CN110152453B - Method and apparatus for capturing acid gases in gas mixtures using solvent absorption - Google Patents
Method and apparatus for capturing acid gases in gas mixtures using solvent absorption Download PDFInfo
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- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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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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- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a method and equipment for trapping acid gas in a gas mixture by using a solvent absorption method, wherein the method comprises the following steps: and shunting the high-temperature barren solution flowing out of the bottom of the desorption tower before or during heat exchange, and respectively exchanging heat with the internal liquid in the solvent absorption process and the cold fluid outside the solvent absorption process. The process of shunting the high-temperature barren solution in the solvent absorption method before or during heat exchange is called barren solution shunting, so that the comprehensive energy consumption for capturing and separating the acid gases such as carbon dioxide and the like by the absorption method can be reduced by about 5-10%.
Description
Technical Field
The invention relates to the technical field of gas separation, in particular to a method and equipment for trapping acid gas in a gas mixture by using a solvent absorption method.
Background
Carbon dioxide (CO)2) The emission of greenhouse gases is a main factor causing climate change, and how to enrich CO2Low energy consumption and low cost CO capture or separation in gas mixtures or liquefied gases2It is very important. These mixtures include flue gases, refinery gases, natural gases, liquefied gases, synthesis gases, shift gases, and hydrogen production, among others. The gas mixture contains 5-50% of CO2Other acid gases include SO2、H2S and organic sulfur CH3S, COS, etc., other gases consisting of N2、O2、Ar、CO、H2、CH4、C2H6. The pressure variation range of the gas is large (0.5-90 bar), and the method is suitable for capturing and separating CO by adopting a chemical absorption method, a physical absorption method or a chemical and physical composite absorption method2And the like acid gas components.
At present, the industrial mature capture and separation of CO at home and abroad2The solvent of acidic gas is mainly chemical absorption solvent such as organic amine and inorganic salt, and physical absorption solvent such as alcohols, esters, ethers, etc. Organic amine solvents such as a monoethanolamine Method (MEA), a diethanolamine method (DEA), a 2-amino-2-methyl-1-propanol (AMP), a diisopropanolamine method (DIPA) and a methyldiethanolamine Method (MDEA) are mainly suitable for trapping and separating acid gases in medium and low pressure gases. And physical solvents such as methanol, propylene carbonate, polyether alcohol and the like are mainly suitable for separating high-concentration acid gas in a high-pressure system. In order to improve the absorption solution to acidic gas CO2The solvent with higher absorption speed, such as MEA and Piperazine (PZ), is added into the solvent with lower absorption speed to form a mixed solvent with high absorption solubility and high absorption speed, so that the energy consumption and the cost for the capture and separation of the acid gas can be greatly reduced.
In addition to the absorption solvent, the process flow of the absorption process is also CO reduction2And the key of energy consumption and cost for capturing and separating the acid gas. The conventional absorption process flow comprises raw material gas pretreatment, absorption, purified gas cooling and gas-liquid separation, barren solution and rich solution heat exchange, heating desorption, regenerated gas cooling and separation, barren solution cooling and the like. The following process flow is improved on the basis of the conventional process flow, so that the energy consumption for trapping and separating is reduced to different degrees.
Cooling inside the absorber is an improved Process which has been extensively studied in numerous documents (Woertz, b.b.,1966.Process for removing acidic compositions from gas sources laboratories. patent No. us 3266220a1, Union Oil Co.). The absorption tower is internally cooled, namely, a part or all of liquid phase materials are taken out from the middle of the absorption tower, the taken-out liquid phase is cooled by heat exchange equipment, and the cooled material flow is sent back to the absorption tower. It is also possible to use a cooling device directly in the middle of the absorption column. Due to CO2When the absorption process of the acidic gas is exothermic, the temperature rise in the absorption tower is not beneficial to absorption in the absorption process, and the CO content of the solvent is reduced2The absorption effect of (2) increases the circulation amount of the solvent, and then increases the energy consumption of the reboiler of the desorption tower. The solution in the middle of the absorption tower is obtained by improving the cold flow in the absorption towerThe temperature of the agent is reduced, and the absorption of CO by the solvent is improved2The solvent circulation amount is finally reduced, and the energy consumption of the reboiler is reduced. Aiming at different solvents, the energy consumption of the reboiler can be reduced by 3-7%.
