CN102824815A - Absorption extraction process for carbon dioxide in normal-pressure gas - Google Patents

Absorption extraction process for carbon dioxide in normal-pressure gas Download PDF

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Publication number
CN102824815A
CN102824815A CN2012103421677A CN201210342167A CN102824815A CN 102824815 A CN102824815 A CN 102824815A CN 2012103421677 A CN2012103421677 A CN 2012103421677A CN 201210342167 A CN201210342167 A CN 201210342167A CN 102824815 A CN102824815 A CN 102824815A
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absorption
section
tower
desorber
carbon dioxide
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CN102824815B (en
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陈健
黄永权
施建超
俞惠
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JIANGSU RUNFENG ENVIRONMENTAL ENGINEERING Co Ltd
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JIANGSU RUNFENG ENVIRONMENTAL ENGINEERING Co Ltd
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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
    • 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

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Abstract

The invention discloses an absorption extraction process for carbon dioxide in normal-pressure gas. The invention comprises a three-section absorption tower and a two-section desorption tower. Lean solution and semi-lean solution respectively enter the first section and the second section of the absorption tower; a cooler is arranged between the second section and the third section of the absorption tower; liquid flowing out of the bottom part of the first section of desorption tower is divided into two parts, and the two parts of the liquid respectively enter the second section of the absorption tower and the second section of the desorption tower after heat exchange is ended. Moreover, continuous heat exchange heating of pregnant solution is adopted. For the absorption extraction of the carbon dioxide in the normal-pressure gas, the absorption extraction process for the carbon dioxide in the normal-pressure gas has the advantage of lower energy consumption.

