CN103521053B - Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for - Google Patents

Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for Download PDF

Info

Publication number
CN103521053B
CN103521053B CN201310449986.6A CN201310449986A CN103521053B CN 103521053 B CN103521053 B CN 103521053B CN 201310449986 A CN201310449986 A CN 201310449986A CN 103521053 B CN103521053 B CN 103521053B
Authority
CN
China
Prior art keywords
solution
outlet
rich
water
hollow fiber
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201310449986.6A
Other languages
Chinese (zh)
Other versions
CN103521053A (en
Inventor
晏水平
贺清尧
艾平
王媛媛
徐红梅
张衍林
樊啟洲
袁巧霞
蔡凯
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Huazhong Agricultural University
Original Assignee
Huazhong Agricultural University
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Huazhong Agricultural University filed Critical Huazhong Agricultural University
Priority to CN201310449986.6A priority Critical patent/CN103521053B/en
Publication of CN103521053A publication Critical patent/CN103521053A/en
Application granted granted Critical
Publication of CN103521053B publication Critical patent/CN103521053B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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
    • 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
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals

Abstract

Designed by the present invention a kind of based on concentration of absorbing conversion gas in CO 2chemical absorbing System and method for, CO in gas of the present invention 2at CO 2absorption stage is absorbed by chemical absorbent and forms initial rich CO 2absorbent solution, initial rich CO 2absorbent solution was carried out concentrating and separating by rich solution concentration systems before hot recycling, obtained mutually concentrated and dilute phase, concentrated and comprised absorbent solute and entrained CO mutually 2, and only regenerate concentrated phase at regeneration stage, improve the CO of rich solution 2equilibrium partial pressure, intensifying regenerating mass transfer force, reduce the water heat of evaporation demand in regenerative process, also the rich solution flow entered in regenerating unit can be reduced, thus the rich solution intensification latent demand in reduction regenerative process, reach from these two aspects and reduce rich solution regeneration energy consumption demand, solve traditional chemical absorption process technique high energy consumption problem.