The study of the process of splitting rich liquid dates back to Eisenberg and Johnson at the earliest (Eisenberg and Johnson,1979.Amine regeneration Process. patent No. US 4152217A1, Exxon Research and Engineering Company.). The simple improved process is to divide the rich liquid taken out from the bottom of the absorption tower into two parts, wherein one part is not heated by a heat exchanger and is directly injected into the top of the desorption tower, and the other part enters the part below the top of the desorption tower after being heated by the heat exchanger. By applying the improved flow of rich liquid flow division, the energy consumption of the reboiler of the desorption tower can be obviously reduced. The unheated cold rich liquid enters from the top of the desorption tower and meets high-temperature gas phase (the main component is gaseous H) at the top of the desorption tower2O and CO2) Then absorbing the heat of the high-temperature gas phase and releasing CO2While part of the steam in the high-temperature gas phase is cooled and liquefied, CO2The discharge from the top of the column is continued. The temperature of the gas phase extracted from the top of the tower is lower, the heat taken away by the gas phase is reduced, and the energy consumption of the reboiler is reduced. Meanwhile, the other cold rich liquid can be heated to a higher temperature when passing through the heat exchanger due to the reduction of the amount, so that CO2 is released in the desorption tower more easily, and the energy consumption required by the reboiler is reduced. Aiming at different solvents, the energy consumption of the reboiler can be reduced by 8-15% by adopting a process flow of rich liquid shunting.
Another similar method of utilizing the heat of the stripping gas is the heat exchange between the rich and desorbed gases (Herrin,1989.Process sequencing for amine regeneration. patent No. us 4798910a1.) which is based on the same principle as the split stream of the rich liquid, but with no mass exchange between the rich and desorbed gases, only heat exchange.
The semi-barren liquor diversion technique, which may also be referred to as solution diversion, was first proposed by Shoeld (Shoeld,1934.Purification and separation of gases mixtures. patent No. US 1971798, The Koppers Co.). The absorption column and the desorption column are both divided into upper and lower portions, and the liquid absorbing more gas in the lower portion of the absorption is desorbed in the upper portion of the desorption column, and the solution absorbing less gas in the upper portion of the absorption column is desorbed in the lower portion of the desorption column. Another Improved process, in the case of a single absorber and a single desorber, takes a portion of the solution in the middle of the desorber, after heat exchange and cooling, is sent to the middle of the absorber (Reddy, et al, 2004.Improved split flow process and apparatus. patent No. wo 2004005818a2, Fluor Corporation.). The technology utilizes the advantage of low CO2 desorption heat in high-load solution, and can save energy by about 7-10%.
Lean flash compression is one of the most widely improved processes being studied (Benson and McRea,1979.Removal of acid gases from hot gases mixtures. patent No. US4160810A1, Benfield Corporation.) (Reddy et al, 2007.Integrated compressor/rectifier configurations and methods. patent No. WO2007075466A2, Fluor Technologies Corporation). The hot barren solution extracted from the bottom of the desorption tower is firstly introduced into a low-pressure flash tank for flash evaporation, the gas phase obtained by flash evaporation is compressed by a compressor and then introduced into the position above the bottom of the desorption tower, and the liquid phase obtained by flash evaporation is still subjected to heat exchange and cooling and then enters the absorption tower. The gas phase obtained from the flash tank works through the compressor, can reach higher temperature, and can provide part of heat for the desorption process after being introduced into the desorption tower, so that the heat load of the reboiler of the desorption tower is reduced. Aiming at different solvents, the energy consumption of the reboiler can be reduced by 10-13% by adopting a lean solution flash evaporation compression process flow. Because the compressor is introduced into the flow, the total energy consumption is reduced by 3-5% after the power consumption is considered.
The energy consumption in the trapping and separating process can be further reduced by combining the improvement of the process flow. For example, the energy consumption can be reduced by 10-20% in the total process of cold in the absorption tower, rich liquid diversion, cold in the absorption tower, lean liquid flash compression and the like.
