CN208771134U - CO based on heat pipe intensified recuperation of heat2Chemical absorbing system - Google Patents
CO based on heat pipe intensified recuperation of heat2Chemical absorbing system Download PDFInfo
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- CN208771134U CN208771134U CN201821103111.5U CN201821103111U CN208771134U CN 208771134 U CN208771134 U CN 208771134U CN 201821103111 U CN201821103111 U CN 201821103111U CN 208771134 U CN208771134 U CN 208771134U
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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]
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- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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Abstract
CO based on heat pipe intensified recuperation of heat designed by the utility model2Chemical absorbing system, it includes booster fan, CO2Absorption equipment, rich solution pump, three-way flow divider valve, liquid liquid gravity type heat pipe heat exchanger, lean solution cooler, lean pump, gas-liquid gravity type heat pipe heat exchanger, CO2Generating apparatus and reboiler again, the utility model can be in the CO for keeping original maturation2The thermal energy in the high-temperature barren liquor being discharged with the high temperature regeneration gas waste heat and high efficiente callback regenerator bottom on the basis of rich solution regeneration techniques, efficiently using the discharge of rich solution hot recycling tower top is absorbed, to reduce heat exchanger volume needed for regeneration gas waste heat recycles and investment.
Description
Technical field
The utility model relates to rich CO2CO in gas2Chemical absorption process energy conservation field, in particular to one kind
CO based on heat pipe intensified recuperation of heat2Chemical absorbing system.
Background technique
CO2As one of most important greenhouse gases, a series of environmental problems such as global warming are caused.Carbon capture
It can solve CO with the conduct of (CCS) technology is sealed up for safekeeping2The effective means of emission problem, it is considered to be the nearly following extensive reduction CO2Row
One of most economical in putting, feasible method.Wherein, the CO based on chemical absorption method2Isolation technics is because of technology maturation, CO2It is de-
Except the high advantage of rate can carry out large-scale application, but key factor is in its economy problems, especially richness CO2Absorbent solution
The high problem of (rich solution) regeneration energy consumption.Such as typical biogas CO2In chemical absorption process, the regeneration heat consumption of rich solution can account for total energy consumption
60% or more.By taking classical ethanol amine (MEA) absorbent system as an example, typical heat regeneration energy consumption is about 4.0MJ/kgCO2,
CO2Separation costs are up to 250-300 yuan/ton of CO2.Based on this, the target that system lowers consumption is concentrated mainly on out by domestic and international researcher
Hair New Absorbent, improvement regeneration technology and regeneration heat integration utilize etc. in research directions.Such as use ammonium hydroxide absorbent, ionic liquid
Body absorbent and two-phase absorbent etc., or set about from process optimization, using absorption tower cooling during rolling technique, rich solution shunting process
With heating process etc. among regenerator.But it no matter is directed to any consumption reduction mode or system, is directed to heat exchanger in technique
It uses.As one of heat recovery element basic in entire process flow, the superiority and inferiority of heat exchanger performance is largely affected
The regeneration heat consumption of rich solution.In existing chemical absorption method technique, the cooling and regeneration overhead of heat exchange, lean solution between rich or poor liquid
The regeneration air cooling in portion etc. all refers to the use of heat exchanger.The economic temperature difference of current general heat exchanger is 20K, the coefficient of heat transfer compared with
It is small, it is such as intended to reach lower heat transfer temperature difference (5~10K), then will need huge heat exchange area, and lead to cost of investment and land occupation face
Product becomes larger.Therefore, if a kind of high-performance heat exchanger can be used, keep heat transfer temperature difference or heat exchange area big using its higher coefficient of heat transfer
Width decline will be not necessarily to carry out prior art system big transformation, and be suitably adapted for any hot recycling absorbent system, thus
It realizes and further decreases regeneration energy consumption on the basis of original system itself consumption reduction.