Description

The absorption and separation technology of carbon dioxide in the atmosphere gas
Technical field
The present invention relates to the absorption and separation technology of carbon dioxide in a kind of atmosphere gas.
Background technology
Carbon dioxide (CO 2) capture of isothermal chamber gas separates, and amount is applied to the flue gas of industries such as coal fired power generation, Ferrous Metallurgy, cement, petrochemical industry, Coal Chemical Industry.Generally contain 5%～35% CO in these admixture of gas 2, the pressure range of gas is generally near normal pressure.And CO in such gas 2Separation, mainly adopt chemical absorbing solvent or Chemical Physics double solvents absorption process.
Comparatively ripe chemical absorption method absorption and separation CO in the present domestic and international industry 2Solvent mainly contain MEA (MEA), diethanol amine (DEA), diisopropanolamine (DIPA) (DIPA) and methyl diethanolamine (MDEA) and be the mixed solvent of main body.
And aspect absorption technique, to CO in the atmosphere gas 2Absorption and separation, be mostly simple absorption and desorption technology, energy consumption is very high, is generally 3.5～4.5GJ/ ton CO 2One Chinese patent application numbers 200310106567.9 has adopted two sections absorption towers and two sections desorbers, and the compound amine aqueous solution adopts lean solution and rich solution heat exchange, adopts the technological process of lean solution cooler, semi lean solution cooler again.One Chinese patent application numbers 200510021160.5 has announced that adopting MDEA to add phenodiazine penta ring, two piperazines and sterically hindered amines absorbs CO 2, but adopted the flow process of having only lean solution and rich solution and heat exchange thereof.One Chinese patent application numbers 200510021158.8 has announced that on the basis of above-mentioned this patent application the flash tank that has added a rich solution is used for other impurity such as flash distillation O2, SO2, NOX, CO.
For the carbon dioxide absorption in the atmosphere gas, technologic improvement is few at present.Therefore in order further to cut down the consumption of energy, be necessary to propose a kind of novel absorption technique, the energy of the various grades in the utilization system, the absorption and separation of realization low energy consumption.
Summary of the invention
The object of the present invention is to provide a kind of solubility that improves low pressure CO 2, desorption effect is good, the absorption and separation technology of carbon dioxide in the atmosphere gas that energy consumption is lower concerning absorbing and separating CO 2 simultaneously.
Technical solution of the present invention is:
The absorption and separation technology of carbon dioxide in a kind of atmosphere gas, the system that adopts absorption tower, Analytic Tower to form is characterized in that:
Three sections absorptions are adopted on the absorption tower, and first section has lean solution and semi lean solution entering absorption tower respectively with second section top, and cooling device is arranged between second section and the 3rd section, is used for cooling liquid or liquids and gases; The saturated absorption of coming out at the bottom of the tower CO 2Liquid become rich solution;
Desorber adopts two sections desorbs; The rich solution that comes out at the bottom of the absorption tower pass through respectively with semi lean solution, lean solution heat exchange after, get into desorber and carry out desorb for first section; The liquid over half that comes out in first section desorber bottom gets into second section on absorption tower through cooling off the back again with the rich solution heat exchange as semi lean solution, the liquid of the remainder that comes out in first section desorber bottom through and the lean solution heat exchange after second section top of entering desorber; The liquid that comes out at the bottom of second section desorber gets into first section top, absorption tower through heat exchange and cooling back as lean solution; Heater is equipped with in the desorber bottom, and CO is equipped with in the overhead gas outlet 2Cooler and knockout drum;
Absorption tower pressure is normal pressure, and scope is 0.80～1.5bar; The temperature range that absorption liquid enters the absorption tower is 30～50 ℃;
Desorber pressure is 1.5～2.5bar, and the temperature range of liquid outlet is 100～150 ℃ at the bottom of the tower.
Lyosoption in the system is a kind of amino organic amine aqueous solution of at least one organic uncle that contains, and the amino concentration of organic uncle is 25-55%; Said organic uncle's amino is N methyldiethanol amine (MDEA), triethanolamine (TEA), N-ethyl diethylamide (EDEA), N, in one in N-dimethyl-3-amino-1-propyl alcohol (DMAP), N-diethyl ethylene diamine (DEEA), the N methyl piperazine (MPZ) or several kinds.
The organic amine component that also contains at least a organic primary amino radical or secondary amino group in the lyosoption, its concentration are 5%～15%.
Primary amine is one or more in MEA (MEA), 2-methyl-2-amino-1-propyl alcohol (AMP), the single Propanolamine (MPA).Secondary amine is one or more in diethanol amine (DEA), piperazine (PZ), diisopropanolamine (DIPA) (DIPA), the 2-methyl piperazine (2-MPA).