In the aspect of energy integration in other industrial processes such as separation and collection process, coal-fired power generation and the like, the main process flow comprises utilization of flue gas energy, utilization of desorption gas energy and the like.
There are two methods of utilizing the energy of the high-temperature flue gas, one is to utilize the high-temperature flue gas to heat the rich liquor (Bens)on Homer and Mcrea Donald,1979.Removal of acid gases from hot gases mixtures. patent No. US4160810.Benfield Corp.). The other is to heat the middle liquid of the desorption tower by using high-temperature flue gas (TAKASHI et al, 2006, Apparatus and method for CO)2recovery. JP20050047857.Mitsubishi gravity Ind, Kansai Electric Power Co.). However, the flue gas contains sulfur dioxide, and the flue gas forms sulfuric acid after being cooled, so that a high-standard anticorrosive material is required.
In a method of utilizing energy of a desorption gas in a regeneration column of a carbon dioxide capture device, a gas temperature is raised by compression, water is sprayed to generate steam, and then heat is utilized by heat exchange (Woodhouse, 2008.Improved adsorbent regeneration. patent No. wo2008063082, cn101610828a. aker clean carbon As.). The recovered energy can be used for regenerating steam at the bottom of the regeneration tower and heating other material flows.
In the process flow, there are techniques for reducing the trapping energy consumption in the trapping process by the absorption method, and there are also comprehensive utilization of the flue gas heat and the desorbed gas heat. In the absorption method trapping process, high-temperature barren liquor coming out of the bottom of a desorption tower or the bottom of a reboiler of the desorption tower is used for heating rich liquor in a heat exchanger, or steam is firstly flashed out and then subjected to heat exchange in the heat exchanger for cooling, the temperature of the barren liquor is reduced to about 333K, then the barren liquor is cooled to about 313K by cooling water, and then the barren liquor enters an absorption tower for recycling. Before being cooled by cooling water, the temperature of the barren solution is only about 333K, which is not used greatly in other industrial processes such as coal-fired power plants and the like, and only cooling water is used for cooling.
Disclosure of Invention
The invention aims to provide a method for trapping acid gas in a gas mixture by using a solvent absorption method, which comprises the following steps:
and shunting the high-temperature barren solution flowing out of the bottom of the desorption tower, and respectively exchanging heat with the internal liquid in the solvent absorption process and the cold fluid outside the solvent absorption process.
The acid gas in the present invention means carbon dioxide, sulfur dioxide, etc.
The method of shunting the high-temperature lean solution may be referred to as a lean solution shunting. The invention divides the high-temperature barren solution flowing out from the bottom of the desorption tower, and the high-temperature barren solution is respectively used for heat exchange with the internal liquid and heating the low-temperature fluid in other processes, so that the comprehensive energy consumption for capturing and separating the acid gases such as carbon dioxide and the like by an absorption method can be reduced by about 5-10%.
Wherein, the desorption tower comprises a reboiler, and the high-temperature barren liquor can also be the high-temperature barren liquor flowing out from the bottom of the reboiler.
The invention can divide the high-temperature lean solution into two streams, namely, the high-temperature lean solution is divided into at least two streams of liquid, wherein at least one stream is used for exchanging heat with the internal liquid (which can be rich liquid in the solvent absorption process) in the solvent absorption process, at least another stream is used for exchanging heat with the cold fluid outside the solvent absorption process, namely, a first part of the lean solution is used for exchanging heat with the rich solution, and a second part of the lean solution is used for heating the cold fluid in other processes, such as circulating water for coal-fired power generation and the like.
