CN203803335U - Multistage split regeneration carbon dioxide trapping system - Google Patents

Multistage split regeneration carbon dioxide trapping system Download PDF

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Publication number
CN203803335U
CN203803335U CN201420212954.4U CN201420212954U CN203803335U CN 203803335 U CN203803335 U CN 203803335U CN 201420212954 U CN201420212954 U CN 201420212954U CN 203803335 U CN203803335 U CN 203803335U
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China
Prior art keywords
communicated
rich solution
pregnant solution
regeneration
rich
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CN201420212954.4U
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Chinese (zh)
Inventor
牛红伟
郜时旺
刘练波
王金意
郭东方
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中国华能集团清洁能源技术研究院有限公司
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Priority to CN201420212954.4U priority Critical patent/CN203803335U/en
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Abstract

The utility model discloses a multistage split regeneration carbon dioxide trapping system which comprises an absorption tower, wherein a pregnant solution discharged from the absorption tower is divided into two parts, a first pipeline for the pregnant solution is communicated with an upper pregnant solution inlet of a regeneration tower, a second part for the pregnant solution is communicated with a pregnant solution inlet of a barren /pregnant solution heat exchanger; pregnant solution discharged from the barren/pregnant solution heat exchanger is divided into two parts, one part of pregnant solution is communicated with a middle pregnant solution inlet of the regeneration tower and the other part of pregnant solution is communicated with a pregnant solution inlet of the pregnant solution reheater; a pregnant solution outlet of the pregnant solution reheater is communicated with a pregnant solution inlet of a pregnant solution flash tank, and a pregnant solution outlet in the bottom of the pregnant solution flask tank is communicated with a lower pregnant solution inlet of the regeneration solution. According to the multistage split regeneration carbon dioxide trapping system, heat consumption of steam required by pregnant solution regeneration can be reduced when the regeneration degree of the pregnant solution is improved, and a steam condensate is recycled to a dewatering collecting box of main equipment, so that the consumption of demineralized water of the trapping system is reduced.

