CN102580467A - CO2 trapping system on basis of thermal steam compression and spraying temperature regulation - Google Patents
CO2 trapping system on basis of thermal steam compression and spraying temperature regulation Download PDFInfo
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- CN102580467A CN102580467A CN2012100176527A CN201210017652A CN102580467A CN 102580467 A CN102580467 A CN 102580467A CN 2012100176527 A CN2012100176527 A CN 2012100176527A CN 201210017652 A CN201210017652 A CN 201210017652A CN 102580467 A CN102580467 A CN 102580467A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
The invention relates to a CO2 trapping system on the basis of thermal steam compression and spraying temperature regulation. The system is characterized in that one-step or multistage thermal steam compression is adopted; overheated or saturated steam is used as working steam; after condensed water 13 is processed by a flash evaporation heater 30, flash evaporated water vapor enters a thermal steam compressor to be compressed to have steam parameters required by a solution scalder; and the temperature of the steam is regulated by adopting a condensed water reflux spraying mode. According to the system, the high energy grade of the overheated steam is sufficiently utilized, the overheated steam is used as the working steam of the thermal steam compressor and low-grade heat energy generated in the production process of the CO2 trapping system is recycled, so that the energy consumption of the system is greatly reduced and the thermal pollution to the environment is reduced.
Description
Technical field
Core of the present invention is to have proposed a kind of CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system is mainly used in and reduces chemical absorption method CO
2The energy consumption of trapping system.
Background technology
Fig. 1 carries out power-plant flue gas CO for adopting chemical absorption method
2Trapping system figure, its groundwork flow process is: send into absorption tower 2 by air-introduced machine, wherein a part of CO after flue gas behind the power plant desulfurization 1 is regulated flow
2Be absorbed agent and absorb, tail gas 3 enters atmosphere by cat head.Absorb CO
2After rich solution 4 by being pumped into poor rich liquid heat exchanger 5 through rich solution at the bottom of the absorption tower, reclaim the CO behind the heat
2 Rich solution 6 is sent into regenerator 7 and is carried out desorb.Separate the CO of sucking-off
2 Gas 14 after cooler 15 coolings, obtains purity products C O 99.5% or more after moisture is removed in 17 separation through the regeneration gas gas-liquid separator together with steam
2Gas 18 is sent into CO again
2Compressor boost, refrigeration liquefying, final storage and entrucking are defeated outward.
The rich solution 6 that comes out from poor rich liquid heat exchanger 5 gets into from regenerator 7 tops, through stripping desorb portion C O
2, get into solution boiling device 8 then, make CO wherein
2Further desorb.The heating steam 12 that drops in the solution boiling device comes from the superheated steam 9 that power plant steam turbine provides HTHP.Require (relevant with absorbent, generally about 100 ℃) in order to satisfy desorption temperature lower in the solution boiling device, the parameter that obtains technological requirement is mixed with superheated steam 9 and pressure and temperature reducing water 10 by system.The thermodynamics sophistication of this system is very low, and this mainly shows two aspects.One is that the superheated steam of high temperature, high pressure is middle pressure steam through mixed process decompression, is that a typical high-grade can directly convert the process that low-grade energy utilizes into, has produced very big available energy loss.Another is that the heat of this system is superfluous, but can not obtain utilizing because its grade is low.For example, heating steam 11 temperature of the condensed water under the condensation in the solution boiling device are higher relatively, and this part heat is not fully used; Leave the CO of regenerator
2Lean solution 21 further gets into and gets into absorption tower 2, CO after cooler 23 is emitted heat behind heat exchanger 5 heat exchangers
2Lean solution liberated heat in lean solution cooler 23 does not obtain utilizing yet; Leave the temperature very high (approximating resolution temperature) of the regeneration gas 14 of regenerator, also directly dump as used heat at cooler 15 liberated heats.
In sum, at existing power-plant flue gas CO
2In the trapping system, the superheated steam of high temperature, high pressure mixes the middle pressure steam that obtains technological requirement with pressure and temperature reducing water, causes the available energy loss, and superheated steam high-grade energy is not utilized effectively; Heating steam condensed water under the condensation in the solution boiling device is not rationally utilized; Lean solution cooler 23 is not recycled with regeneration gas cooler 15 liberated heats yet, and such energy utility system is unfavorable for the reduction of system energy consumption.The present invention is intended to make full use of the high-grade energy of superheated steam, and (Thermal Vapor Compressor, TVC) recycling system does not have the heat of recycling, reduces system energy consumption by the thermodynamic steam compressor.