The invention can also further cool the high-temperature barren solution after heat exchange and add the cooled high-temperature barren solution into the absorption tower corresponding to the desorption tower for circularly absorbing the acid gas. Specifically, as shown in fig. 1, the flue gas G1 enters the absorption tower, and contacts with the lean liquid L4 (cooled by the cooler E5 at this time) entering the top of the absorption tower to absorb CO2The post-rich liquid R1 is output from the bottom of the tower, and part of CO is removed2The temperature of the overhead gas flow is reduced by E3, and then the overhead gas flow is separated by a gas-liquid separator F1, the separated purified gas G2 is output to an absorption tower, and the liquid flows back to the absorption tower. And the rich liquid R1 is heated by a heat exchanger E1 and enters the top of the desorption tower for desorption. A reboiler E2 was provided at the bottom of the desorption column, and the column was heated and reboiled with steam Z1. The high-temperature lean liquid L1 flowing out of the bottom of the desorption tower or the bottom of a reboiler of the desorption tower is divided into two streams (L2 and L3) or more, at least one stream L2 is used for exchanging heat with liquid (such as rich liquid R1) in the absorption process (in a heat exchanger E1), and at least one stream L3 is used for exchanging heat with cold fluid W1 outside the absorption process (in a heat exchanger E6). The barren solution after heat exchange is combined with L4 or respectively further cooled and then enters an absorption tower for circularly absorbing the dioxideCarbon and other acidic gases. The desorption gas G3 coming out of the top of the desorption tower is cooled by a cooler E4 and then enters a gas-liquid separator F2, the separated gas G4 is discharged, and the liquid flows back to the top of the desorption tower.
In the invention, the lean-rich liquid heat exchanger can also be divided into two or more than three heat exchangers connected in series, and part of lean liquid is extracted in the middle of the heat exchange process and is used for heating the low-temperature fluid in other processes. Specifically, as shown in fig. 2, the flue gas G1 enters the absorption tower, and contacts with the lean liquid L4 (cooled by the cooler E5 at this time) entering the top of the absorption tower to absorb CO2The post-rich liquid R1 is output from the bottom of the tower, and part of CO is removed2The temperature of the overhead gas flow is reduced by E3, and then the overhead gas flow is separated by a gas-liquid separator F1, the separated purified gas G2 is output to an absorption tower, and the liquid flows back to the absorption tower. And the rich liquid R1 is heated by heat exchangers E1 and E7 and enters the top of the desorption tower for desorption. A reboiler E2 was provided at the bottom of the desorption column, and the column was heated and reboiled with steam Z1. The high-temperature lean liquid L1 flowing out of the bottom of the desorption tower or the bottom of a reboiler of the desorption tower is divided into two streams (L2 and L3) or more after being subjected to heat exchange (carried out in a heat exchanger E7) with a liquid in the absorption process (such as a rich liquid R2), at least one stream L2 is continuously subjected to heat exchange (carried out in a heat exchanger E1) with the liquid in the absorption process (such as a rich liquid R1), and at least one stream L3 is subjected to heat exchange (carried out in a heat exchanger E6) with a cold fluid W1 outside the absorption process. The lean solution after heat exchange is combined with L4 or respectively further cooled and then enters an absorption tower for circularly absorbing acid gases such as carbon dioxide and the like. The desorption gas G3 coming out of the top of the desorption tower is cooled by a cooler E4 and then enters a gas-liquid separator F2, the separated gas G4 is discharged, and the liquid flows back to the top of the desorption tower.
The invention can also adopt a complex heat exchanger to exchange heat between the cryogenic fluid in other processes and a plurality of streams of barren solution, rich solution and the like. Namely, the high-temperature barren solution can exchange heat with at least one strand of internal liquid in the solvent absorption process and at least one strand of cold fluid outside the solvent absorption process, and the barren solution after heat exchange enters an absorption tower after being cooled for circularly absorbing acid gas. Specifically, as shown in FIG. 3, flue gas G1 enters an absorption tower, andlean liquid L4 (cooled by cooler E5) entering from the top of the absorption tower is contacted to absorb CO2The post-rich liquid R1 is output from the bottom of the tower, and part of CO is removed2The temperature of the overhead gas flow is reduced by E3, and then the overhead gas flow is separated by a gas-liquid separator F1, the separated purified gas G2 is output to an absorption tower, and the liquid flows back to the absorption tower. And the rich liquid R1 is heated by a heat exchanger E1 and enters the top of the desorption tower for desorption. A reboiler E2 was provided at the bottom of the desorption column, and the column was heated and reboiled with steam Z1. The high-temperature lean liquid L1 from the bottom of the desorption tower or the bottom of a reboiler of the desorption tower, at least one liquid in the absorption process (such as a rich liquid R1) and at least one cold fluid W1 outside the absorption process exchange heat in a complicated heat exchanger E1. The lean liquid L4 after heat exchange is further cooled and then enters an absorption tower for circularly absorbing acid gases such as carbon dioxide. The desorption gas G3 coming out of the top of the desorption tower is cooled by a cooler E4 and then enters a gas-liquid separator F2, the separated gas G4 is discharged, and the liquid flows back to the top of the desorption tower.