Description

Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for
Technical field
The present invention relates to CO in mist 2separation process technique field, refers to a kind of based on CO in the gas of concentration of absorbing conversion particularly 2chemical absorbing System and method for.
Technical background
Based on CO in the coal-fired flue-gas of chemical absorbing principle, biogas and rubbish landfill gas 2absorption techniques be the main flow CO in current above-mentioned field 2one of isolation technics, but the absorbent adopted in traditional chemical absorption process technique is difficult to meet high CO simultaneously 2absorption reaction speed and low regeneration energy consumption requirement, thus for meeting CO 2removal efficiency requirement, as the high CO of selection 2during the absorbent of absorption rate, with CO 2react the carbaminate regeneration difficulty formed large, regeneration energy consumption is high, and investment is large, CO 2separation costs is high.And when selecting the absorbent of easily regeneration, absorbent and CO 2reaction rate is low, causes absorbent solution demand large, the high and CO of equipment investment 2separation costs is high, and system cloud gray model is less economical.Classical CO 2in chemical absorption method technique, CO 2absorption stage and rich CO 2the concentration of absorbing substantially constant of absorbent solution (abbreviation rich solution) regeneration stage is constant, and classical chemical absorption method technique effectively can not utilize CO 2the CO of chemical absorbent under variable concentrations state 2absorb and regeneration comprehensive advantage, thus the concentration of absorbent is selected to have certain restriction, and as in typical monoethanolamine chemical absorption process, its mass concentration is generally no more than 30%.Due to the restriction of concentration, cause the CO of the bigger than normal and rich solution of the liquid inventory entered in regenerator in the rich solution thermal regeneration stage 2equilibrium partial pressure is less than normal, in order to reach desirable regeneration effect, needs higher regeneration condition, thus causes regeneration energy consumption to remain high.In typical monoethanolamine chemical absorption process, in regenerator, regeneration pressure and temperature generally need to reach about 2.1bar and 120 DEG C, and its typical heat regeneration energy consumption can up to 4GJ/t CO 2, more than 80% of whole process energy consumption can be accounted for.Although Many researchers is attempted screening or developed brand-new absorbent to reduce regeneration energy consumption, only limited by the innovation of the absorbent potential that may lower consumption.Therefore, reducing amplitude to obtain larger regeneration energy consumption, the innovation of technique must be coordinated, be thus necessary to develop new CO 2absorption technique.
Summary of the invention
Object of the present invention is exactly to provide a kind of based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for, this system and method can significantly improve CO in gas 2assimilation effect, and significantly can reduce CO 2regeneration energy consumption.
For realizing this object, designed by the present invention a kind of based on concentration of absorbing conversion gas in CO 2chemical absorbing system, comprises CO 2absorption equipment, separator, CO 2reclaim equiment, lean pump, input and CO 2the rich solution pump that the liquid outlet of absorption equipment connects, output and CO 2the condenser of the absorbing liquid input port connection of absorption equipment, described CO 2absorption equipment is also provided with top exhaust outlet and air inlet, it is characterized in that: it also comprises heater, hollow fiber membrane contactors group, water pump, poor rich liquid heat exchanger and mixing arrangement, wherein, rich solution delivery side of pump connects the tube-side inlet of hollow fiber membrane contactors group by heater, the shell-side outlet of hollow fiber membrane contactors group connects the low concentration salt solution entrance of separator, the Separation of Water delivery outlet of separator connects the dilution water entrance of mixing arrangement by water pump, the high concentration salt solutions outlet of separator connects the shell side inlet of hollow fiber membrane contactors group, the tube side outlet of hollow fiber membrane contactors group connects the cry-fluid inlet of poor rich liquid heat exchanger, the cryogenic fluid outlet of poor rich liquid heat exchanger connects CO 2the rich solution input port of reclaim equiment, CO 2the lean solution delivery outlet of reclaim equiment connects the high temperature fluid import of poor rich liquid heat exchanger, and the high temperature fluid outlet of poor rich liquid heat exchanger connects the high concentration lean solution entrance of mixing arrangement by lean pump, and the mixed solution outlet of mixing arrangement connects condenser,
Described CO 2reclaim equiment is also provided with CO 2exhaust outlet.