Description

A kind of carbon dioxide capture system of multi-stage diffluence regeneration
Technical field
The utility model belongs to flue gases purification field, is particularly useful for low concentration CO in flue gas that coal-burning boiler, gas turbine and Industrial Stoves etc. produce 2trapping, the particularly carbon dioxide capture system of a kind of multi-stage diffluence regeneration.
Background technology
Electric power, chemical industry need to consume a large amount of fossil feedstock such as coal, natural gas, and its use can bring with CO 2be main greenhouse gas emission, the climate change problem causing has thus become the focus that the whole world is paid close attention to.
Ripe in chemical industry taking alkaline alcohol amine lyosoption as main smoke carbon dioxide capture recovery process, similarly technology is also launched demonstration in power industry, but to have flow large for the flue gas producing due to power industry, the features such as content is low, in solution, the regeneration of carbon dioxide need to consume a large amount of steam, cause system energy consumption large, reason is, for existing collecting carbonic anhydride technology, carbon dioxide is in the process of regeneration, because regeneration is not thorough, desorb degree is lower, in solution, approximately there is 1/3rd carbon dioxide discharged and reenter absorber portion, cause solution absorbability deficiency, ensure identical trapping output, solution circulation flow certainly will will be increased, cause that regeneration steam consumption causes circulating pump merit to increase when increase, meanwhile, in prior art, steam is through heat exchanger to for once heat release of solution, and Btu utilization is insufficient, is also one of reason that system energy consumption is higher.
Summary of the invention
In order to overcome the shortcoming of above-mentioned prior art, the purpose of this utility model is to provide a kind of carbon dioxide capture system of multi-stage diffluence regeneration, be applicable to the trapping of low fractional pressure carbon dioxide in chemical industry, power industry generation flue gas, optimized the chemical absorption method technique of the collecting carbonic anhydride of current use, have steam heat utilization fully, the high and energy of regeneration of waste liquor degree consumes the features such as low.
To achieve these goals, the technical solution adopted in the utility model is:
A kind of carbon dioxide capture system of multi-stage diffluence regeneration, comprise absorption tower 1, the rich solution that goes out absorption tower 1 is divided into two-way, be communicated with the first pipeline 2 of the first control valve 3 and the top rich solution entrance 4 of regenerator 8, the second pipeline 5 is communicated with the rich solution entrance of poor rich liquid heat exchanger 6, the rich solution that goes out poor rich liquid heat exchanger 6 is also divided into two-way, one tunnel is established the second control valve 7 and is communicated with the middle part rich solution entrance 9 of regenerator 8, another road is established the 3rd control valve 10 and is communicated with the rich solution entrance of rich solution reheater 11, the rich solution outlet of rich solution reheater 11 is communicated with the rich solution entrance of rich solution flash tank 12, the rich solution outlet of described rich solution flash tank 12 bottoms and the bottom rich solution entrance 13 of regenerator 8 are communicated with, after the gas vent at rich solution flash tank 12 tops and the top gas export pipeline of regenerator 8 are communicated with and the gas access of regeneration gas cooler 14 is communicated with, the gas access of the gas vent of regeneration gas cooler 14 and regeneration gas separator 15 is communicated with, the bottom discharge channel of regeneration gas separator 15 and the second pipeline 5 are communicated with, the regeneration gas export pipeline at regeneration gas separator 15 tops is communicated with subsequent compression liquefaction workshop section.
Described regenerator 8 bottoms are provided with reboiler 16, low-pressure steam from pipe network is communicated with the steam inlet of reboiler 16, cooling vapour/the liquid of the steam entrance of the outlet of reboiler 16 and rich solution reheater 11 is communicated with, and the steam cooling liquid outlet pipeline of rich solution reheater 11 and the drains collecting tank 17 of main equipment are communicated with.
The lean solution outlet of described regenerator 8 bottoms and the lean solution entrance pipe of poor rich liquid heat exchanger 6 are communicated with, and the lean solution outlet of poor rich liquid heat exchanger 6 is communicated with the lean solution entrance on absorption tower 1.
The collecting carbonic anhydride technique of a kind of multi-stage diffluence regeneration of the utility model, divide three branch roads by the rich solution that goes out absorption tower 1, first control valve 3 of leading up to enters from the top of regenerator 8, this part rich solution temperature is relatively low, its flow-control is 5%~10% of rich solution total flow, an other road enters from the middle part of regenerator 8 by the second control valve 7 after poor rich liquid heat exchanger 6 heating, this part rich solution temperature is relatively high, its flow-control is 70%~80% of rich solution total flow, remain a road and carry out adjust flux by the 3rd control valve 10 after poor rich liquid heat exchanger 6 heating, and then after rich solution reheater 11 heating, enter 12 flash distillations of rich solution flash tank and resolve part carbon dioxide gas, rich solution flash tank 12 bottoms rich solution out enters from regenerator 8 bottoms, this part rich solution temperature is the highest, its flow-control is 15%~20% of rich solution total flow.
Gas out of rich solution flash tank 12 tops and regenerator 8 tops gas are out converged and sends into regeneration gas separator 15 after cooling by regeneration gas cooler 14 and carry out gas-liquid separation, regeneration gas separator 15 bottoms parting liquid is out sent into the rich solution entrance of poor rich liquid heat exchanger 6, and regeneration gas separator 15 tops regeneration gas is out sent into subsequent compression liquefaction workshop section.
