CN208406530U - A kind of energy-saving carbon dioxide regeneration and compressibility - Google Patents
A kind of energy-saving carbon dioxide regeneration and compressibility Download PDFInfo
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- CN208406530U CN208406530U CN201820354448.7U CN201820354448U CN208406530U CN 208406530 U CN208406530 U CN 208406530U CN 201820354448 U CN201820354448 U CN 201820354448U CN 208406530 U CN208406530 U CN 208406530U
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Abstract
A kind of energy-saving carbon dioxide regeneration and compressibility, the utility model is by CO2Before compressing the preposition gas condenser to regeneration of link, and by CO2Compressor is substituted for vapour compression machine.The preposition increase that can cause to compress power consumption of compression link, because containing the vapor of about 30wt% in the gas of compression, but since compressed regeneration gas heat is recycled by heat exchanger, the steam heat consumption of reboiler can be greatly lowered, in general, the whole energy consumption of regeneration and compression link is remarkably decreased, and is played the role of energy-efficient.
Description
Technical field
The utility model belongs to collecting carbonic anhydride technical field, and in particular to a kind of energy-saving carbon dioxide regeneration and pressure
Compression system, by industries such as electric power, chemical industry, steel, cement using one of chemical absorption method carbon dioxide capture system section
Energy system and method, for reducing CO2The whole energy consumption level of regeneration and compression link.
Background technique
The CO that the industries such as electric power, chemical industry, steel, cement are largely discharged2It is the greenhouse gases for causing global climate change
Discharge important sources, by recent years constantly grope, flue gas (or tail gas) collecting carbonic anhydride, using with seal (CCUS) skill up for safekeeping
Art is widely regarded as the important technology approach realized extensive reduction of greenhouse gas discharge, contain climate change.Made using organic amine
Chemical absorption method for carbon dioxide absorption solvent is the smoke carbon dioxide capture technology of current main-stream, has developed hundred at present
10,000 tons are commercialized carbon capture device.Current the main reason for hindering carbon capture technology large-scale promotion first is that trapping operation at
This is excessively high.And CO2Steam heat consumption and CO in regenerative process2The energy consumption costs such as the power consumption during compressing and liquefying account for always running
80% or more of cost.Therefore, reduce carbon capture system energy consumption be current collecting carbonic anhydride technical research core hot spot it
One.
Conventional CO2It regenerates and to compress and liquefy technique as shown in Fig. 1.
Conventional CO2It regenerates and to compress and liquefy process flow as follows:
CO is absorbed in absorption tower2Solution (rich solution) afterwards enters regenerator 1 by top, heats and solves by reboiler 2
CO is sucked out2Gas；Lean solution after parsing is flowed out from 1 bottom of regenerator, carries out next absorption cycle into absorption tower；Regeneration gas
It is discharged at the top of regenerator 1, is cooled to 40 DEG C or so by regenerating Gas Cooler 3；Condensed water in regeneration gas is from gas-liquid separation
The outflow of 4 bottom of tank is injected from 1 tower top of regenerator by being condensed back pump 5, keeps systematic water balance；CO2Gas is from gas-liquid separation
It is discharged at the top of tank 4, into CO2Compressor 6 is compressed to 2.5MPa or so, is cooled to -20 DEG C or so subsequently into ammonia cold 7, obtains
To the liquid CO of supercooling2Product.
The heat of regenerator desorption is provided by reboiler 2.The MEA absorbent solution for being 30% for mass fraction, desorption
1 ton of CO out22 tons of steam are about consumed, regeneration heat consumption is about 3.8~4.2GJ/tCO2, regeneration steam cost accounts for always trapping cost
60%~70%, in addition compression and power consumption of refrigerating, entire energy consumption cost accounts for 80% or more of trapping cost.Therefore, seek one
Kind energy-saving regeneration and compression process, are very significant.