In technique scheme, in the pipeline between the tube-side inlet of described heater and hollow fiber membrane contactors group, be provided with flowmeter and thermometer; Flowmeter and thermometer is provided with in pipeline between the high concentration salt solutions outlet of described separator and the shell side inlet of hollow fiber membrane contactors group; Flowmeter and thermometer is provided with in pipeline between the dilution water entrance of described water pump and mixing arrangement; Flowmeter and thermometer is provided with in pipeline between the high concentration lean solution entrance of described lean pump and mixing arrangement; Flowmeter and thermometer is provided with in pipeline between the mixed solution outlet of described mixing arrangement and condenser; Be provided with water absorbing agent concentration sensor in the shell side of described hollow fiber membrane contactors group, in the mixed solution outlet of described mixing arrangement, be provided with concentration of absorbing sensor.
In technique scheme, described mixing arrangement also offers replenisher entrance.
In technique scheme, between the shell-side outlet of hollow fiber membrane contactors group and the low concentration salt solution entrance of separator, be provided with salting liquid reflux pump.
A kind of utilize above-mentioned based on concentration of absorbing conversion gas in CO 2cO in the gas of chemical absorbing system 2chemical absorption process, is characterized in that, it comprises the steps:
Step 1: at CO 2cO is added in absorption equipment 2chemical absorbent;
Step 2: CO to be separated 2gas enter CO by air inlet 2absorption equipment, and and CO 2cO in absorption equipment 2chemical absorbent sends reaction, generates initial rich CO 2solution, initial rich CO 2solution is by CO 2the liquid outlet of absorption equipment enters rich solution pump;
Step 3: initial rich CO 2solution enters heater via rich solution pump, the tube-side inlet of hollow fiber membrane contactors group is entered after being heated to 60 ~ 80 DEG C in the heater, and flow in the tube side of hollow fiber membrane contactors group and stop 150 ~ 180S, simultaneously, flow in hollow fiber membrane contactors group shell side water absorbing agent, the rear initial rich CO of the heating in tube side 2water absorbing agent in solution and shell side forms reverse movement, initial rich CO after heating 2water in solution is initial rich CO after the heating 2under the driving of the steam partial pressure of solution and the difference of water absorbing agent steam partial pressure, entered into the water absorbing agent of shell side as water vapor from the tube side of hollow fiber membrane contactors group by fenestra, thus make the rear initial rich CO of heating 2solution obtains concentrated and obtains absorbent solute and entrained CO 2mass concentration scope be 50% ~ 60% concentrated phase, the concentrated cry-fluid inlet being entered poor rich liquid heat exchanger by tube side outlet; And the water absorbing agent after water suction is being entered separator by shell-side outlet, and absorbed moisture is discharged through heating and/or reduced pressure treatment in separator, this moisture discharged is dilute phase, dilute phase is exported by Separation of Water delivery outlet, and be transported in mixing arrangement via water pump, discharge the water absorbing agent after moisture in separator and export output by high concentration salt solutions, enter hollow fiber membrane contactors group Inner eycle and use;
Step 4: described the concentrated of hollow fiber membrane contactors tube side outlet enters poor rich liquid heat exchanger and CO mutually 2the lean solution that reclaim equiment obtains carries out heat exchange intensification, and enters CO by cryogenic fluid outlet 2reclaim equiment regenerates, CO 2regeneration temperature in reclaim equiment is 80 ~ 120 DEG C, and regenerates CO 2, then the CO born 2by CO 2the CO of reclaim equiment 2exhaust outlet enters CO 2in collecting device, the absorbent Solute mass concentration range of the lean solution obtained after regeneration is 50% ~ 60%, and the lean solution obtained after regeneration is by CO 2the lean solution delivery outlet of reclaim equiment enters poor rich liquid heat exchanger by high temperature fluid import and carries out heat exchange cooling mutually with concentrated, and exports input lean pump by high temperature fluid, is transported in mixing arrangement through lean pump;
Step 5: the lean solution in mixing arrangement after regeneration is fully mixed by stirring with dilute phase, controls the lean solution mass concentration after diluting by the flow controlling the lean solution after regenerating and dilute phase, thus makes lean solution concentration return to initial CO 2the state of chemical absorbent, then enters condenser condenses by mixed solution outlet and return CO after the temperature of specifying 2again CO is carried out in absorption equipment 2absorb.
In described step 5, return to initial CO 2the lean solution of chemical absorbent state enters condenser condenses and return CO after 30 ~ 40 DEG C 2again CO is carried out in absorption equipment 2absorb.
In described step 3, in hollow fiber membrane contactors group shell side, the water absorbing agent of flowing is not for absorb CO 2water imbibition salt, describedly do not absorb CO 2water imbibition salt be calcium chloride or lithium chloride or lithium bromide.
In described step 5, the lean solution mass concentration after diluting is controlled by the flow controlling the lean solution after regenerating and dilute phase, concentration of absorbing sensor simultaneously in conjunction with mixed solution outlet detects the rear lean solution mass concentration state of dilution, when determining the loss having absorbent solute or water in whole system, through the replenisher entrance of mixing arrangement from the corresponding pure absorbent of external complement or water.