In the invention, the method of the invention can be combined with one or more processes in other energy-saving technologies (such as cold in an absorption tower, rich liquid shunting, semi-barren liquid shunting, barren liquid flash compression and the like) to form a more complex energy-saving process, thereby further reducing the total energy consumption for capturing and separating acid gases such as carbon dioxide and the like by an absorption method.
The invention also provides an apparatus for capturing acid gases in a gas mixture using solvent absorption, comprising: the absorption tower and the desorption tower, the bottom of the desorption tower is provided with a high-temperature barren solution output pipeline, and the high-temperature barren solution output pipeline is used for enabling the high-temperature barren solution to be shunted and used for exchanging heat with the internal liquid in the solvent absorption method process and the cold fluid outside the solvent absorption method process.
In a preferred embodiment of the present invention, the apparatus further comprises:
an internal liquid transfer pipe connected to the absorption column for transferring the internal liquid during the solvent absorption process;
a cold fluid transfer line for transferring cold fluid outside the solvent absorption process;
after the high-temperature lean solution in the high-temperature lean solution output pipeline is shunted, heat exchange is respectively carried out between the high-temperature lean solution and the internal liquid in the internal liquid conveying pipeline and between the high-temperature lean solution and the cold fluid in the cold fluid conveying pipeline through a heat exchanger;
the barren liquor conveying pipeline is connected with the absorption tower and is used for conveying the barren liquor subjected to heat exchange to the absorption tower;
and the internal liquid conveying pipeline is connected with the desorption tower and is used for conveying the internal liquid after heat exchange to the desorption tower.
In a preferred embodiment of the present invention, the apparatus further comprises:
the heat exchanger is arranged close to the joint of the high-temperature barren solution output pipeline and the desorption tower and is used for performing partial heat exchange on the high-temperature barren solution and internal liquid and then shunting the high-temperature barren solution.
The new method is adopted, and the first part of the lean solution which is separated from the flow is used for exchanging heat with the rich solution, and the second part of the lean solution is used for heating cold fluid in other processes. The temperature of the second part of the lean liquid can reach 353-403K, and is equal to the temperature of the lean liquid of the reboiler in the highest case. The temperature is obviously higher than the temperature of the lean solution of about 333K after the heat exchange of the lean and rich solution in the prior art. The specific temperature is, of course, dependent on the flow rates, temperatures, split ratios, heat transfer areas and flow path designs of the lean and rich solutions. The invention divides the high-temperature barren solution flowing out from the bottom of the desorption tower, and the high-temperature barren solution is respectively used for exchanging heat with the internal liquid such as pregnant solution and the like and heating the low-temperature fluid in other processes, so that the comprehensive energy consumption for capturing and separating the acid gases such as carbon dioxide and the like by an absorption method can be reduced by about 5-10%.
Drawings
FIG. 1 is a flow diagram of the capture of acid gases (pre-heat exchange lean liquid split) in a gas mixture using a solvent absorption process in a preferred embodiment of the present invention;
FIG. 2 is a flow diagram of the capture of acid gases (lean liquid split in heat exchange) in a gas mixture using solvent absorption in another preferred embodiment of the present invention;
FIG. 3 is a flow diagram of the capture of acid gases (lean liquid split in a complex heat exchanger) in a gas mixture using solvent absorption in another preferred embodiment of the invention.
Detailed Description
The following examples are given to further illustrate the embodiments of the present invention. The following examples are provided to illustrate the present invention, but are not intended to limit the scope of the present invention.