Summary of the invention
In order to overcome the above-mentioned problems of the prior art, the purpose of this utility model is to provide a kind of energy-saving dioxies
Change carbon regeneration and compressibility, compared with traditional handicraft, the utility model is by CO2Compress link it is preposition to regeneration gas condenser it
Before, and by CO2Compressor is substituted for vapour compression machine；The preposition increase that can cause to compress power consumption of compression link, because of compression
Gas in contain about 30wt% vapor, but due to compressed regeneration gas heat by heat exchanger recycling, can
The steam heat consumption of reboiler is greatly lowered, in general, the whole energy consumption of regeneration and compression link is remarkably decreased, and is risen
To energy-efficient effect.
In order to achieve the above object, the utility model adopts the following technical solution:
A kind of energy-saving carbon dioxide regeneration and compressibility, including regenerator 1, above 1 packing layer of regenerator and rich solution
Pipeline is connected, and is connected below 1 packing layer of regenerator with 4 cold side input port of heat exchanger, 4 cold side outlet port of heat exchanger and 2 cold side of reboiler
Entrance is connected, and 2 cold side outlet port of reboiler is connected with 1 bottom of regenerator, and 2 hot side entrance of reboiler is connected with jet chimney, then boils
2 hot side outlet of device is connected with condensing water conduit, and 1 bottom liquid outlet of regenerator is connected with lean solution pipeline, regenerates at the top of regenerator 1
Gas outlet is connected with 3 entrance of vapour compression machine, and the outlet of vapour compression machine 3 is connected with 4 hot side entrance of heat exchanger, 4 hot side of heat exchanger
Outlet is connected with 5 entrance of condenser, and the outlet of condenser 5 is connected with 6 entrance of knockout drum, and 6 bottom liquid of knockout drum goes out
Mouth is connected with 7 entrances of pump are condensed back, and condensing reflux pump 7 is exported to be connected with 8 entrance of current divider, and current divider 8 exports I and regenerator
1 top is connected, and current divider 8 exports II and is connected with 3 entrance of vapour compression machine, the outlet of 6 top gas of knockout drum and ammonia cold 9
Entrance is connected, the outlet of ammonia cold 9 and liquid CO2Output channel is connected.
It is 30% MEA as absorbent solution that the regenerator 1, which uses mass fraction,.
The energy-saving carbon dioxide regeneration and the carbon dioxide regeneration of compressibility and compression method, absorb CO2Afterwards
Rich solution is flowed through packing layer, is successively entered heat exchanger 4 and reboiler 2, be heated by entering regenerator 1 above 1 packing layer of regenerator
To 110~120 DEG C, CO is desorbed2Gas；Lean solution after parsing is flowed out from 1 bottom of regenerator, is carried out into absorption tower next
Absorption cycle；The regeneration gas being discharged at the top of regenerator 1 enters vapour compression machine 3, by multi-stage compression and entrance spraying cooling,
The overheat regeneration gas of high pressure is obtained, it is regeneration gas condensed water that the spraying cooling of 3 entrance of vapour compression machine, which comes from current divider 8 with water,；
The high pressure superheater regeneration gas that vapour compression machine 3 exports enters heat exchanger 4, exchanges heat with cold side rich solution, regeneration gas temperature is down to
125~130 DEG C, the vapor in regeneration gas is largely condensed into liquid, is cooled further to 35~40 subsequently into condenser 5
DEG C, gas-liquid separation is carried out into gas-liquid separator 6；The CO separated2Gas enters ammonia cold 9 and is cooled to -20 DEG C, obtains
The liquid CO of supercooling2Product；The condensate liquid that 6 bottom of gas-liquid separator is separated, which is condensed back, pumps 7 and current divider 8, and one
Divide into 3 entrance of vapour compression machine and enter the cooling of 1 top spray of regenerator for spraying desuperheat, remaining condensed water, holding is
System water balance.