In described step 2, CO to be separated 2gas be biogas, flue gas or rubbish landfill gas, CO 2chemical absorbent is ethanolamine solutions, and the monoethanolamine mass concentration of this ethanolamine solutions is 30%.
In described step 3, concentrate and comprise absorbent solute and entrained CO mutually 2.
Beneficial effect of the present invention is:
1, in the present invention, only regeneration has the rich solution of high concentration, and entering rich solution mass flow in reclaim equiment will lower than traditional handicraft, and CO in rich solution in regenerative process 2equilibrium partial pressure is higher, and mass transfer force is stronger, thus under traditional hot recycling condition, compares the regeneration of low concentration rich solution, unit CO 2regeneration energy consumption can reduce by 30% ~ 40%.
2, the present invention due to absorbent rich solution mass concentration in regenerative process higher, mass transfer force is stronger, thus regeneration temperature can Selection radio traditional chemical absorption process technique lower (less than 100 DEG C), thus this partial heat needed for rich solution regeneration can adopt waste heat or other low-grade energy, therefore has the potential reducing regeneration energy consumption further.
3, the present invention is owing to adopting the lean solution of relatively low concentration at absorber portion, and only regeneration high concentration rich solution also selects lower regeneration temperature, and initial rich solution adopts the concentrating and separating of lower temperature simultaneously, therefore can have good CO simultaneously 2the volatilization of assimilation effect, lower regeneration energy consumption and lower absorbent is lost with high temperature degradation.
4, the present invention is applicable to isolate CO from inert gas (not with alkali reaction) system 2, as separation of C O in the gases such as flue gas, biogas and rubbish landfill gas 2.
Accompanying drawing explanation
Fig. 1 be the present invention is based on concentration of absorbing conversion gas in CO 2the structural representation of chemical absorbing system.
Wherein, 1-CO 2absorption equipment, 1.1-liquid outlet, 1.2-absorbing liquid input port, 1.3-top exhaust outlet, 1.4-air inlet, 2-rich solution pump, 3-heater, 4-hollow fiber membrane contactors group, 4.1-tube-side inlet, 4.2-tube side exports, 4.3-shell side inlet, 4.4-shell-side outlet, 5-separator, 5.1-low concentration salt solution entrance, 5.2-Separation of Water delivery outlet, 5.3-high concentration salt solutions exports, 6-water pump, 7-poor rich liquid heat exchanger, 7.1-cry-fluid inlet, 7.2-cryogenic fluid outlet, the import of 7.3-high temperature fluid, 7.4-high temperature fluid exports, 8-CO 2reclaim equiment, 8.1-rich solution input port, 8.2-lean solution delivery outlet, 8.3-CO 2the outlet of exhaust outlet, 9-lean pump, 10-mixing arrangement, 10.1-dilution water entrance, 10.2-high concentration lean solution entrance, 10.3-mixed solution, 10.4-replenisher entrance, 11-condenser, 12-flowmeter, 13-thermometer, 14-water absorbing agent concentration sensor, 15-salting liquid reflux pump, 16-concentration of absorbing sensor
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail:
As shown in Figure 1 based on concentration of absorbing conversion gas in CO 2chemical absorbing system, comprises CO 2absorption equipment 1, separator 5, CO 2reclaim equiment 8, lean pump 9, input and CO 2the rich solution pump 2 that the liquid outlet 1.1 of absorption equipment 1 connects, output and CO 2the condenser 11, CO of absorbing liquid input port 1.2 connection of absorption equipment 1 2absorption equipment 1 is also provided with top exhaust outlet 1.3 and air inlet 1.4, it also comprises heater 3, hollow fiber membrane contactors group 4, water pump 6, poor rich liquid heat exchanger 7 and mixing arrangement 10, wherein, the output of rich solution pump 2 connects the tube-side inlet 4.1 of hollow fiber membrane contactors group 4 by heater 3, the shell-side outlet 4.4 of hollow fiber membrane contactors group 4 connects the low concentration salt solution entrance 5.1 of separator 5, the Separation of Water delivery outlet 5.2 of separator 5 connects the dilution water entrance 10.1 of mixing arrangement 10 by water pump 6, the high concentration salt solutions outlet 5.3 of separator 5 connects the shell side inlet 4.3 of hollow fiber membrane contactors group 4, the tube side outlet 4.2 of hollow fiber membrane contactors group 4 connects the cry-fluid inlet 7.1 of poor rich liquid heat exchanger 7, the cryogenic fluid outlet 7.2 of poor rich liquid heat exchanger 7 connects CO 2the rich solution input port 8.1, CO of reclaim equiment 8 2the lean solution delivery outlet 8.2 of reclaim equiment 8 connects the high temperature fluid import 7.3 of poor rich liquid heat exchanger 7, the high temperature fluid outlet 7.4 of poor rich liquid heat exchanger 7 connects the high concentration lean solution entrance 10.2 of mixing arrangement 10 by lean pump 9, the mixed solution outlet 10.3 of mixing arrangement 10 connects condenser 11,
Described CO 2reclaim equiment 8 is also provided with CO 2exhaust outlet 8.3.
