CN117346564A - Composite heat exchanger and carbon capture pressure increasing system thereof - Google Patents
Composite heat exchanger and carbon capture pressure increasing system thereof Download PDFInfo
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- CN117346564A CN117346564A CN202311656190.8A CN202311656190A CN117346564A CN 117346564 A CN117346564 A CN 117346564A CN 202311656190 A CN202311656190 A CN 202311656190A CN 117346564 A CN117346564 A CN 117346564A
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- exchange structure
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- 239000002131 composite material Substances 0.000 title claims abstract description 37
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 238000007789 sealing Methods 0.000 claims abstract description 10
- 238000009413 insulation Methods 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 31
- 238000003795 desorption Methods 0.000 claims description 25
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 22
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 13
- 239000003546 flue gas Substances 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 6
- 150000001875 compounds Chemical class 0.000 claims description 4
- 238000005192 partition Methods 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 238000005057 refrigeration Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000000034 method Methods 0.000 description 13
- 239000007789 gas Substances 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- 230000006837 decompression Effects 0.000 description 4
- IOLCXVTUBQKXJR-UHFFFAOYSA-M potassium bromide Chemical compound [K+].[Br-] IOLCXVTUBQKXJR-UHFFFAOYSA-M 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000004568 cement Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
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- Gas Separation By Absorption (AREA)
Abstract
The invention belongs to the technical field of carbon capture, and particularly relates to a composite heat exchanger and a carbon capture pressure increasing system thereof, wherein the composite heat exchanger consists of a fixed tube plate type heat exchange structure, a spiral plate type sleeve heat exchange structure and a support plate for connecting the fixed tube plate type heat exchange structure and the spiral plate type sleeve heat exchange structure; the fixed tube-sheet type heat exchange structure comprises a sealing plate with an enclosure structure, four tube-sheet type heat exchanger cylinders which are uniformly distributed are arranged in the sealing plate, and heat insulation plates are arranged between the adjacent tube-sheet type heat exchanger cylinders; the spiral plate type sleeve heat exchange structure comprises an outer pipe and an inner pipe sleeved inside the outer pipe. According to the invention, the lean-rich liquid heat exchanger, the gas cooler, the lean liquid precooler and the condenser are integrated into a composite heat exchanger, and the heat and pressure energy contained in the carbon capture pressure increasing system are recycled, so that the utilization rate of energy in the unit can be improved, the energy consumption of the unit is reduced, and the COP of the unit is improved.
Description
Technical Field
The invention belongs to the technical field of carbon capture, and particularly relates to a composite heat exchanger and a carbon capture pressure increasing system thereof.
Background
At present, the carbon capturing and pressurizing system shown in fig. 1 can be used for capturing and recovering CO in mixed gases such as chemical tail gas, power plant gas tail gas, cement roasting flue gas and the like 2 And can be directly used for CO 2 And (5) lifting and pressing. Carbon capture and CO in the industrial fields of chemical industry, cement, steel, natural gas, coal electricity and the like 2 The equipment investment and the operation cost can be obviously reduced in the hot pressure lifting process, and the method has high economic value and social value.
However, there is room for many process optimizations and equipment integration in the above carbon capture pressure boost system process. For example, heat contained in low-pressure flue gas is not utilized before entering the fan, and the compression and pressure boosting of high-temperature flue gas increase the power consumption of the fan; the low-pressure steam passes through a temperature and pressure reducing device before entering the reboiler, and part of heat energy is not utilized; CO desorbed from the top of the desorption column 2 The mixture of the water vapor and the heat energy is at a higher temperature, and part of the heat energy is not utilized and directly enters the condenser, so that the cold energy required by condensation is larger; in the prior art, the rich liquid only passes through a lean-rich liquid heat exchanger to recover heat contained in the lean liquid flowing out of the bottom of the desorption tower before the rich liquid is sent to the desorption tower. The lean solution flowing out of the desorption tower is throttled and decompressed by a decompression valve and then enters the absorption tower, so that the entropy of the high-pressure lean solution is increased due to throttling and decompression, the work capacity is reduced, and part of high-pressure energy is not utilized.