Energy-saving CO described in the utility model2Regeneration and compressibility and method have the following characteristics that
1) CO described in the utility model2Regeneration and compressibility improve in such a way that regeneration gas is first compressed and condensed again
Vapor waste heat is sampled in regeneration gas, is recycled by heat exchanger, is considerably reduced reboiler；If using quality
The MEA that score is 30% can reduce reboiler 45% as absorbent solution, energy conserving system described in the utility model and method
Left and right.
2) CO described in the utility model2The power consumption of compressor of regeneration and compressibility increased, this is because compression is again
In anger caused by vapor, but from the point of view of energy consumption cost, the increase of compression link power consumption is much smaller than the heat consumption for regenerating link
It reduces, comprehensive energy consumption cost is significantly reduced；By taking 30%MEA solution system as an example, the increase of power consumption is about 90kWh/tCO2,
The reduction of steam heat consumption is about 1.8GJ/tCO2, estimated by 0.35 yuan/kWh of electricity price, 60 yuan/GJ of steam, comprehensive trapping energy consumption at
70 yuan/tCO of this reduction2。
3) CO described in the utility model2Regeneration and compressibility can considerably reduce the cooling load of regeneration gas；With
For 30%MEA solution system, regeneration air cooling load (containing the cooling load of compressor) 75% or so is reduced.
4) CO described in the utility model2Regeneration and compressibility can reduce CO2Water content in product gas；It is molten with 30%MEA
For liquid system, CO2Aqueous in product gas is down to 0.2% hereinafter, considerably reducing refining system by original 2% or so
Molecular sieve remove Water l oad.
5) CO described in the utility model2The compressor of regeneration and compressibility is vapour compression machine, than making in traditional handicraft
CO2Compressor has higher high temperature resistant and corrosion-resistant requirement, equipment cost higher.
Detailed description of the invention
Fig. 1 is conventional CO2Regenerate and compress and liquefy the process flow diagram of system.
Fig. 2 is CO described in the utility model2The process flow diagram of regeneration and compressibility.
Figure of description is used to provide a further understanding of the present invention, and constitutes a part of the utility model, this
The illustrative embodiments and their description of utility model do not constitute the improper limit to the utility model for explaining the utility model
It is fixed.
Specific embodiment
The utility model to clearly illustrate carries out the utility model further detailed below with reference to examples and drawings
Explanation.Skilled in the art realises that following the description is not the limitation to scope of protection of the utility model, it is any practical new at this
The improvements and changes made on the basis of type, are within the protection scope of the utility model.
As shown in Figure 1, a kind of energy-saving carbon dioxide regeneration of the utility model and compressibility, including regenerator 1, regeneration
It is connected above 1 packing layer of tower with rich solution pipeline, is connected below 1 packing layer of regenerator with 4 cold side input port of heat exchanger, heat exchanger 4 is cold
Side outlet is connected with 2 cold side input port of reboiler, and 2 cold side outlet port of reboiler is connected with 1 bottom of regenerator, 2 hot side entrance of reboiler
It is connected with jet chimney, 2 hot side outlet of reboiler is connected with condensing water conduit, 1 bottom liquid outlet of regenerator and lean solution pipeline
It is connected, the outlet of 1 top regeneration gas of regenerator is connected with 3 entrance of vapour compression machine, the outlet of vapour compression machine 3 and 4 hot side of heat exchanger
Entrance is connected, and 4 hot side outlet of heat exchanger is connected with 5 entrance of condenser, and the outlet of condenser 5 is connected with 6 entrance of knockout drum, gas
6 bottom liquid outlet of liquid knockout drum is connected with 7 entrances of pump are condensed back, and is condensed back 7 outlet of pump and is connected with 8 entrance of current divider,
Current divider 8 exports to be connected at the top of I and regenerator 1, and current divider 8 exports II and is connected with 3 entrance of vapour compression machine, knockout drum 6
Top gas outlet is connected with 9 entrance of ammonia cold, the outlet of ammonia cold 9 and liquid CO2Output channel is connected.