In technique scheme, in the pipeline between described heater 3 and the tube-side inlet 4.1 of hollow fiber membrane contactors group 4, be provided with flowmeter 12 and thermometer 13; Flowmeter 12 and thermometer 13 is provided with in pipeline between the high concentration salt solutions outlet 5.3 of described separator 5 and the shell side inlet 4.3 of hollow fiber membrane contactors group 4; Flowmeter 12 and thermometer 13 is provided with in pipeline between described water pump 6 and the dilution water entrance 10.1 of mixing arrangement 10; Flowmeter 12 and thermometer 13 is provided with in pipeline between the high concentration lean solution entrance 10.2 of described lean pump 9 and mixing arrangement 10; Flowmeter 12 and thermometer 13 is provided with in pipeline between the mixed solution outlet 10.3 of described mixing arrangement 10 and condenser 11, be provided with water absorbing agent concentration sensor 14 in the shell side of described hollow fiber membrane contactors group 4, in the mixed solution outlet 10.3 of described mixing arrangement 10, be provided with concentration of absorbing sensor 16.
In technique scheme, said temperature meter 13, flowmeter 12 and each concentration sensor are all for measuring the relevant parameter of solution everywhere, determine whether native system runs in normal scope, there is deficiency or exceed relevant parameter, will to heater, separators etc. regulate, and ensure the normal work of system.
In technique scheme, mixing arrangement 10 also offers replenisher entrance 10.4.
In technique scheme, between the shell-side outlet 4.4 of hollow fiber membrane contactors group 4 and the low concentration salt solution entrance 5.1 of separator 5, be provided with salting liquid reflux pump 15.
A kind of utilize above-mentioned based on concentration of absorbing conversion gas in CO 2cO in the gas of chemical absorbing system 2chemical absorption process, in the method, CO in gas 2at CO 2absorption stage is absorbed by chemical absorbent and forms initial rich CO 2absorbent solution, and be with traditional handicraft difference, initial rich CO 2absorbent solution first will be carried out concentrating and separating by rich solution concentration systems (comprising hollow fiber membrane contactors group 4 and separator 5) before hot recycling, obtained mutually concentrated and dilute phase, concentrated mutually and contained the absorbent solute of the overwhelming majority and entrained CO 2, dilute phase is mainly water, and only regenerates concentrated phase at regeneration stage, improves the CO of rich solution 2equilibrium partial pressure, intensifying regenerating mass transfer force, reduce the water heat of evaporation demand in regenerative process, also can reduce the rich solution flow entered in regenerating unit simultaneously, thus the rich solution intensification latent demand in reduction regenerative process, reach from these two aspects and reduce rich solution regeneration energy consumption demand, solve the problem of traditional chemical absorption process technique high energy consumption.Meanwhile, to the poor CO obtained after regeneration 2absorbent solution (abbreviation lean solution) adopts initial rich CO 2the dilute phase obtained in absorbent solution concentrating and separating process is diluted, and makes concentration of absorbing return to CO 2the state of absorption stage, does not affect CO 2the etching characteristic of absorption efficiency and absorbent.
The present invention comprises the steps: specifically
Step 1: at CO 2cO is added in absorption equipment 1 2chemical absorbent (as monoethanolamine absorbent);
Step 2: CO to be separated 2gas enter CO by air inlet 1.4 2absorption equipment 1, and and CO 2cO in absorption equipment 1 2chemical absorbent sends reaction, generates initial rich CO 2solution, initial rich CO 2solution is by CO 2the liquid outlet 1.1 of absorption equipment 1 enters rich solution pump 2;
Step 3: initial rich CO 2solution enters heater 3 via rich solution pump 2, and in heater 3, being heated to 60 ~ 80 DEG C, (actual temp can by CO 2chemical absorbent and hollow fiber membrane contactors group 4 actual conditions are determined, for CO 2after reaction, the main absorbent system forming bicarbonate, can select lower critical temperature, and for CO 2after reaction, the main absorbent system generating carbaminate product can adopt upper critical point temperature) after enter the tube-side inlet 4.1 of hollow fiber membrane contactors group 4, and to flow in the tube side of hollow fiber membrane contactors group 4 and the concentration stopping 150 ~ 180S(high concentration rich solution determined primarily of the time of staying of initial rich solution in hollow fiber membrane contactors (4)), simultaneously, flow in hollow fiber membrane contactors group 4 shell side water absorbing agent, the rear initial rich CO of the heating in tube side 2water absorbing agent in solution and shell side forms reverse movement, initial rich CO after heating 2water in solution is initial rich CO after the heating 2under the driving of the steam partial pressure of solution and the difference of water absorbing agent steam partial pressure, entered into the water absorbing agent of shell side as water vapor from the tube side of hollow fiber membrane contactors group 4 by fenestra, thus make the rear initial rich CO of heating 2solution obtains concentrated and obtains absorbent solute and entrained CO 2mass concentration scope be 50% ~ 60% concentrated phase, the concentrated cry-fluid inlet 7.1 being entered poor rich liquid heat exchanger 7 by tube side outlet 4.2; And the water absorbing agent after water suction is being entered separator 5 by shell-side outlet, and absorbed moisture is discharged through heating and/or reduced pressure treatment in separator 5, this moisture discharged is dilute phase, dilute phase is exported by Separation of Water delivery outlet 5.2, and be transported in mixing arrangement 10 via water pump 6, discharge the water absorbing agent after moisture in separator 5 and export 5.3 outputs by high concentration salt solutions, enter hollow fiber membrane contactors group 4 Inner eycle and use;