Summary of the invention
The present invention recycles condensed water, CO for effectively utilizing the high-grade energy of superheated steam
2The heat of lean solution and regeneration gas reduces system energy consumption.
The technical scheme that the present invention proposes is: drive single-stage or multistage thermodynamic steam compressor with the high temperature of steam turbine extraction, the superheated steam of high pressure as working steam (driving steam); Condensed water 13 is introduced the flash vessel flash distillation, and the water vapour that flash distillation obtains is sent into the steam parameter that thermodynamic steam compressor compresses to solution boiling device requires.For flash distillation steam as much as possible, make full use of the tow taste heat that produces in the system production process, can lean solution that leave heat exchanger 5 22 and the regeneration gas of leaving regenerator 14 be introduced in flash distillation-heaters 30 the flash process heating to condensed water 13.The steam parameter that comes out from thermal compressor possibly be higher than needed middle pressure steam (parsing) temperature, for this reason, can adopt condensate return, to the steam cooling of spraying, it is adjusted to the needed temperature of technical process.Technical scheme sketch map of the present invention is as shown in Figure 2.
The present invention has following major technique advantage:
1. the high-grade heat energy of superheated steam is rationally utilized.Adopt the thermodynamic steam compressor; High steam (driving steam) with from steam turbine is a working media; Low parameter steam to from the condensate flash distillation compresses; The low grade heat energy that other position of low-grade condensed water and system is produced obtains recycling, and has improved the efficiency of system greatly, has reduced energy consumption.
2. system condensing water, CO
2The heat of lean solution and regeneration gas is recycled fully, has improved the thermodynamics sophistication of system greatly, has reduced the consumption of working steam 31.
3. practical.The thermodynamic steam compressor is 29 simple in structure, no-rotary part, life-span are long, reliable, is the equipment of technical maturation; Flash distillation-heater 30 is aggregates of a flash vessel and heat exchanger, and technical development is also very ripe.And, as if appropriate design, can save the lean solution cooler 23 and regeneration gas cooler 15 of original system.Therefore, improve the workable of system.
Description of drawings
Fig. 1 is power-plant flue gas CO
2Trapping system figure;
Fig. 2 is a technical scheme sketch map of the present invention;
Fig. 3 is for only recycling the system diagram of condensed water;
Fig. 4 is for reclaiming condensed water and CO
2The system diagram of lean solution heat;
Fig. 5 is for reclaiming the system diagram of condensed water and regeneration gas heat;
Label is among the accompanying drawing 1-5:
1-gets into the flue gas on absorption tower
The 2-absorption tower
3-leaves the flue gas on absorption tower
4-gets into the CO on absorption tower
2Rich solution
The 5-poor rich liquid heat exchanger
6-gets into the CO of regenerator
2Rich solution
The 7-regenerator
8-solution boiling device
9-superheated steam (mass flow is m, and temperature is t)
10-pressure and temperature reducing water
The 11-temperature-decreased pressure reducer
12-advances the saturated vapor of boiling device
13-leaves the condensed water of boiling device
14-leaves the regeneration gas of regenerator
15-regeneration gas cooler
16-gets into the regeneration gas of gas-liquid separator
The 17-gas-liquid separator
The 18-CO that regenerates
2
The 19-condensate liquid
The fluid infusion of 20-amine
21-leaves the CO of regenerator
2Lean solution
22-leaves the CO of heat exchanger
2Lean solution
23-lean solution cooler
24-gets into the CO on absorption tower
2Lean solution
The circulation water inlet of 25-washing tail gas
The cyclic water outlet of 26-washing tail gas
27-leaves the CO of boiling device
2
28-gets into the CO of boiling device
2Rich solution
29-thermodynamic steam compressor (TVC)
30-flash distillation-heater
(mass flow is m to 31-injector high-pressure work steam
p, pressure is p
p, temperature is t
pSuperheated steam)
(mass flow is m to the 32-flash-off steam
h, pressure is p
h, temperature is t
hSaturated vapor)
(mass flow is m to the 33-mixed vapour
c, pressure is p
c, temperature is t
cSuperheated steam)
34-spraying temperature adjustment water
35-flash distillation saturation water
36-waste heat source import (22 or 14 or two strands of hot-fluids)
37-waste heat source outlet (24 or 16 or two fluid streams)
The specific embodiment
The specific embodiment is that condensed water 13 is introduced the flash vessel flash distillation, and the water vapour that flash distillation obtains is sent into the steam parameter that thermodynamic steam compressor compresses to solution boiling device requires.For flash distillation steam as much as possible, the tow taste heat that produces in the system production process can be introduced in flash distillation-heaters 30 the flash process heating to condensed water 13 with the lean solution of leaving heat exchanger 5 22 and the regeneration gas of leaving regenerator 14.Adopt condensate return,, it is adjusted to the needed temperature of technical process the mixed vapour cooling of spraying.Fig. 2 to Fig. 5 has provided the recycling condensed water, reclaims condensed water and CO
2The lean solution heat reclaims condensed water and regeneration gas heat, reclaims condensed water, CO
2The system schematic of the heat of lean solution and regeneration gas.
1. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises absorption tower 2, poor rich liquid heat exchanger 5, regenerator 7; Solution boiling device 8, temperature-decreased pressure reducer 11, regeneration gas cooler 15, gas-liquid separator 17; Lean solution cooler 23 is characterized in that: also include thermodynamic steam compressor 29, flash distillation-heater 30.
Foregoing description be the flow process shown in the Figure of description 3.
2. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises absorption tower 2, poor rich liquid heat exchanger 5, regenerator 7, solution boiling device 8, temperature-decreased pressure reducer 11, regeneration gas cooler 15, gas-liquid separator 17 is characterized in that: also include thermodynamic steam compressor 29, flash distillation-heater 30.
Poor rich liquid heat exchanger 5 is connected with regenerator 7, and regenerator 7 is connected with gas-liquid separator 17 through regeneration gas cooler 15, and regenerator 7 also is connected with solution boiling device 8; Thermodynamic steam compressor 29 1 ends connect flash distillation-heater 30, and the other end connects temperature-decreased pressure reducer 11, and thermodynamic steam compressor 29 connects flash distillation-heater 30, solution boiling device 8, temperature-decreased pressure reducer 11 another loops of formation.
Explain: foregoing description be the flow process shown in the Figure of description 4.
3. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises absorption tower 2, poor rich liquid heat exchanger 5, regenerator 7, solution boiling device 8, temperature-decreased pressure reducer 11, gas-liquid separator 17, lean solution cooler 23 is characterized in that: also include thermodynamic steam compressor 29, flash distillation-heater 30.
Foregoing description be the flow process shown in the Figure of description 5.
4. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises absorption tower 2, poor rich liquid heat exchanger 5, regenerator 7, solution boiling device 8, temperature-decreased pressure reducer 11, gas-liquid separator 17 is characterized in that: also include thermodynamic steam compressor 29, flash distillation-heater 30.
Foregoing description be the flow process shown in the Figure of description 2.
Below with certain cover CO in fortune power plant
2Trapping system be that example is explained energy-saving effect of the present invention:
Fig. 1 is existing CO
2The main schematic flow sheet of trapping system.In order to satisfy the heating process requirement in the regenerator, the heat that consumes in the boiling device comes from the extracted steam from turbine of power plant.This system need extract 200t/h out, 1.1MPa, and 300 ℃ superheated steam produces 220t/h through temperature reducing and pressure reducing system, and pressure is that 0.4MPa, temperature are that 144 ℃ saturated vapor advances the solution boiling device, in the solution boiling device, heats CO
2Be condensed into 0.25MPa, temperature after the rich solution and be 128 ℃ condensed water.
Example 1 adopts the system of recovery condensed water heat shown in Figure 3, adopts two-stage to spray the flash-off steam of recycling condensed water.The technological parameter of regenerator and solution boiling device is constant, and the working steam of thermodynamic steam compressor comes from drawing gas of steam turbine, and 1.1MPa, 300 ℃ produces the superheated steam of 0.4MPa behind the suction flash-off steam.Main result of calculation is: first order jet coefficient 0.63, second level jet coefficient 0.29; Flash-off steam pressure 0.05MPa, the flash-off steam flow of suction is 16.9t/h; The mixed vapour flow that the thermodynamic steam compressor outlet obtains is 195.56t/h, and temperature is 274 ℃; Needing 24.44t/h spraying temperature adjustment water, is that 144 ℃ saturated vapor advances the solution boiling device with the mixed vapour temperature adjustment to temperature; The working steam flow that consumes altogether is 178.68t/h, and effectively jet coefficient is 0.094, the working steam amount Δ m=200-178.68=21.32t/h of saving, and fractional energy savings is 11.9%.Thus it is clear that, the CO of compression of employing thermodynamic steam and spraying temperature adjustment
2Behind the trapping system, energy consumption reduces.
