed gas pipeline is communicated with the inlet of the liquid separating tank through a first heat exchanger; the outlet at the bottom of the liquid separating tank is communicated with the methanol-water separation tower through a fourth heat exchanger, and the outlet at the top of the liquid separating tank is communicated with the lower section of the washing tower; the outlet at the top of the washing tower is communicated with the outside of the boundary region through a first heat exchanger; the bottom outlet of the washing tower is communicated with the inlet of the middle-pressure flash tower, the gas outlet at the top of the middle-pressure flash tower is communicated with a raw material gas pipeline through a circulating gas compressor, the bottom outlet of the middle-pressure flash tower is communicated with the inlet of the upper section of the thermal regeneration tower through a third heat exchanger, and the bottom outlet of the thermal regeneration tower is communicated with the inlet of the upper section of the washing tower through the third heat exchanger and a second heat exchanger in sequence; the bottom outlet of the thermal regeneration tower is communicated with the top inlet of the methanol-water separation tower through a fourth heat exchanger; and the outlet at the top of the thermal regeneration tower is communicated with the inlet of the sulfur recovery system through a fifth heat exchanger, and the tail gas outlet of the sulfur recovery system is communicated with the inlet pipeline of the circulating gas compressor through a sulfur recovery tail gas compressor.
2. The zero carbon rejection low temperature methanol scrubbing and desulfurization system of claim 1, wherein the feed gas line is in communication with a first heat exchanger heat medium inlet, and wherein the first heat exchanger heat medium outlet is in communication with a knock out pot inlet.
3. The zero carbon rejection low temperature methanol scrubbing and desulfurizing system according to claim 1, wherein the bottom outlet of the medium pressure flash tower is in communication with a third heat exchanger refrigerant inlet, and the third heat exchanger refrigerant outlet is in communication with an upper section inlet of the thermal regeneration tower.
4. The zero carbon rejection low temperature methanol scrubbing and desulfurizing system according to claim 1, wherein the bottom outlet of the thermal regeneration tower is communicated with a third heat exchanger heat medium inlet through a pump, the third heat exchanger heat medium outlet is communicated with a second heat exchanger heat medium inlet, and the second heat exchanger heat medium outlet is communicated with an upper section inlet of the scrubbing tower.
5. The zero carbon rejection low temperature methanol wash desulfurization system of claim 1, wherein the thermal regenerator bottom outlet is in communication with a fourth heat exchanger heat medium inlet via a pump, the fourth heat exchanger heat medium outlet being in communication with a methanol-water separator top inlet.
6. The zero carbon rejection low temperature methanol scrubbing and desulfurizing system of claim 1, wherein the bottom lean methanol outlet of the thermal regeneration tower is in communication with a feed gas line.
7. The zero carbon rejection low temperature methanol wash sulfur removal system of claim 1 wherein the top outlet of the thermal regeneration column is in communication with a fifth heat exchanger heat medium inlet, the fifth heat exchanger heat medium outlet being in communication with a sulfur recovery system inlet.
8. The zero carbon rejection low temperature methanol scrubbing and desulfurizing system according to claim 1, wherein the sulfur recovery system tail gas outlet is in communication with a recycle gas compressor inlet line via a sulfur recovery tail gas compressor, and the recycle gas compressor outlet is in communication with a feed gas line.
9. The zero carbon rejection low temperature methanol wash sulfur removal system of claim 1 wherein the methanol to water separation column top outlet is in communication with a thermal regeneration column.
10. The zero-carbon-emission low-temperature methanol sulfur eluting method is characterized by comprising the following steps of: after spraying methanol on the raw material gas, cooling the raw material gas by a cooler, and then feeding the raw material gas into a liquid separating tank to separate water and sprayed methanol in the raw material gas; feeding the separated raw material gas into a washing tower, washing and desulfurizing by using low-temperature methanol, and sending purified gas at the top of the washing tower out of a boundary region after heat exchange by a first heat exchanger; sulfur and small amount of CO at the bottom of the scrubber 2 The methanol rich in (2) is decompressed and then subjected to decompression flash evaporation in a medium-pressure flash tower to recover effective gas; the rich methanol at the bottom of the medium-pressure flash distillation tower enters a heat regeneration tower for regeneration after heat exchange by a third heat exchanger, and lean methanol at the bottom of the heat regeneration tower is sent to the top of a washing tower after pressure boosting and cooling; the regenerated acid gas at the top of the thermal regeneration tower is cooled by a fifth heat exchanger and sent to a sulfur recovery system;
the tail gas of the sulfur recovery system is boosted to be equivalent to the pressure of flash steam of the low-temperature methanol washing medium-pressure flash tower through a tail gas compressor, and is compressed together with flash gas of the medium-pressure flash tower through a circulating gas compressor and then returns to the feed gas.
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| CN202410103450.7A CN117839391A (en) | 2024-01-25 | 2024-01-25 | Zero-carbon-emission low-temperature methanol washing desulfurization system and method |
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| CN202410103450.7A CN117839391A (en) | 2024-01-25 | 2024-01-25 | Zero-carbon-emission low-temperature methanol washing desulfurization system and method |
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