Step 4: described the concentrated of hollow fiber membrane contactors 4 tube side outlet 4.2 enters poor rich liquid heat exchanger 7 and CO mutually 2lean solution (the CO that reclaim equiment 8 obtains 2by the CO in rich solution in reclaim equiment 8 2absorbing liquid after bearing again, containing less CO2.This absorbing liquid is lean solution) carry out heat exchange intensification, and enter CO by cryogenic fluid outlet 7.2 2reclaim equiment 8 regenerates, CO 2regeneration temperature in reclaim equiment 8 is 80 ~ 120 DEG C (regeneration temperature here can be selected from 80 ~ 120 DEG C according to the difference of regeneration), and regenerates CO 2, then the CO born 2by CO 2the CO of reclaim equiment 8 2exhaust outlet 8.3 enters CO 2in collecting device so that other aspects utilize, and the absorbent Solute mass concentration range of the lean solution obtained after regeneration is 50% ~ 60%(CO 2lean solution mass fraction out and above concentrated consistent in reclaim equiment 8), the lean solution obtained after regeneration is by CO 2the lean solution delivery outlet 8.2 of reclaim equiment 8 enters poor rich liquid heat exchanger 7 by high temperature fluid import 7.3 and carries out heat exchange cooling mutually with concentrated, and exports 7.4 input lean pumps 9 by high temperature fluid, is transported in mixing arrangement 10 through lean pump 9;
Step 5: the lean solution in mixing arrangement 10 after regeneration is fully mixed by stirring with dilute phase, controls the lean solution mass concentration after diluting by the flow controlling the lean solution after regenerating and dilute phase, thus makes lean solution concentration return to initial CO 2the state of chemical absorbent, is then entered after condenser 11 condenses to the temperature of specifying by mixed solution outlet 10.3 and returns CO 2again CO is carried out in absorption equipment 1 2absorb, namely complete the technological process of " absorption-concentrated-regeneration-dilution-absorb ".
In the step 5 of technique scheme, return to initial CO 2the lean solution of chemical absorbent state enters after condenser 11 condenses to 30 ~ 40 DEG C and returns CO 2again CO is carried out in absorption equipment 1 2absorb.
In the step 3 of technique scheme, in hollow fiber membrane contactors group 4 shell side, the water absorbing agent of flowing is not for absorb CO 2water imbibition salt, describedly do not absorb CO 2water imbibition salt be calcium chloride or lithium chloride or lithium bromide.
In the step 5 of technique scheme, the lean solution mass concentration after diluting is controlled by the flow controlling the lean solution after regenerating and dilute phase, concentration of absorbing sensor 16 simultaneously in conjunction with mixed solution outlet 10.3 detects the rear lean solution mass concentration state of dilution, when determining the loss having absorbent solute or water in whole system, through the replenisher entrance 10.4 of mixing arrangement 10 from the corresponding pure absorbent of external complement or water.
Whether whether in system, whether absorbent solute loses, and is obtained by sampling detection, detect absorbent and react with other impurity, or be decomposed.In system, whether water loses the concentration mainly detecting solution, and concentration uprises the loss illustrating and have water.The loss of water may be had in concentration process, in absorption equipment and reclaim equiment, also have a small amount of water loss.
In the step 2 of technique scheme, CO to be separated 2gas be biogas, flue gas, rubbish landfill gas or natural gas etc., CO 2chemical absorbent is ethanolamine solutions (absorbent of this technique can be not only ethanolamine solutions, also can be other non-volatile absorbent, as amidates, alcamines absorbent etc.), and the monoethanolamine mass concentration of this ethanolamine solutions is 30%.
In the step 3 of technique scheme, concentrate and comprise absorbent solute and entrained CO mutually 2.
In technique scheme, all pipe-line systems and hollow fiber membrane contactors group 4 outer wall all wrap up insulation material, to reduce initial rich solution at the operating thermal loss of pipeline, ensure the constant of the temperature of initial rich solution when arriving hollow fiber membrane contactors group 4 entrance, meanwhile, ensure that system heat loss rate is within 5%.
In technique scheme, CO 2absorption equipment 1 and CO 2the structure of reclaim equiment 8 and kind can not be limit, and both can adopt traditional filler tower structure, also can use the structures such as novel hollow fiber membrane contactors.
In technique scheme, hollow fiber membrane contactors group 4 is encapsulated by hydrophobic hollow fiber film and forms.
In technique scheme, for CO in the present invention 2the chemical absorbent absorbed is the absorbent that can meet renewable, the low volatility recycled.
The content that description is not described in detail belongs to the known prior art of professional and technical personnel in the field.