Heat pipe is kind of an efficient phase-change heat-exchange element, is generally divided into evaporator section, adiabatic section and condensation section, working medium (Ru Shui, first
Alcohol etc.) the heated vaporization of spontaneous evaporation section forms steam, and steam diffuses to condensation section under pressure, releases in condensation section to cold source
It is condensed back by gravity to evaporator section after the latent heat of vaporization.Compared with usual heat exchanger, heat pipe heat transfer efficiency with higher and biography
The advantages such as thermoae limit, structure are simple, manufacturing cost is cheap, required heat exchange area is smaller can pass in the case where temperature difference very little
Sizable heat flow is passed, suitable for the recycling of low grade heat energy, is widely used in industrial afterheat recovery application at present.
Summary of the invention
The purpose of the utility model is to provide a kind of CO based on heat pipe intensified recuperation of heat2Chemical absorbing system, the system
Core be using high-performance heat exchanger heat pipe as CO2Heat exchange element in chemical absorption process process replaces tradition with this
Heat exchanger (pipe heat exchanger, plate heat exchanger etc.).It therefore, can be in the CO for keeping original maturation2It absorbs and rich solution regeneration techniques
On the basis of, the high temperature regeneration gas waste heat of effective use rich solution hot recycling tower top discharge and the discharge of high efficiente callback regenerator bottom
High-temperature barren liquor in thermal energy, with reduce regeneration gas waste heat recycle needed for heat exchanger volume and investment.
In order to achieve this, a kind of CO based on heat pipe intensified recuperation of heat designed by the utility model2Chemical absorbing system
System, it is characterised in that: it includes booster fan, CO2Absorption equipment, rich solution pump, three-way flow divider valve, the heat exchange of liquid liquid gravity type heat pipe
Device, lean solution cooler, lean pump, gas-liquid gravity type heat pipe heat exchanger, CO2Generating apparatus and reboiler again, wherein CO2Absorption is set
The output end of standby air inlet connection booster fan, CO2The top of absorption equipment is equipped with top exhaust outlet, CO2The bottom of absorption equipment
Portion's liquid outlet connects the input terminal of rich solution pump, CO2The output end of the absorbing liquid input port connection lean pump of absorption equipment, rich solution
The first port of the output end connection three-way flow divider valve of pump, the second port connection gas-liquid gravity type heat pipe heat exchange of three-way flow divider valve
The liquid phase entrance of device, the low temperature rich solution entrance of the third port connection liquid liquid gravity type heat pipe heat exchanger of three-way flow divider valve, liquid liquid
The high temperature rich solution outlet of gravity type heat pipe heat exchanger connects CO2First rich solution input port of generating apparatus again, liquid liquid gravity type heat pipe
The lean solution entrance of the low-temperature barren liquor outlet connection lean solution cooler of heat exchanger, the high-temperature barren liquor of liquid liquid gravity type heat pipe heat exchanger enter
The lean solution delivery outlet of mouth connection reboiler, CO2The rich solution input port of the bottom end leakage fluid dram connection reboiler of generating apparatus again, CO2Regeneration
The gas phase side condensation-water drain of the top condensate return entrance connection gas-liquid gravity type heat pipe heat exchanger of equipment, CO2Regeneration is set
The gas phase entrance of standby top vent connection gas-liquid gravity type heat pipe heat exchanger, CO2Second rich solution input port of generating apparatus again
The liquid-phase outlet of gas-liquid gravity type heat pipe heat exchanger is connected, the gaseous phase outlet of gas-liquid gravity type heat pipe heat exchanger is for being discharged CO2,
The reboiler top exhaust outlet of reboiler connects CO2The bottom end air inlet of generating apparatus again, the reboiler have saturated vapor defeated
Entrance and high temperature water output, the input terminal of the lean solution outlet connection lean pump of lean solution cooler.
The utility model has the following beneficial effects:
1, the utility model is using gas-liquid gravity type heat pipe heat exchanger as the heat transferring medium between regeneration gas and cold rich solution,
Can intensifying regenerating gas to the quantity of heat convection of cold rich solution, regeneration gas is substantially improved to the heat transfer efficiency of cold rich solution, makes regeneration gas
Waste heat recovery efficiency greatly enhances, and there is good regeneration heat consumption to reduce latent heat.