Example 2 adopts Fig. 5 to reclaim the system of receiving condensed water and regeneration gas heat, and regeneration gas is introduced flash distillation-heater 30, and the condensed water after the regeneration gas heating step-down flashes off more steam, is recycled by the suction of two-stage heating power vapour compression machine.Systematic parameter is 1 identical with example, and promptly the technological parameter of regenerator and solution boiling device is constant, and the working steam of thermodynamic steam compressor comes from drawing gas of steam turbine, 1.1MPa, 300 ℃, the superheated steam of generation 0.4MPa behind the suction flash-off steam.Main result of calculation is: first order jet coefficient 0.62, second level jet coefficient 0.34; Flash-off steam pressure 0.07MPa, the flash-off steam flow of suction is 18.13t/h; The mixed vapour flow that the thermodynamic steam compressor outlet obtains is 187.55t/h, and temperature is 273 ℃; Needing 32.45t/h spraying temperature adjustment water, is that 144 ℃ saturated vapor advances the solution boiling device with mixed vapour temperature adjustment temperature; The working steam flow that consumes altogether is 169.44t/h, and effectively jet coefficient is 0.107, the working steam amount Δ m=200-169.44=30.56t/h of saving, and fractional energy savings is 18.0%.Thus it is clear that, the CO of compression of employing thermodynamic steam and spraying temperature adjustment
2Behind the trapping system, energy consumption reduces, and energy-saving effect is remarkable.
Claims (4)
1. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises the absorption tower, poor rich liquid heat exchanger, regenerator, the solution boiling device, temperature-decreased pressure reducer, the regeneration gas cooler, gas-liquid separator, the lean solution cooler is characterized in that: also include the thermodynamic steam compressor, flash distillation-heater;
The absorption tower connects poor rich liquid heat exchanger, connects into a closed-loop path through the lean solution cooler; Poor rich liquid heat exchanger is connected with regenerator, and regenerator is connected with gas-liquid separator through the regeneration gas cooler; Regenerator is connected with the solution boiling device, and the solution boiling device connects temperature-decreased pressure reducer and forms a closed-loop path; Thermodynamic steam compressor one end connects flash distillation-heater, and the other end connects temperature-decreased pressure reducer; The thermodynamic steam compressor connects flash distillation-heater, solution boiling device, another closed-loop path of temperature-decreased pressure reducer formation.
2. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises the absorption tower, poor rich liquid heat exchanger, regenerator, the solution boiling device, temperature-decreased pressure reducer, the regeneration gas cooler, gas-liquid separator is characterized in that: also include the thermodynamic steam compressor, flash distillation-heater;
The absorption tower connects poor rich liquid heat exchanger, and poor rich liquid heat exchanger connects an end of flash distillation-heater, and the other end of flash distillation-heater is connected to the absorption tower, and poor rich liquid heat exchanger, flash distillation-heater and absorption tower connect into a closed-loop path;
Poor rich liquid heat exchanger is connected with regenerator, and regenerator is connected with gas-liquid separator through the regeneration gas cooler, and regenerator also is connected with the solution boiling device; Thermodynamic steam compressor one end connects flash distillation-heater, and the other end connects temperature-decreased pressure reducer, and the thermodynamic steam compressor connects flash distillation-heater, solution boiling device, closed-loop path of temperature-decreased pressure reducer formation.
3. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises the absorption tower, poor rich liquid heat exchanger, regenerator, the solution boiling device, temperature-decreased pressure reducer, gas-liquid separator, the lean solution cooler is characterized in that: also include the thermodynamic steam compressor, flash distillation-heater;
The absorption tower connects poor rich liquid heat exchanger, connects into a closed-loop path through the lean solution cooler; Poor rich liquid heat exchanger is connected with regenerator, and the regeneration gas that regenerator comes out connects an end of flash distillation-heater, and the other end of flash distillation-heater is connected to gas-liquid separator, and regenerator also is connected with the solution boiling device; Thermodynamic steam compressor one end connects flash distillation-heater, and the other end connects temperature-decreased pressure reducer, and the thermodynamic steam compressor connects flash distillation-heater, solution boiling device, temperature-decreased pressure reducer formation closed-loop path.
4. CO based on thermodynamic steam compression and spraying temperature adjustment
2Trapping system, system mainly comprises the absorption tower, poor rich liquid heat exchanger, regenerator, the solution boiling device, temperature-decreased pressure reducer, gas-liquid separator is characterized in that: also include the thermodynamic steam compressor, flash distillation-heater;
The absorption tower connects poor rich liquid heat exchanger, and poor rich liquid heat exchanger connects an end of flash distillation-heater, and the other end of flash distillation-heater is connected to the absorption tower, and poor rich liquid heat exchanger, flash distillation-heater and absorption tower connect into a closed-loop path; Poor rich liquid heat exchanger is connected with regenerator, and the regeneration gas that regenerator comes out also connects an end of flash distillation-heater, and the other end of flash distillation-heater is connected to gas-liquid separator, and regenerator also is connected with the solution boiling device; Thermodynamic steam compressor one end connects flash distillation-heater, and the other end connects temperature-decreased pressure reducer, and the thermodynamic steam compressor connects flash distillation-heater, solution boiling device, temperature-decreased pressure reducer formation closed-loop path.
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| CN201210017652.7A CN102580467B (en) | 2012-01-19 | 2012-01-19 | CO2 trapping system on basis of thermal steam compression and spraying temperature regulation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210017652.7A CN102580467B (en) | 2012-01-19 | 2012-01-19 | CO2 trapping system on basis of thermal steam compression and spraying temperature regulation |
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| CN102580467A true CN102580467A (en) | 2012-07-18 |
| CN102580467B CN102580467B (en) | 2014-07-09 |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1229690A (en) * | 1998-03-19 | 1999-09-29 | 南化集团研究院 | Pressure variable regeration tech. of low supplying heat source |
| US20040219400A1 (en) * | 2003-01-22 | 2004-11-04 | Said Al-Hallaj | Hybrid fuel cell/desalination systems and method for use |
| CN101389913A (en) * | 2004-03-11 | 2009-03-18 | 先进提取技术有限公司 | Use of cryogenic temperatures in processing gases containing light components with physical solvents |
| CN101583411A (en) * | 2006-11-24 | 2009-11-18 | 阿克清洁碳公司 | Improved absorbent regeneration with flashed lean solution and heat integration |
| US8080089B1 (en) * | 2008-04-14 | 2011-12-20 | Bechtel Power Corporation | Method and apparatus for efficient gas treating system |
| CN202506294U (en) * | 2012-01-19 | 2012-10-31 | 北京工业大学 | Carbon dioxide (CO2) trapping system based on heating power vapor compression and spray temperature regulation |
-
2012
- 2012-01-19 CN CN201210017652.7A patent/CN102580467B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1229690A (en) * | 1998-03-19 | 1999-09-29 | 南化集团研究院 | Pressure variable regeration tech. of low supplying heat source |
| US20040219400A1 (en) * | 2003-01-22 | 2004-11-04 | Said Al-Hallaj | Hybrid fuel cell/desalination systems and method for use |
| CN101389913A (en) * | 2004-03-11 | 2009-03-18 | 先进提取技术有限公司 | Use of cryogenic temperatures in processing gases containing light components with physical solvents |
| CN101583411A (en) * | 2006-11-24 | 2009-11-18 | 阿克清洁碳公司 | Improved absorbent regeneration with flashed lean solution and heat integration |
| US8080089B1 (en) * | 2008-04-14 | 2011-12-20 | Bechtel Power Corporation | Method and apparatus for efficient gas treating system |
| CN202506294U (en) * | 2012-01-19 | 2012-10-31 | 北京工业大学 | Carbon dioxide (CO2) trapping system based on heating power vapor compression and spray temperature regulation |
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Inventor after: Liu Zhongliang Inventor after: Zhang Kefang Inventor after: Li Yanxia Inventor before: Liu Zhongliang Inventor before: Zhang Kefang Inventor before: Li Yanxia Inventor before: Li Da |
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Free format text: CORRECT: INVENTOR; FROM: LIU ZHONGLIANG ZHANG KEFANG LI YANXIA LI DA TO: LIU ZHONGLIANG ZHANG KEFANG LI YANXIA |
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Granted publication date: 20140709 Termination date: 20170119 |