Example 1
One strand of CO with the concentration of 13.1 percent2、73.5％N2、8.0％O2And 5.4% H2O, 25% ethanolamine (MEA), CO at a flow rate of 4310 standard cubic meters per hour and a flow rate of 20.5 cubic meters per hour are neutralized in an absorption tower2Contacting with aqueous solution of MEA with mole ratio of 0.28, CO2The absorption was 90%. The logarithmic mean temperature difference of the lean-rich liquid heat exchanger is 7.5K, the temperature of the lean liquid after heat exchange is 328.85K, the bottom pressure of the desorption tower is 1.6bar, and the temperature of the lean liquid at the bottom of the desorption tower is 385.75K. In a conventional process having an absorption column, a desorption column, a lean-rich heat exchanger and a reboiler, the energy consumption for heating in the reboiler is 3.86 GJ/ton CO2。
On the basis of a conventional process, a lean solution shunting technology is added, the process of the figure 1 is adopted, a heat exchanger E6 is added for heat exchange of shunted high-temperature lean solution and external cold fluid, the shunting proportion L3/L1 of the lean solution at the bottom of the desorption tower is 20% (generally 15% -35%, and can be optimized according to process conditions), the temperature is 385.75K, and the energy consumption of a reboiler is 4.05 GJ/ton CO2The heat available for heating other cold fluids (385.75K-328.85K) was 0.87 GJ/ton CO2. The ratio of the steam power generation efficiency of the average temperature 357.3K in the temperature range of 385.75K-328.85K to the steam power generation efficiency of 393.15K is 0.635, and the overall energy consumption is 4.05-0.87 × 0.635-3.5 GJ/ton CO23.86 GJ/ton CO of the original conventional process2Compared with the energy-saving mode, the energy is saved by 9.4 percent.
Example 2
The method adopts a flow of increasing the cold in the absorption tower and the flow of rich liquid diversion on the basis of the conventional flow in the same embodiment 1, and a share of CO with the concentration of 13.1 percent2、73.5％N2、8.0％O2And 5.4% H2O, 25% ethanolamine (MEA), CO at a flow rate of 4310 standard cubic meters per hour and at a flow rate of 18.7 cubic meters per hour are neutralized in an absorption tower2And an aqueous solution having a molar ratio of MEA of 0.28. Cooling the liquid in the middle of the absorption tower by adopting an absorption tower internal cooling technology, and then sending the cooled liquid back to the absorption tower, wherein the cold quantity is 0.485 GJ/ton CO2。CO2The absorption was 90%. Meanwhile, rich liquor is used for shunting, a first part of shunted rich liquor directly enters the top of the desorption tower, and a second part of shunted rich liquor enters the upper part of the desorption tower after passing through the lean and rich liquor heat exchanger. The proportion of the first part of rich solution in the whole rich solution is 25%, the logarithmic mean temperature difference of the lean rich solution heat exchanger is 7.5K, the temperature of the lean solution after heat exchange is 333.45K, the bottom pressure of the desorption tower is 1.6bar, the temperature of the lean solution at the bottom of the desorption tower is 385.75K, and the energy consumption for heating in a reboiler is 3.49 GJ/ton CO2。
On the basis of the flow, a lean solution shunting technology in heat exchange is added, two heat exchangers (such as E7 and E6 in figure 2) are added, the added E7 is used for heat exchange of high-temperature lean solution and rich solution, the added heat exchanger E6 is used for heat exchange of shunted lean solution and external cold fluid, the shunting ratio L3/L1 of the lean solution at the bottom of the desorption tower is 25%, the temperature is 373.45K, and the energy consumption of a reboiler is 3.55 GJ/ton CO2The additional heat (temperature range 373.45K-333.45K) for heating other cold fluids is 0.69 GJ/ton CO 2. The ratio 0.0.592 of the steam power generation efficiency of the average temperature 353.45K of the temperature interval of 373.45K-333.45K to the steam power generation efficiency of 393.15K, and the overall energy consumption is 3.55-0.69 x 0.592-3.14 GJ/ton CO2And the energy consumption of the process originally adopting the inner cooling of the absorption tower and the rich liquid flow splitting is 3.49 GJ/ton CO2Compared with the energy-saving mode, the energy is saved by 10.0 percent.