2, compared with based on conventional suctions systems such as shell-and-tube heat exchanger and plate heat exchangers, the utility model is based on liquid liquid
The CO of gravity type heat pipe heat exchanger and gas-liquid gravity type heat pipe design of heat exchanger2Chemical absorbing system, heat transfer effect with higher
Rate and heat transport limitation, and simple and compact for structure, manufacturing cost is cheap, takes up little area, the advantages such as reliable operation, and can meet it is identical
Heat transfer temperature difference under so that heat exchange area substantially reduces (as shown in appendix 1).
Detailed description of the invention
Fig. 1 is the structural block diagram of the utility model.
Fig. 2 is the gas phase side heat pipe tube bank arrangement schematic diagram of gas-liquid gravity type heat pipe heat exchanger in the utility model.
Fig. 3 is the liquid side heat pipe tube bank arrangement of gas-liquid and liquid liquid gravity type heat pipe heat exchanger signal in the utility model
Figure.
In Fig. 1,1-booster fan, 2-CO2Absorption equipment, 2.1-top exhaust outlets, 2.2-absorbing liquid input ports,
2.3-air inlets, 2.4-bottom liquid outlets, 3-rich solution pumps, 4-three-way flow divider valves, 4.1-first ports, 4.2-second ends
Mouth, 4.3-third ports, 5-liquid liquid gravity type heat pipe heat exchangers, 5.1-low temperature rich solution entrances, 5.2-high temperature rich solution outlets,
5.3-high-temperature barren liquor entrances, the outlet of 5.4-low-temperature barren liquors, 6-lean solution coolers, 6.1-lean solution entrances, 6.2-lean solutions go out
Mouth, 7-lean pumps, 8-gas-liquid gravity type heat pipe heat exchangers, 8.1-liquid phase entrances, 8.2-liquid-phase outlets, 8.3-gas phases enter
Mouth, 8.4-gas phase side condensation-water drains, 8.5-gaseous phase outlets, 9-CO2Again generating apparatus, the 9.1-the first rich solution input port,
9.2-top condensate return entrances, 9.3-top vents, the 9.4-the second rich solution input port, 9.5-bottom end air inlets,
9.6-bottom end leakage fluid drams, 10-reboilers, 10.1-lean solution delivery outlets, 10.2-rich solution input ports, 10.3-reboiler tops
Exhaust outlet, 10.4-saturated vapor input ports, 10.5-high temperature water outputs, 11.1-first flow sensors, 11.2-the
Two flow sensors, 11.3-third flow sensors, the 12.1-the first temperature sensor, 12.2-second temperature sensors,
12.3-third temperature sensors, the 12.4-the four temperature sensor, the 12.5-the five temperature sensor, the 12.6-the six temperature
Spend sensor, the 12.7-the seven temperature sensor, the 12.8-the eight temperature sensor, the 12.9-the nine temperature sensor, 13-
Humidity sensor.
In Fig. 2, fin need to be increased in the gas phase side heat pipe outer wall of gas-liquid gravity type heat pipe heat exchanger, to improve heat convection
Coefficient simultaneously significantly increases heat exchange area.Meanwhile heat pipe tube bank is set using fork arrangement, and fluid flow resistance between pipe can be made to become larger,
To which flow-disturbing is abundant, be conducive to strengthen heat convection effect.
In Fig. 3, in gas-liquid and liquid liquid gravity type heat pipe heat exchanger, heat pipe tube bank liquid side is usually to increase liquid changing
Residence time in hot device, can be in interbank arrangement baffle plate with enhanced heat exchange.