In addition, low-pressure flue gas and lean solution before entering the absorption tower in the prior art system and CO desorbed from the top of the desorption tower 2 The mixture of the water vapor and the gas precooler, the lean solution precooler and the condenser are required to be cooled and condensed respectively, the part of cooling and condensing is required to take away heat through circulating water in public engineering, and the heat taken away by the part of circulating water is required to release the heat to the atmosphere through a subsequent air cooling tower, so that the power consumption of the air cooling tower is increased. In summer, the temperature of the circulating water is high, so that the low-pressure flue gas before entering the absorption tower is difficult to ensure,Lean liquid and CO desorbed from the top of the desorption column 2 The mixture with water vapor is cooled and condensed to the temperature required by the process, and the optimal running state of the process system cannot be ensured.
Therefore, we propose a composite heat exchanger and a carbon capture pressure increasing system thereof to solve the above problems.
Disclosure of Invention
In order to solve the problems, a composite heat exchanger and a carbon capture pressure increasing system thereof are provided.
The above object is achieved by the following preparation process:
a compound heat exchanger consists of a fixed tube plate type heat exchange structure, a spiral plate type sleeve heat exchange structure positioned above the fixed tube plate type heat exchange structure and two groups of support plates for connecting the fixed tube plate type heat exchange structure and the spiral plate type sleeve heat exchange structure;
the fixed tube-sheet type heat exchange structure comprises a sealing plate with an enclosure structure, four tube-sheet type heat exchanger cylinders which are uniformly distributed are arranged in the sealing plate, heat insulation plates are arranged between the adjacent tube-sheet type heat exchanger cylinders, the upper end and the lower end of each tube-sheet type heat exchanger cylinder are respectively provided with a seal head tube box, and the four tube-sheet type heat exchanger cylinders are sequentially connected with the upper end and the lower end of each seal head tube box through pipelines to form a series structure;
the spiral plate type double-pipe heat exchange structure comprises an outer pipe and an inner pipe sleeved inside the outer pipe, four areas are divided between the outer pipe and the inner pipe by three partition boards, an outer spiral plate is arranged on the outer side of the inner pipe in each area, an inner spiral plate is arranged inside the inner pipe, and material flows of shell passes of the tube plate type heat exchanger respectively enter the four areas of the outer pipe after being discharged and form countercurrent with the material flows flowing inside the inner pipe.
As a further improvement of the above technical scheme: the tube plate type heat exchanger is characterized in that a plurality of vertical heat exchange tubes are arranged inside the tube plate type heat exchanger cylinder body, and the heat exchange tubes are communicated with an upper end socket tube box and a lower end socket tube box.
As a further improvement of the above technical scheme: the tube-plate type heat exchanger cylinder is internally provided with transverse baffle plates which are used for fixing the heat exchange tubes and are staggered with each other.
As a further improvement of the above technical scheme: and the two ends of the outer tube are provided with end closure plates.
As a further improvement of the above technical scheme: four heat flows respectively flow through the shell side of the four tube plate type heat exchanger cylinders, the tube side of the four tube plate type heat exchanger cylinders sequentially flow into rich liquid before the desorber, the four heat flows are discharged from the shell side of the tube plate type heat exchanger cylinders and then enter four areas of the outer tube, cold water flows through the inner tube, and countercurrent is formed between the cold water and the heat flows flowing through the four areas of the outer tube.
The carbon capturing and pressurizing system comprises a fan, an absorption tower, a solution pump, a desorption tower, a reboiler, a gas-liquid separation tank, a lithium bromide refrigerator, a solution turbine and the composite heat exchanger;
containing CO 2 The low-pressure flue gas serving as H4 enters the composite heat exchanger, enters the absorption tower through the fan and is absorbed by lean liquid to form rich liquid;
the rich liquid enters a desorption tower to be desorbed after passing through a solution pump and a compound heat exchanger, and CO coming out of the tower top 2 The mixture of the hydrogen and the water vapor is used as H3, lean solution flowing out from the bottom of the tower is used as H2, the H3 enters a gas-liquid separation tank after passing through a composite heat exchanger, and the H2 enters an absorption tower after passing through a solution turbine;
the low-pressure steam enters a reboiler through a part of the lithium bromide refrigerator, condensate discharged from the reboiler is used as H1 and is discharged after passing through the composite heat exchanger, and the other part of the condensate is used as cold water, after heat absorption is completed by passing through the composite heat exchanger, the condensate returns to the lithium bromide refrigerator for re-refrigeration circulation flow;
wherein the temperature of H1-H4 is H4> H3> H2> H1.
As a further improvement of the above technical scheme: the solution turbine is driven by H2 to provide power for the fan.