Example 3
Adopting the flow of rich solution shunting and semi-lean solution shunting, and one strand of CO with the concentration of 15.0 percent2、72.0％N2、8.0％O2And 5.0% H2O, flow rate 4784 standard cubic meters per hour, 20% 2-amino-2-methyl-1-propanol (AMP) + 10% ethanolamine (MEA), CO in the absorber and entering at the top of the column at a flow rate of 14.54 cubic meters per hour2And organic amine AMP + MEA at a molar ratio of 0.20, and a mid-column feed flow rate of 2.67 cubic meters per hour of a semi-lean solution, CO2The absorption was 85%. And simultaneously adopting rich liquor shunting and semi-lean liquor shunting. The first part of the rich liquid shunting directly enters the top of the desorption tower, and the second part enters the upper part of the desorption tower after passing through the lean rich liquid heat exchanger. The split ratio of the first part of the rich solution to the whole rich solution is 25%. The extraction proportion of the semi-barren solution is 15%. And exchanging heat between partial semi-barren liquor extracted from the middle part of the desorption tower and the split rich liquor, wherein the logarithmic mean temperature difference of the heat exchangers of the rich liquor and the semi-barren liquor is 9.3K. The logarithmic mean temperature difference of the lean-rich liquid heat exchanger is 8.0K, the temperature of the lean liquid after heat exchange is 332.85K, and the logarithmic mean temperature difference of the second lean-rich liquid heat exchanger is 5.0K. The bottom pressure of the desorption tower is 1.6bar, the temperature of the barren solution at the bottom of the desorption tower is 386.15K, and the energy consumption for heating in a reboiler is 2.81 GJ/ton CO2。
On the basis of the flow, a lean solution shunting technology in heat exchange is adopted, two heat exchangers (E7 and E6 in figure 2) are added, the added E7 is used for heat exchange of high-temperature lean solution and rich solution, the added heat exchanger E6 is used for heat exchange of shunted lean solution and external cold fluid, the shunting ratio L3/L1 of the lean solution at the bottom of the desorption tower is 25%, the temperature is 377.65K, and the energy consumption of a reboiler is 2.97 GJ/ton CO2The heat quantity (the temperature range is 377.65K-332.85K) added for heating other cold fluid is 0.61 GJ/ton CO2. The ratio of the steam power generation efficiency of the average temperature 355.25K in the temperature range of 377.65K-332.85K to the steam power generation efficiency of 393.15K is 0.612, and the overall energy consumption is 2.97-0.61 x 0.612-2.60 GJ/ton CO2And the process energy consumption adopting rich liquid diversion and semi-lean liquid diversion is 2.81 GJ/ton CO2Compared with the energy-saving method, the energy is saved by 7.5 percent.