Specific embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail:
A kind of CO based on heat pipe intensified recuperation of heat of the utility model design2Chemical absorbing system, as shown in Figures 1 to 3,
It includes booster fan 1, CO2Absorption equipment 2, rich solution pump 3, three-way flow divider valve 4, liquid liquid gravity type heat pipe heat exchanger 5 (are used for liquid
Exchange heat between body and liquid), lean solution cooler 6, lean pump 7, gas-liquid gravity type heat pipe heat exchanger 8 (for gas and liquid it
Between exchange heat), CO2Regenerate equipment 9 and reboiler 10, wherein CO2The air inlet 2.3 of absorption equipment 2 connects the defeated of booster fan 1
Outlet, CO2The top of absorption equipment 2 is equipped with top exhaust outlet 2.1, CO2The bottom liquid outlet 2.4 of absorption equipment 2 connects rich solution pump
3 input terminal, CO2The absorbing liquid input port 2.2 of absorption equipment 2 connects the output end of lean pump 7, and the output end of rich solution pump 3 connects
The first port 4.1 of three-way flow divider valve 4 is connect, the second port 4.2 of three-way flow divider valve 4 connects gas-liquid gravity type heat pipe heat exchanger 8
Liquid phase entrance 8.1, the third port 4.3 of three-way flow divider valve 4 connects the low temperature rich solution entrance of liquid liquid gravity type heat pipe heat exchanger 5
5.1, the high temperature rich solution outlet 5.2 of liquid liquid gravity type heat pipe heat exchanger 5 connects CO2Regenerate the first rich solution input port of equipment 9
9.1, the lean solution entrance 6.1 of the 5.4 connection lean solution cooler 6 of low-temperature barren liquor outlet of liquid liquid gravity type heat pipe heat exchanger 5, liquid liquid weight
The high-temperature barren liquor entrance 5.3 of power formula heat exchange of heat pipe 5 connects the lean solution delivery outlet 10.1, CO of reboiler 102Regenerate equipment 9
The rich solution input port 10.2, CO of the connection reboiler 10 of bottom end leakage fluid dram 9.62Regenerate the top condensate return entrance 9.2 of equipment 9
Connect the gas phase side condensation-water drain 8.4, CO of gas-liquid gravity type heat pipe heat exchanger 82The top vent 9.3 for regenerating equipment 9 connects
Connect the gas phase entrance 8.3, CO of gas-liquid gravity type heat pipe heat exchanger 82The the second rich solution input port 9.4 for regenerating equipment 9 connects gas-liquid
The liquid-phase outlet 8.2 of gravity type heat pipe heat exchanger 8, the gaseous phase outlet 8.5 of gas-liquid gravity type heat pipe heat exchanger 8 is for being discharged CO2,
The reboiler top exhaust outlet 10.3 of reboiler 10 connects CO2The bottom end air inlet 9.5 of equipment 9 is regenerated, the reboiler 10 has
There are saturated vapor input port 10.4 and high temperature water output 10.5 (high-temperature water temperature range is 90~100 DEG C), lean solution cooler 6
Lean solution outlet 6.2 connection lean pumps 7 input terminals.
In above-mentioned technical proposal, the saturated vapor input port 10.4 of reboiler 10 and high temperature water output 10.5 are for being passed through
Steam heats rich solution, and rich solution regeneration temperature is generally 100~120 DEG C (can be by selected CO2Chemical absorbent characteristic is determined
It is fixed).
In above-mentioned technical proposal, it further includes first flow sensor 11.1, second flow sensor 11.2 and third stream
The output end of rich solution pump 3 and the first end of three-way flow divider valve 4 is arranged in quantity sensor 11.3, the first flow sensor 11.1
In pipeline between mouth 4.1, the lean solution outlet 6.2 and lean solution of lean solution cooler 6 is arranged in the second flow sensor 11.2
On pipeline between the input terminal of pump 7, the second port 4.2 of three-way flow divider valve 4 is arranged in the third flow sensor 11.3
On pipeline between the liquid phase entrance 8.1 of gas-liquid gravity type heat pipe heat exchanger 8.