Claims (4)

1. one kind based on concentration of absorbing conversion gas in CO 2chemical absorbing system, comprises CO 2absorption equipment (1), separator (5), CO 2reclaim equiment (8), lean pump (9), input and CO 2rich solution pump (2), output and CO that the liquid outlet (1.1) of absorption equipment (1) connects 2the condenser (11) that the absorbing liquid input port (1.2) of absorption equipment (1) connects, described CO 2absorption equipment (1) is also provided with top exhaust outlet (1.3) and air inlet (1.4), it is characterized in that: it also comprises heater (3), hollow fiber membrane contactors group (4), water pump (6), poor rich liquid heat exchanger (7) and mixing arrangement (10), wherein, the output of rich solution pump (2) connects the tube-side inlet (4.1) of hollow fiber membrane contactors group (4) by heater (3), the shell-side outlet (4.4) of hollow fiber membrane contactors group (4) connects the low concentration salt solution entrance (5.1) of separator (5), the Separation of Water delivery outlet (5.2) of separator (5) connects the dilution water entrance (10.1) of mixing arrangement (10) by water pump (6), high concentration salt solutions outlet (5.3) of separator (5) connects the shell side inlet (4.3) of hollow fiber membrane contactors group (4), tube side outlet (4.2) of hollow fiber membrane contactors group (4) connects the cry-fluid inlet (7.1) of poor rich liquid heat exchanger (7), the cryogenic fluid outlet (7.2) of poor rich liquid heat exchanger (7) connects CO 2the rich solution input port (8.1) of reclaim equiment (8), CO 2the lean solution delivery outlet (8.2) of reclaim equiment (8) connects the high temperature fluid import (7.3) of poor rich liquid heat exchanger (7), high temperature fluid outlet (7.4) of poor rich liquid heat exchanger (7) connects the high concentration lean solution entrance (10.2) of mixing arrangement (10) by lean pump (9), mixed solution outlet (10.3) of mixing arrangement (10) connects condenser (11),
Described CO 2reclaim equiment (8) is also provided with CO 2exhaust outlet (8.3);
Flowmeter (12) and thermometer (13) is provided with in pipeline between the tube-side inlet (4.1) of described heater (3) and hollow fiber membrane contactors group (4); Flowmeter (12) and thermometer (13) is provided with in pipeline between high concentration salt solutions outlet (5.3) of described separator (5) and the shell side inlet (4.3) of hollow fiber membrane contactors group (4); Flowmeter (12) and thermometer (13) is provided with in pipeline between the dilution water entrance (10.1) of described water pump (6) and mixing arrangement (10); Flowmeter (12) and thermometer (13) is provided with in pipeline between the high concentration lean solution entrance (10.2) of described lean pump (9) and mixing arrangement (10); Flowmeter (12) and thermometer (13) is provided with in pipeline between mixed solution outlet (10.3) of described mixing arrangement (10) and condenser (11); Be provided with water absorbing agent concentration sensor (14) in the shell side of described hollow fiber membrane contactors group (4), in mixed solution outlet (10.3) of described mixing arrangement (10), be provided with concentration of absorbing sensor (16);
Salting liquid reflux pump (15) is provided with between the shell-side outlet (4.4) of hollow fiber membrane contactors group (4) and the low concentration salt solution entrance (5.1) of separator (5);
Described mixing arrangement (10) also offers replenisher entrance (10.4).
2. one kind utilizes described in claim 1 based on CO in the gas of concentration of absorbing conversion 2cO in the gas of chemical absorbing system 2chemical absorption process, is characterized in that, it comprises the steps:
Step 1: at CO 2cO is added in absorption equipment (1) 2chemical absorbent;
Step 2: CO to be separated 2gas enter CO by air inlet (1.4) 2absorption equipment (1), and and CO 2cO in absorption equipment (1) 2chemical absorbent sends reaction, generates initial rich CO 2solution, initial rich CO 2solution is by CO 2the liquid outlet (1.1) of absorption equipment (1) enters rich solution pump (2);
Step 3: initial rich CO 2solution enters heater (3) via rich solution pump (2), the tube-side inlet (4.1) of hollow fiber membrane contactors group (4) is entered be heated to 60 ~ 80 DEG C in heater (3) after, and flow in the tube side of hollow fiber membrane contactors group (4) and stop 150 ~ 180S, simultaneously, flow in hollow fiber membrane contactors group (4) shell side water absorbing agent, the rear initial rich CO of the heating in tube side 2water absorbing agent in solution and shell side forms reverse movement, initial rich CO after heating 2water in solution is initial rich CO after the heating 2under the driving of the steam partial pressure of solution and the difference of water absorbing agent steam partial pressure, entered into the water absorbing agent of shell side as water vapor from the tube side of hollow fiber membrane contactors group (4) by fenestra, thus make the rear initial rich CO of heating 2solution obtains concentrated and obtains absorbent solute and entrained CO 2mass concentration scope be 50% ~ 60% concentrated phase, the concentrated cry-fluid inlet (7.1) being entered poor rich liquid heat exchanger (7) by tube side outlet (4.2); And the water absorbing agent after water suction is being entered separator (5) by shell-side outlet, and absorbed moisture is discharged through heating and/or reduced pressure treatment in separator (5), this moisture discharged is dilute phase, dilute phase is exported by Separation of Water delivery outlet (5.2), and be transported in mixing arrangement (10) via water pump (6), discharge the water absorbing agent after moisture in separator (5) and export (5.3) output by high concentration salt solutions, enter hollow fiber membrane contactors group (4) Inner eycle and use;
Step 4: the concentrated of described hollow fiber membrane contactors (4) tube side outlet (4.2) enters poor rich liquid heat exchanger (7) and CO mutually 2the lean solution that reclaim equiment (8) obtains carries out heat exchange intensification, and enters CO by cryogenic fluid outlet (7.2) 2reclaim equiment (8) regenerates, CO 2regeneration temperature in reclaim equiment (8) is 80 ~ 120 DEG C, and regenerates CO 2, then the CO born 2by CO 2the CO of reclaim equiment (8) 2exhaust outlet (8.3) enters CO 2in collecting device, the absorbent Solute mass concentration range of the lean solution obtained after regeneration is 50% ~ 60%, and the lean solution obtained after regeneration is by CO 2the lean solution delivery outlet (8.2) of reclaim equiment (8) enters poor rich liquid heat exchanger (7) by high temperature fluid import (7.3) and carries out heat exchange cooling mutually with concentrated, and export (7.4) input lean pump (9) by high temperature fluid, be transported in mixing arrangement (10) through lean pump (9);
Step 5: the lean solution in mixing arrangement (10) after regeneration is fully mixed by stirring with dilute phase, controls the lean solution mass concentration after diluting by the flow controlling the lean solution after regenerating and dilute phase, thus makes lean solution concentration return to initial CO 2the state of chemical absorbent, is then entered after condenser (11) condenses to the temperature of specifying by mixed solution outlet (10.3) and returns CO 2absorption equipment carries out CO in (1) again 2absorb;
In described step 5, return to initial CO 2the lean solution of chemical absorbent state enters after condenser (11) condenses to 30 ~ 40 DEG C and returns CO 2absorption equipment carries out CO in (1) again 2absorb;
In described step 3, in hollow fiber membrane contactors group (4) shell side, the water absorbing agent of flowing is not for absorb CO 2water imbibition salt, describedly do not absorb CO 2water imbibition salt be calcium chloride or lithium chloride or lithium bromide.
In described step 5, the lean solution mass concentration after diluting is controlled by the flow controlling the lean solution after regenerating and dilute phase, concentration of absorbing sensor (16) simultaneously in conjunction with mixed solution outlet (10.3) detects the rear lean solution mass concentration state of dilution, when determining the loss having absorbent solute or water in whole system, through the replenisher entrance (10.4) of mixing arrangement (10) from the corresponding pure absorbent of external complement or water.
3. CO in gas according to claim 2 2chemical absorption process, is characterized in that: in described step 2, CO to be separated 2gas be biogas, flue gas or rubbish landfill gas, CO 2chemical absorbent is ethanolamine solutions, and the monoethanolamine mass concentration of this ethanolamine solutions is 30%.
4. CO in gas according to claim 2 2chemical absorption process, is characterized in that: in described step 3, concentrates and comprises absorbent solute and entrained CO mutually 2.
CN201310449986.6A 2013-09-27 2013-09-27 Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for Active CN103521053B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201310449986.6A CN103521053B (en) 2013-09-27 2013-09-27 Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201310449986.6A CN103521053B (en) 2013-09-27 2013-09-27 Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for