Having added total amount in the lyosoption is 0.01～0.5% auxiliary agent.Auxiliary agent is one or more in corrosion inhibitor, antidegradant, antisludging agent, the antifoaming agent.
Absorption tower and desorber can adopt packed tower or adopt plate column, or a part adopts packed tower and other parts employing plate columns.
Absorbent according to the invention can be used for the various atmosphere gas mixtures of absorption and separation, comprises the CO in flue gas, the refinery gas 2
Experiment showed, and utilize technology absorption and separation CO according to the invention 2Process conditions be: the temperature that absorbent enters the absorption tower is 30～50 ℃; The temperature of lean solution is 100～150 ℃ at the bottom of the regenerator; The pressure on absorption tower is 0.8～1.5bar, and the regenerator bottom pressure is 1.5～2.5bar.
The present invention utilizes the shunting of absorption tower cooling, semi lean solution and comparatively complicated heat-exchange system, can improve the solubility to low pressure CO 2, and desorption effect is good, and energy consumption is lower concerning absorbing and separating CO 2 simultaneously.
Description of drawings
Below in conjunction with accompanying drawing and embodiment the present invention is described further.
Fig. 1 is the system diagram that absorption tower of the present invention, Analytic Tower are formed.
Among the figure: T-1: the absorption tower; T-2: desorber; T-3: knockout drum; E-1: rich solution semi lean solution heat exchanger; E-2: lean solution semi lean solution heat exchanger; E-3: semi lean solution cooler; E-4: lean solution cooler; E-5: absorption tower intercooler; E-6: heater (desorption tower reboiler); E-7:CO 2The gas cooler; E-8: rich solution lean solution heat exchanger.
The specific embodiment
Embodiment 1:
The absorption and separation technology of carbon dioxide in a kind of atmosphere gas, the system that adopts absorption tower, Analytic Tower to form is characterized in that:
Three sections absorptions are adopted on the absorption tower, and first section has lean solution and semi lean solution entering absorption tower respectively with second section top, and cooling device is arranged between second section and the 3rd section, is used for cooling liquid or liquids and gases; The saturated absorption of coming out at the bottom of the tower CO 2Liquid become rich solution;
Desorber adopts two sections desorbs; The rich solution that comes out at the bottom of the absorption tower pass through respectively with semi lean solution, lean solution heat exchange after, get into desorber and carry out desorb for first section; The liquid over half that comes out in first section desorber bottom gets into second section on absorption tower through cooling off the back again with the rich solution heat exchange as semi lean solution, the liquid of the remainder that comes out in first section desorber bottom through and the lean solution heat exchange after second section top of entering desorber; The liquid that comes out at the bottom of second section desorber gets into first section top, absorption tower through heat exchange and cooling back as lean solution; Heater is equipped with in the desorber bottom, and CO is equipped with in the overhead gas outlet 2Cooler and knockout drum;
The temperature range that absorption liquid enters the absorption tower is 30 ℃; The temperature range of liquid outlet is 100 ℃ at the bottom of the parsing Tata.
Flue-gas flow rate 1200m 3/ h, CO 2Concentration is 5%, and absorption tower pressure is 0.8bar, and desorber pressure is 1.5bar, and absorbent solution is the MEA of the MDEA+5% mass concentration of 25% mass concentration, and the lean solution flow is 1.0m 3/ h, semi lean solution flow are 3.0m 3/ h.Experimental result is: CO 2Yield be 95%, capturing energy consumption is 3.0GJ/ ton CO 2Than 3.5GJ/ ton CO 2Reduced by 14%.
Embodiment 2:
The temperature range that absorption liquid enters the absorption tower is 40 ℃; The temperature range of liquid outlet is 120 ℃ at the bottom of the parsing Tata.
Flue-gas flow rate 1500m 3/ h, CO 2Concentration is 20%, and absorption tower pressure is 1.2bar, and desorber pressure is 1.6bar, and absorbent solution is the DEA of the EDEA+10% mass concentration of 35% mass concentration, and the lean solution flow is 4.0m 3/ h, semi lean solution flow are 10.0m 3/ h.Experimental result is: CO 2Yield be 93%, capturing energy consumption is 2.8GJ/ ton CO 2Than 3.5GJ/ ton CO 2Reduced by 20%.All the other are with embodiment 1.
Embodiment 3:
The temperature range that absorption liquid enters the absorption tower is 50 ℃; The temperature range of liquid outlet is 150 ℃ at the bottom of the parsing Tata.
Flue-gas flow rate 1100m 3/ h, CO 2Concentration is 35%, and absorption tower pressure is 1.3bar, and desorber pressure is 2.0bar, and absorbent solution is 55% DEEA+10%DEA+5%PZ, and the lean solution flow is 5.0m 3/ h, semi lean solution flow are 15.0m 3/ h.Experimental result is: CO 2Yield be 92%, capturing energy consumption is 2.5GJ/ ton CO 2Than 3.5GJ/ ton CO 2Reduced by 28%.All the other are with embodiment 1.