The invention has the beneficial effects that:
(1) Low pressure flue gas, CO desorbed from the top of the desorption column 2 With water vapourThe heat contained in the condensate liquid flowing out of the bottom of the desorption tower and the lean liquid and the reboiler is used for preheating the rich liquid before entering the desorption tower. The heat required by desorption in the desorption tower can be reduced, and the energy consumption of the desorption tower is reduced.
(2) The heat originally wasted in the temperature and pressure reducing device by the low-pressure steam is utilized to drive the potassium bromide refrigerator, and cold water is prepared to replace circulating water so as to meet the cooling and condensing requirements in the process system. The method ensures that the process system is in an optimal operation state in summer, recovers and utilizes the heat originally wasted in the temperature and pressure reduction device by low-pressure steam, replaces circulating water, and reduces the energy consumption of public programs.
(3) The lean solution flowing out of the desorption tower is throttled and decompressed by an original decompression valve to be changed into a solution turbine to drive a fan to rotate, so that the low-pressure flue gas is pressurized.
(4) The composite heat exchanger integrates the lean-rich liquid heat exchanger, the gas cooler, the lean liquid precooler and the condenser into one device. The cost of equipment and pipelines can be reduced, and the occupied area of the unit is greatly reduced.
Drawings
FIG. 1 is a schematic diagram of an overall flow of a prior art carbon capture pressure boost system;
FIG. 2 is a front view of the overall simplified structure of the composite heat exchanger of the present invention;
FIG. 3 is a schematic side view of the structure of the composite heat exchanger of the present invention;
FIG. 4 is a schematic view showing a partial structure of a unified heat exchanger according to the present invention;
FIG. 5 is a schematic diagram of the overall flow of the carbon capture pressure increasing system of the present invention.
The diagram is: 1. fixing a tube plate type heat exchange structure; 11. a sealing plate; 12. tube plate type heat exchanger cylinder; 13. a heat insulating plate; 14. a heat exchange tube; 15. a seal head pipe box; 16. a baffle plate; 2. a spiral plate type sleeve heat exchange structure; 21. an outer tube; 22. an inner tube; 23. an outer spiral plate; 24. an inner spiral plate; 25. a partition plate; 26. a closure plate; 3. and a support plate.
Detailed Description
The following detailed description of the present application is provided in conjunction with the accompanying drawings, and it is to be understood that the following detailed description is merely illustrative of the application and is not to be construed as limiting the scope of the application, since numerous insubstantial modifications and adaptations of the application will be to those skilled in the art in light of the foregoing disclosure.
Example 1
As shown in fig. 2 to 4, the composite heat exchanger of the present embodiment is composed of an upper portion, which is a spiral plate type double pipe heat exchange structure 2, and a lower portion, which is a fixed pipe plate type heat exchange structure 1, which is fixed to the lower portion by a support plate 3.
The fixed tube-sheet type heat exchange structure 1 comprises a sealing plate 11 with an enclosure structure, four tube-sheet type heat exchanger barrels 12 which are uniformly distributed are arranged inside the sealing plate 11, heat insulation plates 13 are arranged between the adjacent tube-sheet type heat exchanger barrels 12, head tube boxes 15 are arranged at the upper end and the lower end of each tube-sheet type heat exchanger barrel 12, a plurality of vertical heat exchange tubes 14 are arranged inside the tube-sheet type heat exchanger barrels 12, the heat exchange tubes 14 are communicated with the head tube boxes 15 at the upper end and the lower end, and transverse baffle plates 16 which are used for fixing the heat exchange tubes 14 and are staggered with each other are further arranged inside the tube-sheet type heat exchanger barrels 12.