The process flow of system described in the utility model is as follows:
Absorb CO2Rich solution afterwards is flowed through packing layer, is successively entered heat exchange by entering regenerator 1 above 1 packing layer of regenerator
Device 4 and reboiler 2, are heated to 110~120 DEG C, desorb CO2Gas；Lean solution after parsing is flowed out from 1 bottom of regenerator,
Next absorption cycle is carried out into absorption tower；(180kPa/100 DEG C or so) of the regeneration gas being discharged at the top of regenerator 1 entrance
Vapour compression machine 3 obtains an overheat regeneration gas (2.5MPa/210 DEG C of left side for high pressure by multi-stage compression and entrance spraying cooling
It is right), it is regeneration gas condensed water that the spraying cooling of 3 entrance of vapour compression machine, which comes from current divider 8 with water,；What vapour compression machine 3 exported
High pressure superheater regeneration gas enters heat exchanger 4, exchanges heat with cold side rich solution, and regeneration gas temperature is down to 130 DEG C or so, in regeneration gas
Vapor be largely condensed into liquid, 40 DEG C or so are cooled further to subsequently into condenser 5, into gas-liquid separator 6
Carry out gas-liquid separation；The CO separated2Gas enters ammonia cold 9 and is cooled to -20 DEG C or so, the liquid CO being subcooled2It produces
Product (2.5MPa, -20 DEG C)；The condensate liquid that 6 bottom of gas-liquid separator is separated is condensed back pump 7 and current divider 8, a part
Enter the cooling of 1 top spray of regenerator for spraying desuperheat, remaining condensed water into 3 entrance of vapour compression machine, keep system
Water balance.
Claims (2)
1. a kind of energy-saving carbon dioxide regeneration and compressibility, including regenerator (1), regenerator (1) packing layer top and richness
Liquid pipe road is connected, it is characterised in that: it is connected below regenerator (1) packing layer with heat exchanger (4) cold side input port, heat exchanger
(4) cold side outlet port is connected with reboiler (2) cold side input port, and reboiler (2) cold side outlet port is connected with regenerator (1) bottom, then boils
Device (2) hot side entrance is connected with jet chimney, and reboiler (2) hot side outlet is connected with condensing water conduit, regenerator (1) bottom liquid
Body outlet is connected with lean solution pipeline, and regeneration gas outlet is connected with vapour compression machine (3) entrance at the top of regenerator (1), both vapor compression
Machine (3) outlet is connected with heat exchanger (4) hot side entrance, and heat exchanger (4) hot side outlet is connected with condenser (5) entrance, condenser
(5) outlet is connected with knockout drum (6) entrance, and knockout drum (6) bottom liquid outlet pumps (7) entrance phase with condensing reflux
Even, pump (7) outlet is condensed back to be connected with current divider (8) entrance, current divider (8) exports to be connected at the top of I and regenerator (1), point
Stream device (8) outlet II is connected with vapour compression machine (3) entrance, the outlet of knockout drum (6) top gas and ammonia cold (9) entrance
It is connected, ammonia cold (9) outlet and liquid CO2Output channel is connected.
2. a kind of energy-saving carbon dioxide regeneration according to claim 1 and compressibility, it is characterised in that: the regeneration
It is 30% MEA as absorbent solution that tower (1), which uses mass fraction,.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820354448.7U CN208406530U (en) | 2018-03-15 | 2018-03-15 | A kind of energy-saving carbon dioxide regeneration and compressibility |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820354448.7U CN208406530U (en) | 2018-03-15 | 2018-03-15 | A kind of energy-saving carbon dioxide regeneration and compressibility |
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| CN208406530U true CN208406530U (en) | 2019-01-22 |
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| CN201820354448.7U Active CN208406530U (en) | 2018-03-15 | 2018-03-15 | A kind of energy-saving carbon dioxide regeneration and compressibility |
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2018
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