In above-mentioned technical proposal, it further includes the first temperature sensor 12.1, second temperature sensor 12.2, third temperature
Sensor 12.3, the 4th temperature sensor 12.4, the 5th temperature sensor 12.5, the 6th temperature sensor 12.6, the 7th temperature
Sensor 12.7, the 8th temperature sensor 12.8 and the 9th temperature sensor 12.9, wherein first temperature sensor
12.1 are arranged in CO2In pipeline between the absorbing liquid input port 2.2 of absorption equipment 2 and the output end of lean pump 7, described second
Temperature sensor 12.2 is arranged in the pipeline between the output end of rich solution pump 3 and the first port 4.1 of three-way flow divider valve 4, the
The low-temperature barren liquor outlet 5.4 and lean solution cooler 6 of liquid liquid gravity type heat pipe heat exchanger 5 is arranged in three-temperature sensor 12.3
On pipeline between lean solution entrance 6.1, the rich, high temperature of liquid liquid gravity type heat pipe heat exchanger 5 is arranged in the 4th temperature sensor 12.4
Liquid exports 5.2 and CO2It regenerates on the pipeline between the first rich solution input port 9.1 of equipment 9, the setting of the 5th temperature sensor 12.5
Pipeline between the high-temperature barren liquor entrance 5.3 of liquid liquid gravity type heat pipe heat exchanger 5 and the lean solution delivery outlet 10.1 of reboiler 10
On, the 6th temperature sensor 12.6 is arranged in the gaseous phase outlet 8.5 of gas-liquid gravity type heat pipe heat exchanger 8, the 7th temperature sensing
Device 12.7 is arranged in CO2Regenerate equipment 9 top vent 9.3 and gas-liquid gravity type heat pipe heat exchanger 8 gas phase entrance 8.3 it
Between pipeline on, the 8th temperature sensor 12.8 be arranged in CO2Regenerate the second rich solution input port 9.4 and the gas-liquid gravity of equipment 9
On pipeline between the liquid-phase outlet 8.2 of formula heat exchange of heat pipe 8, the 9th temperature sensor 12.9 is arranged in CO2Regenerate equipment 9
On pipeline between bottom end leakage fluid dram 9.6 and the rich solution input port 10.2 of reboiler 10.Each sensing of above-mentioned design installation
Device can detect the temperature of each pipeline to measure its recuperation of heat effect, convenient for optimizing to operating parameter each in technique.
In above-mentioned technical proposal, it further includes humidity sensor 13, and the humidity sensor 13 is arranged in gas-liquid gravity type
In the gaseous phase outlet 8.5 of heat exchange of heat pipe 8.Humidity sensor 13 is for detecting outlet CO2In whether also contain vapor.
Rich solution temperature in above-mentioned technical proposal, in the low temperature rich solution entrance 5.1 of the liquid liquid gravity type heat pipe heat exchanger 5
Range is 40~60 DEG C, the rich solution temperature range in the high temperature rich solution outlet 5.2 of liquid liquid gravity type heat pipe heat exchanger 5 is 90~
110 DEG C, it is 50~60 DEG C that the low-temperature barren liquor of liquid liquid gravity type heat pipe heat exchanger 5, which exports the lean solution temperature range in 5.4, liquid liquid weight
Lean solution temperature range in the high-temperature barren liquor entrance 5.3 of power formula heat exchange of heat pipe 5 is 100~120 DEG C.
In above-mentioned technical proposal, the CO2The top exhaust outlet 2.1 of absorption equipment 2 is for being discharged removing CO2Residue afterwards
Gas.When purifying gas is biogas, CO is removed2Residual gas afterwards most of (95% or more percent by volume) is methane, when
Purifying gas is desulfurization fume, removes CO2Residual gas afterwards is based on nitrogen.
A kind of CO of above system2Chemical absorption process, it includes the following steps:
Step 1: rich CO2Gas is by entering CO by air inlet 2.3 after the pressurization of booster fan 12Absorption equipment 2, and from CO2
The CO that absorbing liquid input port 2.2 in absorption equipment 2 enters2Chemical absorbent forms counter current contacting, rich CO2CO in gas2Quilt
It absorbs, purified gas is from CO2The discharge of 2 top exhaust outlet of absorption equipment, CO2CO in absorption equipment 22Chemical absorbent (such as ethyl alcohol
Amine, diethanol amine etc.) absorb CO2The initial absorption agent richness CO generated afterwards2Solution is by CO2The bottom liquid outlet 2.4 of absorption equipment 2
Into rich solution pump 3；
Step 2: initial absorption agent richness CO2Solution enters in three-way flow divider valve 4 via rich solution pump 3 to be shunted, shunting
First via initial absorption agent richness CO2Solution enters gas-liquid gravity type heat pipe heat exchanger 8 through the second port 4.2 of three-way flow divider valve 4
Liquid phase entrance 8.1, the second tunnel initial absorption agent richness CO of shunting2Solution enters liquid through the third port 4.3 of three-way flow divider valve 4
Liquid gravity type heat pipe heat exchanger 5, and it is defeated with the lean solution delivery outlet 10.1 of reboiler 10 in liquid liquid gravity type heat pipe heat exchanger 5
100~120 DEG C of high warm lean solution after regeneration out carries out heat exchange, makes the second tunnel initial absorption agent richness CO shunted2It is molten
Liquid is heated to 90~110 DEG C, is then heated to 90~110 DEG C of second tunnel initial absorption agent richness CO2Solution passes through liquid liquid weight
The high temperature rich solution outlet 5.2 of power formula heat exchange of heat pipe 5 enters CO2Regenerate the first rich solution input port 9.1 of equipment 9；
Step 3:CO290~110 DEG C of the high temperature regeneration gas that the top vent 9.3 of regeneration equipment 9 is discharged enters gas-liquid
The gas phase side of gravity type heat pipe heat exchanger 8,40~60 DEG C of first via initial absorption agent after being shunted through three-way flow divider valve 4
Rich CO2Solution carries out heat exchange with high temperature regeneration gas in gas-liquid gravity type heat pipe heat exchanger 8, and wherein heat pipe gas phase side outer wall increases
Add fin, improves convection transfer rate to increase heat exchange area, realize the reinforcing of regeneration gas waste heat recyclability, high temperature is again
Heat pipe gas phase side of the part vapor in gas-liquid gravity type heat pipe heat exchanger 8 in anger condenses and discharges a large amount of latent heat (not
The vapor of condensation is with CO2It is discharged from the gaseous phase outlet 8.5 of gas-liquid gravity type heat pipe heat exchanger 8), and transfer heat to gas-liquid gravity type
The liquid side of heat exchange of heat pipe 8, by 8 liquid side of gas-liquid gravity type heat pipe heat exchanger, 40~60 DEG C of first via initial absorption agent
Rich CO2Solution is warming up to 80~90 DEG C, and at the same time, the temperature of the high temperature regeneration gas in gas-liquid gravity type heat pipe heat exchanger 8 drops
To 45~65 DEG C, then CO2It is discharged from the gaseous phase outlet 8.5 of gas-liquid gravity type heat pipe heat exchanger 8, gas-liquid gravity type heat pipe changes
The gas phase side condensed water of hot device 8 is back to CO by gas phase side condensation-water drain 8.42Regenerate the top condensate return of equipment 9
Entrance 9.2, the cold rich solution of shunting after having recycled high temperature regeneration gas waste heat, i.e., the first via richness CO after recovery waste heat2Solution is through gas
The liquid-phase outlet 8.2 of liquid gravity type heat pipe heat exchanger 8 flows into CO2Regenerate the second rich solution input port 9.4 of equipment 9；
Step 4: entering CO through the first rich solution input port 9.12Regenerate equipment 9 passes through liquid liquid gravity type heat pipe heat exchanger 5
Rich CO2Solution and through the second rich solution input port 9.4 enter CO2Rich CO after regenerating the recovery waste heat of equipment 92Solution is in CO2Again
In generating apparatus 9 with CO2It is inversely contacted with vapor regeneration gas after being heated again, by CO2Regenerate the bottom end leakage fluid dram 9.6 of equipment 9
It flows into heating in reboiler 10 and isolates CO2And absorbent, the CO isolated is heated in reboiler 102Carry saturated steam by
Reboiler top exhaust outlet 10.3 inputs CO2The bottom end air inlet 9.5 of equipment 9 is regenerated, and in CO2Regenerate Xiang Shangliu in equipment 9
It is dynamic；
Step 5: 100~120 DEG C of the high-temperature barren liquor obtained after regeneration in reboiler 10 enters through lean solution delivery outlet 10.1
Liquid liquid gravity type heat pipe heat exchanger 5 is once cooled down, then again through 6 secondary cooling of lean solution cooler to required temperature (about 40
DEG C, actual temp enters lean solution cooler temperature according to lean solution and best lean solution absorbent temperature determines) CO is returned afterwards2Absorption is set
CO is absorbed again in standby 22。
In the step 1 of above-mentioned technical proposal, purified gas is from CO22 top of absorption equipment is after demisting from top exhaust outlet
Discharge.
In above-mentioned technical proposal, CO2Absorption equipment 2 and CO2The structure and type for regenerating equipment 9 can be unlimited, can both use
Traditional filler tower structure, also can be used the structures such as novel hollow fiber membrane contactors.
In above-mentioned technical proposal, it to be used for CO2The chemical absorbent of absorption is that can satisfy recycling renewable, low is waved
The absorbent of hair property.
Table 1: by taking 30% ethanol amine (MEA) solution system as an example, pair of traditional handicraft and heat pipe intensified waste heat reclaiming process
Than (handling CO in gas240%) volume fraction is
The content that this specification is not described in detail belongs to the prior art well known to professional and technical personnel in the field.
Claims (7)
1. a kind of CO based on heat pipe intensified recuperation of heat2Chemical absorbing system, it is characterised in that: it includes booster fan (1), CO2
It is absorption equipment (2), rich solution pump (3), three-way flow divider valve (4), liquid liquid gravity type heat pipe heat exchanger (5), lean solution cooler (6), poor
Liquid pump (7), gas-liquid gravity type heat pipe heat exchanger (8), CO2Generating apparatus (9) and reboiler (10) again, wherein CO2Absorption equipment (2)
Air inlet (2.3) connection booster fan (1) output end, CO2The top of absorption equipment (2) is equipped with top exhaust outlet (2.1),
CO2The input terminal of bottom liquid outlet (2.4) connection rich solution pump (3) of absorption equipment (2), CO2The absorbing liquid of absorption equipment (2) is defeated
Entrance (2.2) connects the output end of lean pump (7), the first port of output end connection three-way flow divider valve (4) of rich solution pump (3)
(4.1), the liquid phase entrance (8.1) of second port (4.2) connection gas-liquid gravity type heat pipe heat exchanger (8) of three-way flow divider valve (4),
The low temperature rich solution entrance (5.1) of third port (4.3) connection liquid liquid gravity type heat pipe heat exchanger (5) of three-way flow divider valve (4), liquid
The high temperature rich solution outlet (5.2) of liquid gravity type heat pipe heat exchanger (5) connects CO2First rich solution input port of generating apparatus (9) again
(9.1), the lean solution entrance of low-temperature barren liquor outlet (5.4) connection lean solution cooler (6) of liquid liquid gravity type heat pipe heat exchanger (5)
(6.1), the lean solution delivery outlet of high-temperature barren liquor entrance (5.3) connection reboiler (10) of liquid liquid gravity type heat pipe heat exchanger (5)
(10.1), CO2The rich solution input port (10.2) of bottom end leakage fluid dram (9.6) connection reboiler (10) of generating apparatus (9) again, CO2Regeneration
The gas phase side condensation-water drain of top condensate return entrance (9.2) connection gas-liquid gravity type heat pipe heat exchanger (8) of equipment (9)
(8.4), CO2The gas phase entrance of top vent (9.3) connection gas-liquid gravity type heat pipe heat exchanger (8) of generating apparatus (9) again
(8.3), CO2The liquid phase of the second rich solution input port (9.4) connection gas-liquid gravity type heat pipe heat exchanger (8) of generating apparatus (9) goes out again
Mouth (8.2), the gaseous phase outlet (8.5) of gas-liquid gravity type heat pipe heat exchanger (8) is for being discharged CO2, the reboiler of reboiler (10)
Top exhaust outlet (10.3) connects CO2There is saturation to steam for the bottom end air inlet (9.5) of generating apparatus (9) again, the reboiler (10)
Vapour input port (10.4) and high temperature water output (10.5), lean solution outlet (6.2) connection lean pump (7) of lean solution cooler (6)
Input terminal.