Publications (2)

Publication Number Publication Date
CN103521053A CN103521053A (en) 2014-01-22
CN103521053B true CN103521053B (en) 2015-07-29

Family

ID=49923622

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201310449986.6A Active CN103521053B (en) 2013-09-27 2013-09-27 Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for

Country Status (1)

Country Link
CN (1) CN103521053B (en)

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101541994B1 (en) * 2014-02-03 2015-08-04 한국에너지기술연구원 Apparatus and process for carbon dioxide capture related to generate electricity
KR101564165B1 (en) * 2014-03-07 2015-10-28 한국에너지기술연구원 Carbon dioxide capture apparatus and process for using self-generating power means
CN107149865A (en) * 2017-05-24 2017-09-12 华中农业大学 CO based on vapor mass transfer enhancement waste heat recovery2Chemical absorbing System and method for
CN108738817A (en) * 2018-06-08 2018-11-06 华中农业大学 CO is increased at regular time and quantity for greenhouse2The System and method for of gas fertilizer
CN110420543B (en) * 2019-08-20 2020-05-26 华中科技大学 CO capture device for reaction phase change2In a device
JP7431708B2 (en) * 2020-09-11 2024-02-15 株式会社東芝 Acid gas removal control device, acid gas removal control method, and acid gas removal device

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102802766A (en) * 2009-06-19 2012-11-28 国际壳牌研究有限公司 Process For The Removal Of Carbon Dioxide And/or Hydrogen Sulphide From A Gas
CN203494386U (en) * 2013-09-27 2014-03-26 华中农业大学 Chemical absorption system for CO2 in gas based on absorbent concentration change
EP2719441A1 (en) * 2011-05-12 2014-04-16 Mitsubishi Heavy Industries, Ltd. Co2 recovery device, and co2 recovery method.

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4956519B2 (en) * 2008-10-06 2012-06-20 株式会社東芝 Carbon dioxide recovery system

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102802766A (en) * 2009-06-19 2012-11-28 国际壳牌研究有限公司 Process For The Removal Of Carbon Dioxide And/or Hydrogen Sulphide From A Gas
EP2719441A1 (en) * 2011-05-12 2014-04-16 Mitsubishi Heavy Industries, Ltd. Co2 recovery device, and co2 recovery method.
CN203494386U (en) * 2013-09-27 2014-03-26 华中农业大学 Chemical absorption system for CO2 in gas based on absorbent concentration change

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Menachem Elimelech et al..The Future of Seawater Desalination:Energy,Technology,and the Environment.《Science》.2011,第333卷 *
Regeneration performance of concentrated Co2-rich alkanolamine solvent: The first step study of a novel concept for reducing regeneration heat consumption by using concentration swing absorption technology;Shuiping Yan et al.;《Chemical Engineering and Processing: Process Intensification》;20130515;第70卷;正文第87页左栏第9行-右栏第2段、附图1 *

Also Published As

Publication number Publication date
CN103521053A (en) 2014-01-22

Similar Documents

Publication Publication Date Title
CN103521053B (en) Based on CO in the gas of concentration of absorbing conversion 2chemical absorbing System and method for
CN104107629B (en) A kind of smoke carbon dioxide capture system and capture method
CN104587804B (en) Gas separation membrane is used to carry out the apparatus system purified
CN104697235B (en) One kind is based on electrodialytic ternary working medium ammonia absorption type refrigeration system
CN104226096B (en) Multi-flow-path circulating desulfurization system and multi-flow-path circulating desulfurization method
CN101703880A (en) Power plant flue gas desulphurization and decarbonization integrated purification system
CN103318850A (en) Low-temperature waste heat recovery system for pyrite and metallurgical off-gas acid making device
CN203803335U (en) Multistage split regeneration carbon dioxide trapping system
CN108211671A (en) A kind of energy-saving carbon dioxide regeneration and compressibility and method
CN105674616B (en) A kind of absorption type refrigeration circulating system of membrane distillation concentration lithium-bromide solution
CN107115776A (en) One kind CO suitable for cement kiln flue gas2The change system continuously trapped
CN203494386U (en) Chemical absorption system for CO2 in gas based on absorbent concentration change
CN105233689B (en) Organic amine wet flue gas desulphurization and desorption system with high-efficiency and low-energy consumption
CN107715650A (en) A kind of carbon trapping system regeneration gas heat recovery structure
CN208771134U (en) CO based on heat pipe intensified recuperation of heat2Chemical absorbing system
CN105236360B (en) A kind of device and method improving ore deposit or the recovery of flue gas during smelting Sulphuric acid Low Temperature Thermal
CN107754568B (en) Low-energy-consumption device for capturing and recovering carbon dioxide by flue gas and gas recovery process
CN207533246U (en) A kind of carbon trapping system regeneration gas heat reclaim unit
CN109513313A (en) A kind of low-temperature catalyzed regeneration method of collecting carbonic anhydride solvent
CN210261116U (en) High-added-value utilization system for geothermal steam field hydrogen sulfide associated gas
CN207886919U (en) Residual neat recovering system
CN114849420B (en) Reinforcing system and method based on gas-steam heat exchange adsorption device
CN207585143U (en) A kind of first-class absorption type heat pump of solar energy auxiliary heating
CN205481906U (en) System for utilize mixed working medium to pass through heating power driven compact desorption carbon dioxide
CN105776694B (en) A kind of energy-efficient treatment system of the organic brine waste of high concentration

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant