CN216986990U - High-efficiency energy-saving regeneration device for recycling low-temperature methanol washing carbon dioxide in grading manner - Google Patents
High-efficiency energy-saving regeneration device for recycling low-temperature methanol washing carbon dioxide in grading manner Download PDFInfo
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Abstract
The utility model discloses a high-efficiency energy-saving regeneration device for recycling low-temperature methanol to wash carbon dioxide in a grading manner, which relates to the technical field of coal chemical industry devices and comprises a sulfur-free flash tank, a sulfur-containing flash tank, a hydrogen sulfide concentration tower, a low-temperature vacuum flash tank, a low-temperature booster pump, a first-stage methanol heat exchanger, a methanol circulating pump, a second-stage methanol heat exchanger, a circulating methanol flash tank, a normal-temperature vacuum flash tank, a thermal regeneration tower, a lean methanol booster pump, a No. 1 carbon dioxide compression-expansion all-in-one machine, a No. 2 carbon dioxide compression-expansion all-in-one machine and a normal-temperature booster pump. The high-efficiency energy-saving regeneration device for recycling low-temperature methanol-washed carbon dioxide in a grading manner saves the traditional power consumption by recycling the pressure potential energy of medium-pressure carbon dioxide gas, cancels nitrogen gas stripping, and can obtain a carbon dioxide product with high purity.
Description
Technical Field
The utility model relates to the technical field of coal chemical industry devices, in particular to a high-efficiency energy-saving regeneration device for recycling low-temperature methanol-washed carbon dioxide in a grading manner.
Background
The low-temperature methanol washing process utilizes the excellent characteristic that methanol has great solubility to acid gas carbon dioxide at low temperature and high pressure, can selectively remove the carbon dioxide in the raw material gas, and is a gas purification technology which has wide application, economy and high purification degree. After absorbing a large amount of dissolved carbon dioxide gas, the low-temperature methanol needs to be regenerated through processes of reduced pressure flash evaporation, nitrogen gas stripping, heating and the like. In the prior art, on one hand, carbon dioxide gas with high pressure dissolved in low-temperature methanol is used as tail gas to be directly decompressed and sent to downstream equipment, and the pressure potential energy is not fully utilized; on the other hand, the nitrogen gas stripping causes the carbon dioxide gas to be mixed with a large amount of nitrogen, so that the purity is sharply reduced, the carbon dioxide gas cannot be reused as a carbon dioxide product, and the carbon dioxide gas can only be discharged as tail gas.
SUMMERY OF THE UTILITY MODEL
The utility model provides a high-efficiency energy-saving regeneration device for recycling low-temperature methanol to wash carbon dioxide in a grading manner, which solves the problems that the pressure potential energy of carbon dioxide dissolved in low-temperature methanol is not fully utilized and the recycling rate of carbon dioxide products is low in the prior art.
The utility model provides a high-efficiency energy-saving regeneration device for recycling low-temperature methanol washing carbon dioxide in a grading manner, which comprises a sulfur-free flash tank, a sulfur-containing flash tank, a hydrogen sulfide concentration tower, a low-temperature vacuum flash tank, a low-temperature booster pump, a first-stage methanol heat exchanger, a methanol circulating pump, a second-stage methanol heat exchanger, a circulating methanol flash tank, a normal-temperature vacuum flash tank, a thermal regeneration tower, a poor methanol booster pump, a 1# carbon dioxide compression and expansion integrated machine, a 2# carbon dioxide compression and expansion integrated machine and a normal-temperature booster pump;
a feed inlet pipeline of the sulfur-free flash tank is connected with a sulfur-free methanol pipeline, a bottom liquid phase outlet pipeline is connected with a feed inlet at the top of an upper tower of the hydrogen sulfide concentration tower, and a top gas phase outlet is respectively connected with a gas collection pipeline, an expansion end inlet of the 1# carbon dioxide compression and expansion integrated machine and an expansion end inlet of the 2# carbon dioxide compression and expansion integrated machine through pipelines;