Example 4
The flow of cooling in the absorption tower, flow splitting of rich liquid and flash compression of lean liquid are adopted, and the method for cooling in the absorption tower and flow splitting of the rich liquid is the same as that of the embodiment 2 and the embodiment 3. One strand of CO with the concentration of 13.1 percent2、73.5％N2、8.0％O2And 5.4% H2O, 25% ethanolamine and CO with a flow rate of 4310 standard cubic meters per hour and a flow rate of 18.7 cubic meters per hour are neutralized in an absorption tower2Contacting with aqueous solution of ethanolamine with a molar ratio of 0.28, and cooling in the absorption towerThe amount of CO is 0.485 GJ/ton CO2，CO2The absorption was 90%. Meanwhile, rich liquor is used for shunting, the shunting proportion is 15%, the logarithmic mean temperature difference of the lean-rich liquor heat exchanger is 7.5K, and the temperature of the lean liquor after heat exchange is 328.15K. The pressure of the bottom of the desorption tower is 1.6bar, the temperature of the barren solution at the bottom of the desorption tower is 385.55K, the barren solution flowing out of the bottom of the desorption tower directly enters a barren solution flash tank, the flash pressure is 1.0bar, the compression pressure of flash steam is 1.6bar, and the liquid after flash evaporation enters a barren solution heat exchanger to exchange heat with rich solution. The energy consumption for heating in the reboiler was 2.39 GJ/ton CO2。
On the basis of the above process, the barren solution after barren solution flash evaporation adopts a flow splitting technology. The first part is continuously sent into a lean-rich liquid heat exchanger to exchange heat with rich liquid, and the second part is exchanged heat with external cold fluid (adding a heat exchanger, such as E6 in figure 1). The proportion (split ratio) of the second part of the lean solution to all the lean solutions is 20%, the temperature is 373.35K, and the energy consumption of a reboiler is 2.52 GJ/ton CO2The heat quantity (the temperature range is 373.35K-328.15K) added for heating other cold fluid is 0.48 GJ/ton CO2. The ratio of the steam power generation efficiency of the average temperature 350.75K in the temperature range of 373.35K-328.15K to the steam power generation efficiency of 393.15K is 0.561, and the overall energy consumption is 2.52-0.48 × 0.561-2.25 GJ/ton CO2And the process energy consumption only adopting the inner cooling of the absorption tower, the flow of rich solution diversion and the flash evaporation compression of the barren solution is 2.39 GJ/ton CO2Compared with the energy-saving method, the energy is saved by 5.8 percent.
Finally, the method of the present invention is only a preferred embodiment and is not intended to limit the scope of the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. A method for capturing acid gases in a gas mixture using solvent absorption, comprising the steps of:
and shunting the high-temperature barren solution flowing out of the bottom of the desorption tower in heat exchange, namely firstly carrying out partial heat exchange on the high-temperature barren solution and the internal liquid in the solvent absorption process and then shunting, wherein one part of the high-temperature barren solution is used for carrying out secondary heat exchange with the internal liquid in the solvent absorption process, and the other part of the high-temperature barren solution is used for carrying out heat exchange with a cold fluid outside the solvent absorption process.
2. The method according to claim 1, characterized in that it comprises in particular the steps of:
and exchanging heat between the high-temperature lean solution and at least one strand of internal liquid in the solvent absorption process and at least one strand of cold fluid outside the solvent absorption process in a multi-strand heat exchanger.
3. The method as claimed in claim 1 or 2, further comprising cooling the heat-exchanged lean solution further and feeding the cooled lean solution into an absorption tower corresponding to the desorption tower for circularly absorbing acid gas.
4. The method according to claim 1 or 2, wherein the desorption tower further comprises a reboiler, and the high-temperature lean solution flows out of the bottom of the reboiler.
5. An apparatus for capturing acid gases in a gas mixture using solvent absorption, comprising: the absorption tower and the desorption tower are provided with a high-temperature barren solution output pipeline at the bottom, and the high-temperature barren solution output pipeline is used for enabling the high-temperature barren solution to exchange heat with the internal liquid in the solvent absorption method process, then is divided and is used for respectively exchanging heat with the internal liquid in the solvent absorption method process and the cold fluid outside the solvent absorption method process.
6. The apparatus of claim 5, further comprising:
an internal liquid transfer pipe connected to the absorption column for transferring the internal liquid during the solvent absorption process;
a cold fluid transfer line for transferring cold fluid outside the solvent absorption process;
after the high-temperature lean solution in the high-temperature lean solution output pipeline is shunted, heat exchange is respectively carried out between the high-temperature lean solution and the internal liquid in the internal liquid conveying pipeline and between the high-temperature lean solution and the cold fluid in the cold fluid conveying pipeline through a heat exchanger;
the barren liquor conveying pipeline is connected with the absorption tower and is used for conveying the barren liquor subjected to heat exchange to the absorption tower;
and the internal liquid conveying pipeline is connected with the desorption tower and is used for conveying the internal liquid after heat exchange to the desorption tower.
7. The apparatus of claim 5 or 6, further comprising:
the heat exchanger is arranged close to the joint of the high-temperature barren solution output pipeline and the desorption tower and is used for performing partial heat exchange on the high-temperature barren solution and internal liquid and then shunting the high-temperature barren solution.
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