Utilize and enter reboiler 16 from the low-pressure steam of pipe network, cooling vapour/liquid after release heat again discharges by rich solution reheater 11 drains collecting tank 17 that the condensate liquid forming after waste heat enters main equipment and reclaims, and regenerator 8 bottoms lean solution out enters absorption tower 1 through poor rich liquid heat exchanger 6.
Compared with prior art, the rich solution of absorption tower outlet is divided into three tunnels by the utility model, wherein a road directly enters from the tip position of regenerator without poor rich liquid heat exchanger heating, this part rich solution temperature is lower can utilize its waste heat to resolve partial CO 2 in cooling to the regeneration gas at regenerator top, this road rich solution substitutes the colder regeneration gas parting liquid of former prior device, and the latter is sent to the rich solution pipeline before heat exchange, to reduce unnecessary heat of evaporation loss; Heat through rich solution reheater after poor rich liquid heat exchanger heating on an other road again, fully absorb, enter rich solution flash tank after utilizing the waste heat from the steam of reboiler cooling (vapour) liquid, enter from regenerator bottom after utilizing the heat flash distillation of twice recovery to resolve part carbon dioxide gas; Remain a road enters from regenerator middle part after poor rich liquid heat exchanger heating; Then, by being set, control valve reasonable distribution enters the rich solution flow on each branch line of regenerator, thereby thermograde in optimization regenerator, realize carbon dioxide in rich solution utilizes waste heat repeatedly parsing at diverse location, and by more thorough that rich solution reheater makes that steam heat utilizes is set, finally in improving rich solution regeneration degree, realize the regenerate reduction of required steam hear rate of rich solution.
The utility model is also recycled to steam condensate the drains collecting tank of main equipment, thereby reduces the demineralized water consumption of trapping system.
Brief description of the drawings
Fig. 1 is the utility model system architecture schematic diagram.
Detailed description of the invention
Describe embodiment of the present utility model in detail below in conjunction with drawings and Examples.
As shown in Figure 1, the collecting carbonic anhydride treatment system of a kind of multi-stage diffluence regeneration of the utility model, comprise absorption tower 1, absorption tower 1 rich solution is out divided into two-way, the first pipeline 2 is established the first control valve 3, and be communicated with the top rich solution entrance 4 of regenerator 8, the rich solution entrance pipe of the second pipeline 5 and poor rich liquid heat exchanger 6 is communicated with, the outlet rich solution of poor rich liquid heat exchanger 6 is divided into again two-way, one tunnel is established the second control valve 7 and is communicated with the middle part rich solution entrance 9 of regenerator 8, another road is established the 3rd control valve 10 and is communicated with the rich solution entrance pipe of rich solution reheater 11, the rich solution outlet of rich solution reheater 11 and the rich solution entrance pipe of rich solution flash tank 12 are communicated with.
The rich solution outlet of rich solution flash tank 12 bottoms and the bottom rich solution entrance 13 of regenerator 8 are communicated with, after the gas vent at rich solution flash tank 12 tops and the top gas export pipeline of regenerator 8 are communicated with and the gas access of regeneration gas cooler 14 is communicated with, the gas access of the gas vent of regeneration gas cooler 14 and regeneration gas separator 15 is communicated with, the bottom discharge channel of regeneration gas separator 15 and the second pipeline 5 are communicated with, and the regeneration gas export pipeline at regeneration gas separator 15 tops is communicated with subsequent compression liquefaction workshop section.
Regenerator 8 bottoms are provided with reboiler 16, low-pressure steam from pipe network is communicated with the steam inlet of reboiler 16, cooling vapour/the liquid of the steam entrance of the outlet of reboiler 16 and rich solution reheater 11 is communicated with, and the steam cooling liquid outlet pipeline of rich solution reheater 11 and the drains collecting tank 17 of main equipment are communicated with.
The lean solution outlet of regenerator 8 bottoms and the lean solution entrance pipe of poor rich liquid heat exchanger 6 are communicated with, and the lean solution outlet of poor rich liquid heat exchanger 6 is communicated with the lean solution entrance on absorption tower 1.
Technical process of the present utility model and principle are:
Absorption tower 1 rich solution out finally point three branch roads enters regenerator 8, and first control valve 3 of leading up to enters from the top of regenerator 8, and this part rich solution temperature is lower, and its flow is adjusted to 5%~10% of rich solution total flow by the first control valve 3; An other road enters from the middle part of regenerator by the second control valve 7 after poor rich liquid heat exchanger 6 heating, and this part rich solution temperature is higher, and its flow is adjusted to 70%~80% of rich solution total flow by the second control valve 7; Remaining a road, after poor rich liquid heat exchanger 6 heating, to regulate this part rich solution flow by the 3rd control valve 10 be 15%~20% of rich solution total flow, and then after rich solution reheater 11 heating, enter 12 flash distillations of rich solution flash tank and resolve part carbon dioxide gas, rich solution flash tank 12 bottoms rich solution out enters from regenerator 8 bottoms, and this part rich solution temperature is the highest.
Gas out of rich solution flash tank 12 tops and regenerator 8 tops gas out converge and enter regeneration gas separator 15 after cooling by regeneration gas cooler 14 and carry out gas-liquid separation, regeneration gas separator 15 bottoms parting liquid out enters the second pipeline 5, and regeneration gas separator 15 tops regeneration gas is out sent into subsequent compression liquefaction workshop section.
Enter reboiler 16 from the low-pressure steam of pipe network, the cooling vapour/liquid after release heat again discharges by rich solution reheater 11 drains collecting tank 17 that the condensate liquid forming after waste heat enters main equipment and reclaims.Regenerator 8 bottoms lean solution out enters absorption tower 1 through poor rich liquid heat exchanger 6.