a feed inlet pipeline of the sulfur-containing flash tank is connected with a sulfur-containing methanol pipeline, a bottom liquid phase outlet pipeline is connected with a feed inlet in the middle of an upper tower of a hydrogen sulfide concentration tower, and a top gas phase outlet is respectively connected with a gas collecting pipeline, an expansion end inlet of a 1# carbon dioxide compression and expansion integrated machine and an expansion end inlet of a 2# carbon dioxide compression and expansion integrated machine through pipelines;
a gas phase outlet at the top of an upper tower of the hydrogen sulfide concentration tower is connected with a carbon dioxide product pipeline through a pipeline, a liquid phase outlet at the bottom of the upper tower is sequentially connected with a methanol circulating pump, a cold side of a second-stage methanol heat exchanger and a feed inlet of a circulating methanol flash tank through pipelines, a discharge outlet at the bottom of a lower tower is connected with a low-temperature vacuum flash tank through a pipeline, and a feed inlet at the bottom of the lower tower is connected with the bottom of the circulating methanol flash tank through a pipeline;
a top gas phase outlet of the circulating methanol flash tank is sequentially connected with a gas collecting pipeline, an expansion end inlet of the 1# carbon dioxide compression and expansion integrated machine and an expansion end inlet of the 2# carbon dioxide compression and expansion integrated machine;
a top gas phase outlet of the low-temperature vacuum flash tank is connected with a compression end inlet of the No. 1 carbon dioxide compression and expansion integrated machine through a pipeline, and a bottom liquid phase outlet is sequentially connected with a low-temperature booster pump and a cold side inlet of the first-stage methanol heat exchanger through pipelines;
the normal-temperature vacuum flash tank is connected with a cold-side discharge port of the first-stage methanol heat exchanger through a pipeline, a bottom liquid-phase outlet is sequentially connected with feed ports of a normal-temperature booster pump and a thermal regeneration tower through pipelines, and a top gas-phase outlet is connected with a compression-end inlet of a 2# carbon dioxide compression-expansion all-in-one machine through a pipeline;
a liquid phase outlet at the bottom of the thermal regeneration tower is sequentially connected with a lean methanol booster pump, a hot side of the first-stage methanol heat exchanger, a hot side of the second-stage methanol heat exchanger and a low-temperature lean methanol pipeline through pipelines;
the export of the compression end of 1# carbon dioxide compression expansion all-in-one and the export of inflation end all loop through pipe connection admission line and hydrogen sulfide concentration tower's last bottom gas feed inlet, and the export of the compression end of 2# carbon dioxide compression expansion all-in-one and the export of inflation end also all loop through pipe connection admission line and hydrogen sulfide concentration tower's last bottom gas feed inlet.
Preferably, a first pressure reducing valve is arranged on a connecting pipeline between a feed inlet of the sulfur-free flash tank and a sulfur-free methanol pipeline, and a second pressure reducing valve is arranged on a connecting pipeline between a liquid phase outlet at the bottom of the sulfur-free flash tank and a feed inlet at the top of an upper tower of the hydrogen sulfide concentration tower.
Preferably, a third pressure reducing valve is arranged on a connecting pipeline between the feed inlet of the sulfur-containing flash tank and the sulfur-containing methanol pipeline, and a fourth pressure reducing valve is arranged on a connecting pipeline between a liquid phase outlet at the bottom of the sulfur-containing flash tank and the feed inlet in the middle of the upper tower of the hydrogen sulfide concentration tower.
Preferably, a fifth pressure reducing valve is arranged on a connecting pipeline between a discharge port at the bottom of the lower tower of the hydrogen sulfide concentration tower and the low-temperature vacuum flash tank.
Preferably, a sixth pressure reducing valve is arranged on a connecting pipeline between the normal-temperature vacuum flash tank and the cold-side discharge port of the first-stage methanol heat exchanger.
Preferably, a seventh reducing valve is arranged on a connecting pipeline between the cold side of the secondary methanol heat exchanger and the feeding hole of the circulating methanol flash tank.
The high-efficiency energy-saving regeneration device for recycling the low-temperature methanol-washed carbon dioxide by stages has the following remarkable advantages:
1. the pressure potential energy of medium-pressure carbon dioxide gas is recovered through the expansion end of the 1# carbon dioxide compression and expansion integrated machine and the compression end of the compression and expansion integrated machine is driven to work, so that the low-temperature and normal-temperature vacuum flash tanks are vacuumized, a special vacuum pump is not required to be arranged, and the traditional power consumption is saved;
2. a two-stage temperature gradient and a two-stage vacuum gradient carbon dioxide regeneration environment are established through the low-temperature and normal-temperature vacuum flash tanks, and the traditional nitrogen gas stripping process is replaced, so that a low-temperature methanol washing device does not consume a large amount of precious clean nitrogen resources;
3. because nitrogen gas stripping is cancelled, the gas discharged from the top of the hydrogen sulfide concentration tower is a carbon dioxide product with high purity, and is not tail gas containing a large amount of nitrogen components in the traditional process, so that the investment of downstream carbon dioxide extraction equipment and the electric quantity consumption of the downstream carbon dioxide extraction equipment are saved;
4. the device has the advantages of ingenious design, simple structure, small floor area, simple operation and large elasticity, does not depend on external power supply, can be applied to the transformation of the existing low-temperature methanol washing device except a newly-built device, and can separate and recover carbon dioxide in the original tail gas.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the prior art descriptions will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic structural diagram of a high-efficiency energy-saving type regeneration device for fractional recovery of low-temperature methanol-washed carbon dioxide.
Description of reference numerals:
1-sulfur-free methanol pipeline, 2-first pressure reducing valve, 3-sulfur-free flash tank, 4-second pressure reducing valve, 5-sulfur-containing methanol pipeline, 6-third pressure reducing valve, 7-sulfur-containing flash tank, 8-fourth pressure reducing valve, 9-hydrogen sulfide concentration tower, 10-low temperature vacuum flash tank, 11-low temperature booster pump, 12-first stage methanol heat exchanger, 13-methanol circulating pump, 14-second stage methanol heat exchanger, 15-circulating methanol flash tank, 16-sixth pressure reducing valve, 17-normal temperature vacuum flash tank, 18-heat regeneration tower, 19-poor methanol booster pump, 20-1# carbon dioxide compression and expansion all-in-one machine, 21-2# carbon dioxide compression and expansion all-in-one machine, 22-low temperature poor methanol pipeline, 23-carbon dioxide product pipeline, 24-a fifth pressure reducing valve, 25-a normal temperature booster pump, 26-a gas collecting pipeline, 27-an air inlet pipeline and 28-a seventh pressure reducing valve.
Detailed Description
In order to make the technical solutions of the present invention better understood and practical for those skilled in the art, the present invention is further described with reference to the following drawings and specific examples, which are not intended to limit the present invention.
Example 1
Referring to fig. 1, the utility model provides a high-efficiency energy-saving type regeneration device for recycling low-temperature methanol to wash carbon dioxide in stages, which comprises a sulfur-free flash tank 3, a sulfur-containing flash tank 7, a hydrogen sulfide concentration tower 9, a low-temperature vacuum flash tank 10, a low-temperature booster pump 11, a first-stage methanol heat exchanger 12, a methanol circulating pump 13, a second-stage methanol heat exchanger 14, a circulating methanol flash tank 15, a normal-temperature vacuum flash tank 17, a thermal regeneration tower 18, a poor methanol booster pump 19, a 1# carbon dioxide compression-expansion all-in-one machine 20, a 2# carbon dioxide compression-expansion all-in-one machine 21 and a normal-temperature booster pump 25.
The feed inlet pipeline of the sulfur-free flash tank 3 is connected with the sulfur-free methanol pipeline 1, wherein a first pressure reducing valve 2 is arranged on a connecting pipeline between the feed inlet of the sulfur-free flash tank 3 and the sulfur-free methanol pipeline 1, a bottom liquid phase outlet pipeline is connected with an upper tower top feed inlet of the hydrogen sulfide concentration tower 9, a second pressure reducing valve 4 is arranged on a connecting pipeline between a bottom liquid phase outlet of the sulfur-free flash tank 3 and the upper tower top feed inlet of the hydrogen sulfide concentration tower 9, a top gas phase outlet is respectively connected with a gas collecting pipeline 26, an expansion end inlet of the 1# carbon dioxide compression and expansion integrated machine 20 and an expansion end inlet of the 2# carbon dioxide compression and expansion integrated machine 21 through pipelines, and the expansion end is driven to do work.
The feed inlet pipeline of the sulfur-containing flash tank 7 is connected with the sulfur-containing methanol pipeline 5, wherein a third pressure reducing valve 6 is arranged on a connecting pipeline between the feed inlet of the sulfur-containing flash tank 7 and the sulfur-containing methanol pipeline 5, a bottom liquid phase outlet pipeline is connected with an upper tower middle feed inlet of the hydrogen sulfide concentration tower 9, wherein a fourth pressure reducing valve 8 is arranged on a connecting pipeline between a bottom liquid phase outlet of the sulfur-containing flash tank 7 and an upper tower middle feed inlet of the hydrogen sulfide concentration tower 9, a top gas phase outlet is respectively connected with a gas collection pipeline 26, an expansion end inlet of the 1# carbon dioxide compression and expansion all-in-one machine 20 and an expansion end inlet of the 2# carbon dioxide compression and expansion all-in-one machine 21 through pipelines, and an expansion end is driven to do work.
The upper tower top gas phase outlet pipeline of the hydrogen sulfide concentration tower 9 is connected with a carbon dioxide product pipeline 23 to obtain qualified carbon dioxide products, the upper tower bottom liquid phase outlet is sequentially connected with a methanol circulating pump 13, the cold side of a second-stage methanol heat exchanger 14 and the feed inlet of a circulating methanol flash tank 15 through pipelines, wherein a seventh reducing valve 28 is arranged on the connecting pipeline between the cold side of the second-stage methanol heat exchanger 14 and the feed inlet of the circulating methanol flash tank 15, the lower tower bottom discharge port is connected with a low-temperature vacuum flash tank 10 through a pipeline, wherein a fifth reducing valve 24 is arranged on the connecting pipeline between the lower tower bottom discharge port of the hydrogen sulfide concentration tower 9 and the low-temperature vacuum flash tank 10, and the lower tower bottom feed inlet is connected with the bottom of the circulating methanol flash tank 15 through a pipeline.
And a top gas phase outlet of the circulating methanol flash tank 15 is sequentially connected with a gas collecting pipeline 26, an expansion end inlet of the 1# carbon dioxide compression-expansion all-in-one machine 20 and an expansion end inlet of the 2# carbon dioxide compression-expansion all-in-one machine 21.
A top gas phase outlet of the low-temperature vacuum flash tank 10 is connected with a compression end inlet of the 1# carbon dioxide compression and expansion all-in-one machine 20 through a pipeline, a bottom liquid phase outlet is sequentially connected with cold side inlets of the low-temperature booster pump 11 and the first-stage methanol heat exchanger 12 through pipelines, and the compression end inlet sucks air to generate vacuum required by normal operation of the low-temperature vacuum flash tank 10.
The normal-temperature vacuum flash tank 17 is connected with a cold-side discharge port of the first-stage methanol heat exchanger 12 through a pipeline, a sixth reducing valve 16 is arranged on a connecting pipeline of the normal-temperature vacuum flash tank 17 and the cold-side discharge port of the first-stage methanol heat exchanger 12, a bottom liquid phase outlet is sequentially connected with a normal-temperature booster pump 25 and a feed inlet of the thermal regeneration tower 18 through pipelines, a top gas phase outlet is connected with a compression end inlet of the 2# carbon dioxide compression and expansion integrated machine 21 through a pipeline, and the compression end inlet sucks air to generate vacuum required by normal operation of the normal-temperature vacuum flash tank 17.
And a liquid phase outlet at the bottom of the thermal regeneration tower 18 is sequentially connected with a lean methanol booster pump 19, a hot side of the first-stage methanol heat exchanger 12, a hot side of the second-stage methanol heat exchanger 14 and a low-temperature lean methanol pipeline 22 through pipelines to obtain a low-temperature lean methanol solvent required by a downstream process.
The compression end outlet and the expansion end outlet of the 1# carbon dioxide compression and expansion integrated machine 20 are respectively connected with the gas inlet pipe 27 and the gas inlet port at the bottom of the upper tower of the hydrogen sulfide concentration tower 9 through the pipeline, and the compression end outlet and the expansion end outlet of the 2# carbon dioxide compression and expansion integrated machine 21 are respectively connected with the gas inlet pipe 27 and the gas inlet port at the bottom of the upper tower of the hydrogen sulfide concentration tower 9 through the pipeline.
Example 2
Sulfur-free methanol from the medium-pressure flash sulfur-free methanol line 1, at a pressure of 1.7MPaA, a temperature of-32.8 ℃ and a flow rate of 2925kmol/H, had a composition (79.05% for methanol, H)2S is 0% and CO220.95 percent), the pressure is reduced to 0.6MpaA through a first reducing valve 2, the sulfur-free flash tank 3 carries out flash evaporation, carbon dioxide gas with the pressure of 0.6MPaA, the temperature of-37.7 ℃ and the flow rate of 76.2kmol/h is generated at the top, and the bottom liquid enters the top of an upper tower of a hydrogen sulfide concentration tower 9 after being reduced to 0.2MPaA through a second reducing valve 4;
sulfur-free methanol from the medium-pressure flashed sulfur-containing methanol line 5 at a pressure of 1.7MPaA, a temperature of-33.1 ℃ and a flow rate of 3179kmol/H, has a composition (methanol 77.68%, H)2S is 0.12% and CO222.20 percent), reducing the pressure to 0.6MpaA through a third pressure reducing valve 6, flashing by a sulfur-free flash tank 3, generating carbon dioxide gas with the pressure of 0.6MPaA at the top, the temperature of-39.4 ℃ and the flow rate of 107.6kmol/h, reducing the pressure of bottom liquid to 0.2MPaA through a fourth pressure reducing valve 8, entering the middle part of the upper tower of a hydrogen sulfide concentration tower 9, mixing with methanol flowing downwards from the tower top, flowing to the bottom of the upper section of the hydrogen sulfide concentration tower 9 from top to bottom, absorbing a small amount of hydrogen sulfide gas components contained in the gas flowing from bottom to top in the tower, finally extracting the methanol at the bottom of the upper section of the hydrogen sulfide concentration tower 9 by a methanol circulating pump 13, exchanging heat with the regenerated poor methanol in a second-stage methanol heat exchanger 14, increasing the temperature to-25.4 ℃, reducing the pressure to 0.6MPaA through a seventh pressure reducing valve 28, and leading CO dissolved in the methanol to be evaporated2Desorbing the gas, introducing into a circulating methanol flash tank 15, separating gas and liquid phases, wherein the pressure of the carbon dioxide gas at the top is 0.6MPaA, the temperature is-25.4 ℃,The flow rate was 481.9kmol/h, and the liquid phase at the bottom was returned to the top feed port of the lower column of the hydrogen sulfide concentrating column 9.
After the three obtained carbon dioxide gas streams are converged, the pressure is 0.6MPaA, the temperature is-28.6 ℃, and the flow is 665.7kmol/h, and then the three carbon dioxide gas streams are respectively sent to the expansion end inlet of the 1# carbon dioxide compression-expansion all-in-one machine 20 and the expansion end inlet of the 2# carbon dioxide compression-expansion all-in-one machine 21 through the gas collecting pipeline 26, the compression end inlet of the coaxial 1# carbon dioxide compression-expansion all-in-one machine 20 is driven to generate the low pressure of 0.04MPaA, and the compression end inlet of the 2# carbon dioxide compression-expansion all-in-one machine 20 generates the low pressure of 0.08 MPaA. The liquid phase discharged from the bottom of the hydrogen sulfide concentration tower 9 is decompressed to 0.04MPaA by a fifth decompression valve 24, enters a low-temperature vacuum flash tank 10, the carbon dioxide gas at the top enters a first-stage methanol heat exchanger 12 by a low-temperature booster pump 11, is heated to 40.8 ℃ by the poor methanol after thermal regeneration, is decompressed to 0.08MPaA by a sixth decompression valve 16, enters a normal-temperature vacuum flash tank 17, the carbon dioxide gas at the top has the pressure of 0.08MPaA, the temperature of 28.9 ℃ and the flow of 26.6kmol/h, and the liquid phase at the bottom enters a thermal regeneration tower 18 by a normal-temperature booster pump 25 for thermal regeneration.
The outlet gas at the compression end and the expansion end of the integrated carbon dioxide compression-expansion machine 1 20 and the outlet gas at the compression end and the expansion end of the integrated carbon dioxide compression-expansion machine 2 are all merged into a gas inlet pipeline 27 at the bottom of the upper tower of the hydrogen sulfide concentration tower 9 to be used as the bottom gas phase feed of the upper tower of the hydrogen sulfide concentration tower 9, the pressure of the carbon dioxide feed gas is 0.21MPaA, the temperature is-27.1 ℃, and the flow rate is 820.6 kmol/h. Finally, qualified carbon dioxide products are obtained from the top of the upper tower of the hydrogen sulfide concentration tower 9 through a carbon dioxide product pipeline 23, the molar concentration of the qualified carbon dioxide products is more than 99%, the yield of the qualified carbon dioxide products is 1314kmol/h, and the recovery rate of the qualified carbon dioxide products reaches 98.5%.
According to the efficient energy-saving regeneration device for recycling low-temperature methanol-washed carbon dioxide in a grading manner, vacuum generated by the carbon dioxide compression and expansion all-in-one machine is utilized for low-pressure flash evaporation regeneration to replace the traditional nitrogen gas stripping process, pressure potential energy in the pressure of the low-temperature methanol-washed carbon dioxide gas is utilized in a grading manner, the purposes of energy saving, consumption reduction and carbon dioxide yield increase are achieved, and a new optimized solution structure is provided for the technical field of low-temperature methanol-washed carbon dioxide recycling and greenhouse gas emission reduction devices.
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. Therefore, it is intended that the appended claims be interpreted as including preferred embodiments and all such alterations and modifications as fall within the scope of the utility model.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the utility model. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (6)
1. The high-efficiency energy-saving regeneration device for recycling low-temperature methanol to wash carbon dioxide in a grading manner is characterized by comprising a sulfur-free flash tank (3), a sulfur-containing flash tank (7), a hydrogen sulfide concentration tower (9), a low-temperature vacuum flash tank (10), a low-temperature booster pump (11), a first-stage methanol heat exchanger (12), a methanol circulating pump (13), a second-stage methanol heat exchanger (14), a circulating methanol flash tank (15), a normal-temperature vacuum flash tank (17), a heat regeneration tower (18), a poor methanol booster pump (19), a No. 1 carbon dioxide compression and expansion integrated machine (20), a No. 2 carbon dioxide compression and expansion integrated machine (21) and a normal-temperature booster pump (25);
a feed inlet pipeline of the sulfur-free flash tank (3) is connected with a sulfur-free methanol pipeline (1), a bottom liquid phase outlet pipeline is connected with a feed inlet at the top of an upper tower of the hydrogen sulfide concentration tower (9), and a top gas phase outlet is respectively connected with a gas collecting pipeline (26), an expansion end inlet of a No. 1 carbon dioxide compression and expansion integrated machine (20) and an expansion end inlet of a No. 2 carbon dioxide compression and expansion integrated machine (21) through pipelines;
a feed inlet pipeline of the sulfur-containing flash tank (7) is connected with a sulfur-containing methanol pipeline (5), a bottom liquid phase outlet pipeline is connected with a feed inlet in the middle of an upper tower of the hydrogen sulfide concentration tower (9), and a top gas phase outlet is respectively connected with a gas collection pipeline (26), an expansion end inlet of the 1# carbon dioxide compression-expansion all-in-one machine (20) and an expansion end inlet of the 2# carbon dioxide compression-expansion all-in-one machine (21) through pipelines;
a gas phase outlet at the top of an upper tower of the hydrogen sulfide concentration tower (9) is connected with a carbon dioxide product pipeline (23), a liquid phase outlet at the bottom of the upper tower is sequentially connected with the methanol circulating pump (13), the cold side of the second-stage methanol heat exchanger (14) and a feed inlet of the circulating methanol flash tank (15) through pipelines, a discharge outlet at the bottom of a lower tower is connected with the low-temperature vacuum flash tank (10) through a pipeline, and a feed inlet at the bottom of the lower tower is connected with the bottom of the circulating methanol flash tank (15) through a pipeline;
a top gas phase outlet of the circulating methanol flash tank (15) is sequentially connected with the gas collecting pipeline (26), an expansion end inlet of the 1# carbon dioxide compression-expansion all-in-one machine (20) and an expansion end inlet of the 2# carbon dioxide compression-expansion all-in-one machine (21);
a top gas phase outlet of the low-temperature vacuum flash tank (10) is connected with a compression end inlet of the 1# carbon dioxide compression and expansion all-in-one machine (20) through a pipeline, and a bottom liquid phase outlet is sequentially connected with a cold side inlet of the first-stage methanol heat exchanger (12) and the low-temperature booster pump (11) through pipelines;
the normal-temperature vacuum flash tank (17) is connected with a cold-side discharge port of the first-stage methanol heat exchanger (12) through a pipeline, a bottom liquid phase outlet is sequentially connected with feed ports of the normal-temperature booster pump (25) and the thermal regeneration tower (18) through pipelines, and a top gas phase outlet is connected with a compression end inlet of the 2# carbon dioxide compression-expansion all-in-one machine (21) through a pipeline;
a liquid phase outlet at the bottom of the thermal regeneration tower (18) is sequentially connected with the lean methanol booster pump (19), the hot side of the first-stage methanol heat exchanger (12), the hot side of the second-stage methanol heat exchanger (14) and the low-temperature lean methanol pipeline (22) through pipelines;
the compression end export and the expansion end export of 1# carbon dioxide compression expansion all-in-one (20) all loop through pipe connection admission line (27) with the last bottom gas feed inlet of hydrogen sulfide concentration tower (9), the compression end export and the expansion end export of 2# carbon dioxide compression expansion all-in-one (21) also all loop through pipe connection admission line (27) with the last bottom gas feed inlet of hydrogen sulfide concentration tower (9).
2. The high-efficiency energy-saving type regeneration device for recycling low-temperature methanol to wash carbon dioxide in a grading manner according to claim 1, wherein a first pressure reducing valve (2) is arranged on a connecting pipeline between a feed inlet of the sulfur-free flash tank (3) and the sulfur-free methanol pipeline (1), and a second pressure reducing valve (4) is arranged on a connecting pipeline between a liquid phase outlet at the bottom of the sulfur-free flash tank (3) and a feed inlet at the top of an upper tower of the hydrogen sulfide concentration tower (9).
3. The high-efficiency energy-saving type regeneration device for recycling low-temperature methanol to wash carbon dioxide in a grading manner according to claim 1, wherein a third pressure reducing valve (6) is arranged on a connecting pipeline between a feed inlet of the sulfur-containing flash tank (7) and the sulfur-containing methanol pipeline (5), and a fourth pressure reducing valve (8) is arranged on a connecting pipeline between a bottom liquid phase outlet of the sulfur-containing flash tank (7) and a feed inlet in the middle of an upper tower of the hydrogen sulfide concentration tower (9).
4. The high-efficiency energy-saving type regeneration device for recycling low-temperature methanol to wash carbon dioxide in grades as claimed in claim 1, wherein a fifth pressure reducing valve (24) is arranged on a connecting pipeline between a discharge port at the bottom of the lower tower of the hydrogen sulfide concentration tower (9) and the low-temperature vacuum flash tank (10).
5. The high-efficiency energy-saving regeneration device for recycling low-temperature methanol to wash carbon dioxide in stages according to claim 1, wherein a sixth pressure reducing valve (16) is arranged on a connecting pipeline between the normal-temperature vacuum flash tank (17) and a cold-side discharge port of the first-stage methanol heat exchanger (12).
6. The high-efficiency energy-saving regeneration device for recycling low-temperature methanol to wash carbon dioxide in stages according to claim 1, characterized in that a seventh reducing valve (28) is arranged on a connecting pipeline between the cold side of the second-stage methanol heat exchanger (14) and the feeding port of the circulating methanol flash tank (15).
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| CN114367171A (en) * | 2022-02-25 | 2022-04-19 | 华陆工程科技有限责任公司 | High-efficiency energy-saving regeneration device for recycling low-temperature methanol washing carbon dioxide in grading manner |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114367171A (en) * | 2022-02-25 | 2022-04-19 | 华陆工程科技有限责任公司 | High-efficiency energy-saving regeneration device for recycling low-temperature methanol washing carbon dioxide in grading manner |
| CN114367171B (en) * | 2022-02-25 | 2024-07-26 | 华陆工程科技有限责任公司 | High-efficiency energy-saving type regeneration device for grading recovery of low-temperature methanol washing carbon dioxide |
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