The four tube sheet type heat exchanger cylinders 12 are sequentially connected with the upper end head tube box 15 and the lower end head tube box 15 through pipelines to form a series structure, and from the view of fig. 2, the structure is specifically as follows: the upper end seal head tube box 15 of the first tube plate type heat exchanger cylinder 12 is connected with the upper end seal head tube box 15 of the adjacent second tube plate type heat exchanger cylinder 12 through a pipeline, the lower end seal head tube box 15 of the second tube plate type heat exchanger cylinder 12 is connected with the lower end seal head tube box 15 of the adjacent third tube plate type heat exchanger cylinder 12 through a pipeline, the upper end seal head tube box 15 of the third tube plate type heat exchanger cylinder 12 is connected with the upper end seal head tube box 15 of the adjacent fourth tube plate type heat exchanger cylinder 12 through a pipeline, the heat exchange tubes 14 are communicated between the upper end seal head tube box 15 and the lower end seal head tube box 15 of each tube plate type heat exchanger cylinder 12, namely, the heat exchange tubes 14 tube passes of the four tube plate type heat exchanger cylinders 12 are communicated, so that tube passes (in the heat exchange tubes 14) are formed between the four tube plate type heat exchanger cylinders 12 in series, and the tube passes are used for cooling material flowRich liquid (before entering the desorber); the shell side of the four tube-sheet heat exchanger cylinder 12 (outside the heat exchange tube 14) is respectively provided with four hot streams (low-pressure flue gas, CO desorbed from the top of the desorption tower) 2 The mixture with water vapor, lean liquid flowing out from the bottom of the desorption tower and condensate flowing out from the reboiler), and the four hot streams respectively enter the spiral plate type double-pipe heat exchange structure 2 and flow out, so that shell passes are connected in parallel between the four tube plate type heat exchanger cylinders 12.
The spiral plate type double-pipe heat exchange structure 2 comprises an outer pipe 21 and an inner pipe 22 sleeved in the outer pipe 21, sealing plates 26 are arranged at two ends of the outer pipe 21, the outer pipe 21 and the inner pipe 22 are divided into four areas by three partition plates 25, an outer spiral plate 23 is arranged on the outer side of the inner pipe 22 in each area, an inner spiral plate 24 is arranged in the inner pipe 22, and material flows of the shell passes of each tube plate type heat exchanger cylinder 12 respectively enter the four areas of the outer pipe 21 after being discharged and form countercurrent with material flows (cold water) flowing in the inner pipe 22.
The outer tube 21 carries hot streams (H1-H4) with adjacent hot streams separated by a separator 25. The temperature in the hot material flow is H1, H2, H3 and H4 from low to high in sequence, and H1-H4 exchanges heat with cold water in sequence, so that pure countercurrent high-efficiency heat exchange is formed, and simultaneously, the hot material flow and the cold water form spiral flow under the guidance of the inner spiral plate and the outer spiral plate, and the directions of the spiral flow are opposite, so that the heat exchange efficiency is higher. All the parts are connected through corresponding pipelines, and the material flows (rich liquid, hot material flows H1-H4 and cold water) flow in the pipeline. Finally, the hot material flows (H1-H4) and the rich liquid pass through the composite heat exchanger to exchange heat, and then return to the respective technological processes.
The composite heat exchanger integrates the lean-rich liquid heat exchanger, the gas cooler, the lean liquid precooler and the condenser into one device. The cost of equipment and pipelines is greatly reduced, and the occupied area of the unit is reduced.
As shown in fig. 5, the carbon capturing and pressurizing system of the embodiment comprises a fan, an absorption tower, a solution pump, a desorption tower, a reboiler, a gas-liquid separation tank, a lithium bromide refrigerator, a solution turbine and a composite heat exchanger;
containing CO 2 The low-pressure flue gas serving as H4 enters the composite heat exchanger, enters the absorption tower through the fan and is absorbed by lean liquid to form rich liquid;
the rich liquid enters a desorption tower to be desorbed after passing through a solution pump and a compound heat exchanger, and CO coming out of the tower top 2 The mixture of the hydrogen and the water vapor is used as H3, lean solution flowing out from the bottom of the tower is used as H2, the H3 enters a gas-liquid separation tank after passing through a composite heat exchanger, and the H2 enters an absorption tower after passing through a solution turbine after passing through the composite heat exchanger;
the low-pressure steam enters a reboiler after passing through the lithium bromide refrigerator, condensate discharged from the reboiler is used as H1 and is discharged after passing through the composite heat exchanger, and the other part of the condensate is used as cold water, and after heat absorption is completed after passing through the composite heat exchanger, the condensate returns to the lithium bromide refrigerator for re-refrigeration circulation flow.
The lower part of the composite heat exchanger is used for separating hot material flows H1-H4 (low-pressure flue gas and CO desorbed from the top of the desorption tower) 2 A mixture with water vapor, a lean liquid flowing out from the bottom of the desorption tower, and a condensate coming out from the reboiler) for preheating the rich liquid before entering the desorption tower. After the heat contained in the hot material flows H1-H4 is recycled, the heat is further cooled and condensed to the temperature required by the process through the upper part by cold water from a lithium bromide refrigerator. Cold water flowing from the lithium bromide refrigerator is produced by low pressure steam driving.
In addition, the lean solution H2 flowing out of the desorption tower is throttled and decompressed by the original decompression valve to be changed into a solution turbine to drive the fan to rotate, so that the low-pressure flue gas is pressurized.
The heat and pressure energy contained in the process system can be recycled, the utilization rate of energy in the unit can be improved, the energy consumption of the unit can be reduced, and the COP of the unit can be improved. The heat originally wasted in the temperature and pressure reducing device by the low-pressure steam is utilized to drive the potassium bromide refrigerator, and cold water is prepared to replace circulating water so as to meet the cooling and condensing requirements in the process system. The method ensures that the process system is in an optimal operation state in summer, recovers and utilizes the heat originally wasted in the temperature and pressure reduction device by low-pressure steam, replaces circulating water, and reduces the energy consumption of public programs.
The foregoing examples illustrate only a few embodiments of the invention and are described in detail herein without thereby limiting the scope of the invention. It should be noted that it will be apparent to those skilled in the art that modifications can be made without departing from the spirit of the invention, which are within the scope of the invention.
Claims (7)
1. The composite heat exchanger is characterized by comprising a fixed tube-plate heat exchange structure (1), a spiral plate type sleeve heat exchange structure (2) positioned above the fixed tube-plate heat exchange structure (1) and two groups of support plates (3) for connecting the fixed tube-plate heat exchange structure (1) and the spiral plate type sleeve heat exchange structure (2);
the fixed tube-sheet type heat exchange structure (1) comprises a sealing plate (11) with an enclosure structure, four tube-sheet type heat exchanger cylinders (12) which are uniformly distributed are arranged in the sealing plate (11), heat insulation plates (13) are arranged between the adjacent tube-sheet type heat exchanger cylinders (12), seal head tube boxes (15) are arranged at the upper end and the lower end of each tube-sheet type heat exchanger cylinder (12), and the four tube-sheet type heat exchanger cylinders (12) are sequentially connected with the upper end seal head tube boxes (15) and the lower end seal head tube boxes (15) through pipelines to form a series structure;
the spiral plate type double-pipe heat exchange structure (2) comprises an outer pipe (21) and an inner pipe (22) sleeved inside the outer pipe (21), four areas are separated between the outer pipe (21) and the inner pipe (22) by three partition boards (25), an outer spiral plate (23) is arranged on the outer side of the inner pipe (22) in each area, an inner spiral plate (24) is arranged inside the inner pipe (22), and each material flow of a shell side of the tube plate type heat exchanger cylinder (12) enters the four areas of the outer pipe (21) after being discharged respectively, and forms countercurrent with the material flow flowing inside the inner pipe (22).
2. The composite heat exchanger according to claim 1, wherein a plurality of vertical heat exchange tubes (14) are arranged inside the tube plate type heat exchanger cylinder (12), and the heat exchange tubes (14) are communicated with upper and lower head tube boxes (15).
3. A composite heat exchanger according to claim 2, wherein the tube-sheet heat exchanger cylinder (12) is further internally provided with transverse baffles (16) for securing the heat exchange tubes (14) and being staggered with respect to each other.
4. A composite heat exchanger according to claim 1, wherein the outer tube (21) is provided with end plates (26) at both ends.
5. The composite heat exchanger according to claim 1, wherein the shell passes of the four tube sheet heat exchanger cylinders (12) respectively flow four hot streams, and the tube passes of the four tube sheet heat exchanger cylinders (12) sequentially flow rich liquid before entering the desorber, the four hot streams enter four areas of the outer tube (21) after being discharged from the shell passes of the tube sheet heat exchanger cylinders (12), the inner tube (22) flows cold water, and the cold water and the hot streams flowing in the four areas of the outer tube (21) form countercurrent flow.