Claims (3)

1. the carbon dioxide capture system of a multi-stage diffluence regeneration, it is characterized in that, comprise absorption tower (1), the rich solution that goes out absorption tower (1) is divided into two-way, be communicated with first pipeline (2) of the first control valve (3) and the top rich solution entrance (4) of regenerator (8), the second pipeline (5) is communicated with the rich solution entrance of poor rich liquid heat exchanger (6), the rich solution that goes out poor rich liquid heat exchanger (6) is also divided into two-way, one tunnel is established the second control valve (7) and is communicated with the middle part rich solution entrance (9) of regenerator (8), another road is established the 3rd control valve (10) and is communicated with the rich solution entrance of rich solution reheater (11), the rich solution outlet of rich solution reheater (11) is communicated with the rich solution entrance of rich solution flash tank (12), the rich solution outlet of described rich solution flash tank (12) bottom and the bottom rich solution entrance (13) of regenerator (8) are communicated with, after the gas vent at rich solution flash tank (12) top and the top gas export pipeline of regenerator (8) are communicated with and the gas access of regeneration gas cooler (14) is communicated with, the gas access of the gas vent of regeneration gas cooler (14) and regeneration gas separator (15) is communicated with, the bottom discharge channel of regeneration gas separator (15) and the second pipeline (5) are communicated with, the regeneration gas export pipeline at regeneration gas separator (15) top is communicated with subsequent compression liquefaction workshop section.
2. the carbon dioxide capture system of multi-stage diffluence regeneration according to claim 1, it is characterized in that, described regenerator (8) bottom is provided with reboiler (16), low-pressure steam from pipe network is communicated with the steam inlet of reboiler (16), cooling vapour/the liquid of the steam entrance of the outlet of reboiler (16) and rich solution reheater (11) is communicated with, and the drains collecting tank (17) of the steam cooling liquid outlet pipeline of rich solution reheater (11) and main equipment is communicated with.
3. the carbon dioxide capture system of multi-stage diffluence regeneration according to claim 1, it is characterized in that, the lean solution outlet of described regenerator (8) bottom and the lean solution entrance pipe of poor rich liquid heat exchanger (6) are communicated with, and the lean solution outlet of poor rich liquid heat exchanger (6) is communicated with the lean solution entrance of absorption tower (1).
CN201420212954.4U 2014-04-28 2014-04-28 Multistage split regeneration carbon dioxide trapping system CN203803335U (en)

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103961979A (en) * 2014-04-28 2014-08-06 中国华能集团清洁能源技术研究院有限公司 Multistage division regenerative carbon dioxide trapping system and technology
CN104817102A (en) * 2015-04-30 2015-08-05 华能国际电力股份有限公司 System device and process for liquid-phase indirect capture of carbon dioxide in mineralization smoke
CN106362551A (en) * 2016-11-23 2017-02-01 四川大学 System and technology for trapping CO2 in smoke
CN111203073A (en) * 2020-01-07 2020-05-29 浙江大学 Flue gas CO2Desorption device of trapping system
CN111203086A (en) * 2020-01-07 2020-05-29 浙江大学 CO with low regeneration energy consumption and low pollutant emission2Trapping system

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103961979A (en) * 2014-04-28 2014-08-06 中国华能集团清洁能源技术研究院有限公司 Multistage division regenerative carbon dioxide trapping system and technology
CN104817102A (en) * 2015-04-30 2015-08-05 华能国际电力股份有限公司 System device and process for liquid-phase indirect capture of carbon dioxide in mineralization smoke
CN104817102B (en) * 2015-04-30 2016-05-04 华能国际电力股份有限公司 A kind of liquid phase traps system and device and the technique of mineralising carbon dioxide in flue gas indirectly
CN106362551A (en) * 2016-11-23 2017-02-01 四川大学 System and technology for trapping CO2 in smoke
CN111203073A (en) * 2020-01-07 2020-05-29 浙江大学 Flue gas CO2Desorption device of trapping system
CN111203086A (en) * 2020-01-07 2020-05-29 浙江大学 CO with low regeneration energy consumption and low pollutant emission2Trapping system

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