Claims (6)

1. the absorption and separation technology of carbon dioxide in the atmosphere gas, the system that adopts absorption tower, Analytic Tower to form is characterized in that:
Three sections absorptions are adopted on the absorption tower, and first section has lean solution and semi lean solution entering absorption tower respectively with second section top, and cooling device is arranged between second section and the 3rd section, is used for cooling liquid or liquids and gases; The saturated absorption of coming out at the bottom of the tower CO 2Liquid become rich solution;
Desorber adopts two sections desorbs; The rich solution that comes out at the bottom of the absorption tower pass through respectively with semi lean solution, lean solution heat exchange after, get into desorber and carry out desorb for first section; The liquid over half that comes out in first section desorber bottom gets into second section on absorption tower through cooling off the back again with the rich solution heat exchange as semi lean solution, the liquid of the remainder that comes out in first section desorber bottom through and the lean solution heat exchange after second section top of entering desorber; The liquid that comes out at the bottom of second section desorber gets into first section top, absorption tower through heat exchange and cooling back as lean solution; Heater is equipped with in the desorber bottom, and CO is equipped with in the overhead gas outlet 2Cooler and knockout drum;
Absorption tower pressure is normal pressure, and scope is 0.80～1.5bar; The temperature range that absorption liquid enters the absorption tower is 30～50 ℃;
Desorber pressure is 1.5～2.5bar, and the temperature range of liquid outlet is 100～150 ℃ at the bottom of the tower.
2. the absorption and separation technology of carbon dioxide in the atmosphere gas according to claim 1 is characterized in that: the lyosoption in the system is a kind of amino organic amine aqueous solution of at least one organic uncle that contains, and the amino concentration of organic uncle is 25-55%; Said organic uncle's amino is N methyldiethanol amine, triethanolamine, N-ethyl diethylamide, N, in one in N-dimethyl-3-amino-1-propyl alcohol, N-diethyl ethylene diamine, the N methyl piperazine or several kinds.
3. the absorption and separation technology of carbon dioxide in the atmosphere gas according to claim 1 and 2 is characterized in that: also contain the organic amine component of at least a organic primary amino radical or secondary amino group in the lyosoption, its concentration is 5%～15%.
4. the absorption and separation technology of carbon dioxide in the atmosphere gas according to claim 3 is characterized in that: primary amine is one or more in MEA, 2-methyl-2-amino-1-propyl alcohol, the single Propanolamine; Secondary amine is one or more in diethanol amine, piperazine, diisopropanolamine (DIPA), the 2-methyl piperazine.
5. the absorption and separation technology of carbon dioxide in the atmosphere gas according to claim 1 and 2 is characterized in that: having added total amount in the lyosoption is 0.01～0.5% auxiliary agent; Auxiliary agent is one or more in corrosion inhibitor, antidegradant, antisludging agent, the antifoaming agent.
6. the absorption and separation technology of carbon dioxide in the atmosphere gas according to claim 1 and 2 is characterized in that: absorption tower and desorber can adopt packed tower or adopt plate column, or a part adopts packed tower and other parts employing plate columns.
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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109999618A (en) * 2019-04-25 2019-07-12 华能国际电力股份有限公司 System and method for separating carbon dioxide from medium-high pressure gas source
CN111298604A (en) * 2020-03-26 2020-06-19 中国神华能源股份有限公司国华电力分公司 System and method for capturing carbon dioxide in flue gas
CN113499671A (en) * 2021-08-25 2021-10-15 北京美斯顿科技开发有限公司 Layered carbon reduction system
CN115634566A (en) * 2022-10-28 2023-01-24 大连理工大学 MDEA semi-lean cycle desulfurization device and method using low-temperature heat

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1197763A (en) * 1998-04-10 1998-11-04 刘金成 Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes
CN101804286A (en) * 2010-02-10 2010-08-18 清华大学 Mixed absorbing agent for catching or separating carbon dioxide

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1197763A (en) * 1998-04-10 1998-11-04 刘金成 Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes
CN101804286A (en) * 2010-02-10 2010-08-18 清华大学 Mixed absorbing agent for catching or separating carbon dioxide

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109999618A (en) * 2019-04-25 2019-07-12 华能国际电力股份有限公司 System and method for separating carbon dioxide from medium-high pressure gas source
CN109999618B (en) * 2019-04-25 2024-05-14 华能国际电力股份有限公司 System and method for separating carbon dioxide from medium-high pressure gas source
CN111298604A (en) * 2020-03-26 2020-06-19 中国神华能源股份有限公司国华电力分公司 System and method for capturing carbon dioxide in flue gas
CN113499671A (en) * 2021-08-25 2021-10-15 北京美斯顿科技开发有限公司 Layered carbon reduction system
CN115634566A (en) * 2022-10-28 2023-01-24 大连理工大学 MDEA semi-lean cycle desulfurization device and method using low-temperature heat

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