6. A carbon capturing and pressurizing system, which comprises a fan, an absorption tower, a solution pump, a desorption tower, a reboiler, a gas-liquid separation tank and a lithium bromide refrigerator, and is characterized by also comprising a solution turbine and the composite heat exchanger of claim 5;
containing CO 2 The low-pressure flue gas serving as H4 enters the composite heat exchanger, enters the absorption tower through the fan and is absorbed by lean liquid to form rich liquid;
the rich liquid enters a desorption tower to be desorbed after passing through a solution pump and a compound heat exchanger, and CO coming out of the tower top 2 The mixture of the hydrogen and the water vapor is used as H3, lean solution flowing out from the bottom of the tower is used as H2, the H3 enters a gas-liquid separation tank after passing through a composite heat exchanger, and the H2 enters an absorption tower after passing through a solution turbine after passing through the composite heat exchanger；
The low-pressure steam enters a reboiler through a part of the lithium bromide refrigerator, condensate discharged from the reboiler is used as H1 and is discharged after passing through the composite heat exchanger, and the other part of the condensate is used as cold water, after heat absorption is completed by passing through the composite heat exchanger, the condensate returns to the lithium bromide refrigerator for re-refrigeration circulation flow;
wherein the temperature of H1-H4 is H4> H3> H2> H1.
7. The carbon capture boost system of claim 6, wherein the solution turbine is driven by H2 to power a blower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311656190.8A CN117346564B (en) | 2023-12-05 | 2023-12-05 | Composite heat exchanger and carbon capture pressure increasing system thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202311656190.8A CN117346564B (en) | 2023-12-05 | 2023-12-05 | Composite heat exchanger and carbon capture pressure increasing system thereof |
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| CN117346564B CN117346564B (en) | 2024-02-23 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0066096A2 (en) * | 1981-05-29 | 1982-12-08 | Krupp Koppers GmbH | Process for the simultaneous heat treatment of several coal streams |
| JP2005147480A (en) * | 2003-11-13 | 2005-06-09 | Toyo Radiator Co Ltd | Multi-fluid heat exchanger |
| CN201844718U (en) * | 2010-10-11 | 2011-05-25 | 北京广厦环能科技有限公司 | Combined heat exchanger of corrugated pipe |
| CN202329301U (en) * | 2011-05-30 | 2012-07-11 | 中国石油化工集团公司 | Fixed tube sheet heat exchanger combined with heat exchange unit modules |
| CN103925814A (en) * | 2014-04-24 | 2014-07-16 | 南京国昌化工科技有限公司 | Combined heat exchange system |
| CN104167956A (en) * | 2013-05-17 | 2014-11-26 | 宝山钢铁股份有限公司 | Flue gas waste heat thermoelectric recovery device |
| CN107255422A (en) * | 2017-07-31 | 2017-10-17 | 郑州大学 | Shell side multiple flow wound tube heat exchanger |
| CN207247399U (en) * | 2017-05-10 | 2018-04-17 | 袁一军 | A kind of heat transmission equipment and asymmetric heat transfer system |
| CN115523774A (en) * | 2022-09-30 | 2022-12-27 | 镇海石化建安工程股份有限公司 | Heat recovery system for heat high-pressure gas in hydrogenation device |
-
2023
- 2023-12-05 CN CN202311656190.8A patent/CN117346564B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0066096A2 (en) * | 1981-05-29 | 1982-12-08 | Krupp Koppers GmbH | Process for the simultaneous heat treatment of several coal streams |
| JP2005147480A (en) * | 2003-11-13 | 2005-06-09 | Toyo Radiator Co Ltd | Multi-fluid heat exchanger |
| CN201844718U (en) * | 2010-10-11 | 2011-05-25 | 北京广厦环能科技有限公司 | Combined heat exchanger of corrugated pipe |
| CN202329301U (en) * | 2011-05-30 | 2012-07-11 | 中国石油化工集团公司 | Fixed tube sheet heat exchanger combined with heat exchange unit modules |
| CN104167956A (en) * | 2013-05-17 | 2014-11-26 | 宝山钢铁股份有限公司 | Flue gas waste heat thermoelectric recovery device |
| CN103925814A (en) * | 2014-04-24 | 2014-07-16 | 南京国昌化工科技有限公司 | Combined heat exchange system |
| CN207247399U (en) * | 2017-05-10 | 2018-04-17 | 袁一军 | A kind of heat transmission equipment and asymmetric heat transfer system |
| CN107255422A (en) * | 2017-07-31 | 2017-10-17 | 郑州大学 | Shell side multiple flow wound tube heat exchanger |
| CN115523774A (en) * | 2022-09-30 | 2022-12-27 | 镇海石化建安工程股份有限公司 | Heat recovery system for heat high-pressure gas in hydrogenation device |
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| CN117346564B (en) | 2024-02-23 |
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