2. the CO according to claim 1 based on heat pipe intensified recuperation of heat2Chemical absorbing system, it is characterised in that: it is also wrapped
First flow sensor (11.1), second flow sensor (11.2) and third flow sensor (11.3) are included, it is described first-class
The pipeline that quantity sensor (11.1) is arranged between the output end of rich solution pump (3) and the first port (4.1) of three-way flow divider valve (4)
It is interior, the second flow sensor (11.2) setting lean solution cooler (6) lean solution outlet (6.2) and lean pump (7) it is defeated
Enter on the pipeline between end, the third flow sensor (11.3) setting three-way flow divider valve (4) second port (4.2) with
On pipeline between the liquid phase entrance (8.1) of gas-liquid gravity type heat pipe heat exchanger (8).
3. the CO according to claim 1 based on heat pipe intensified recuperation of heat2Chemical absorbing system, it is characterised in that: it is also wrapped
Include the first temperature sensor (12.1), second temperature sensor (12.2), third temperature sensor (12.3), the 4th temperature sensing
Device (12.4), the 5th temperature sensor (12.5), the 6th temperature sensor (12.6), the 7th temperature sensor (12.7), the 8th
Temperature sensor (12.8) and the 9th temperature sensor (12.9), wherein first temperature sensor (12.1) is arranged in CO2
In pipeline between the absorbing liquid input port (2.2) of absorption equipment (2) and the output end of lean pump (7), the second temperature is passed
In the pipeline that sensor (12.2) is arranged between the output end of rich solution pump (3) and the first port (4.1) of three-way flow divider valve (4),
Third temperature sensor (12.3) is arranged cold in the low-temperature barren liquor outlet (5.4) of liquid liquid gravity type heat pipe heat exchanger (5) and lean solution
But on the pipeline between the lean solution entrance (6.1) of device (6), the setting of the 4th temperature sensor (12.4) is changed in liquid liquid gravity type heat pipe
The high temperature rich solution outlet (5.2) and CO of hot device (5)2Again on the pipeline between the first rich solution input port (9.1) of generating apparatus (9),
High-temperature barren liquor entrance (5.3) and reboiler in liquid liquid gravity type heat pipe heat exchanger (5) is arranged in 5th temperature sensor (12.5)
(10) on the pipeline between lean solution delivery outlet (10.1), the setting of the 6th temperature sensor (12.6) is changed in gas-liquid gravity type heat pipe
In the gaseous phase outlet (8.5) of hot device (8), the 7th temperature sensor (12.7) is arranged in CO2The top vent of generating apparatus (9) again
(9.3) on the pipeline between the gas phase entrance (8.3) of gas-liquid gravity type heat pipe heat exchanger (8), the 8th temperature sensor
(12.8) it is arranged in CO2The liquid of second rich solution input port (9.4) and gas-liquid gravity type heat pipe heat exchanger (8) of generating apparatus (9) again
Mutually on the pipeline between outlet (8.2), the 9th temperature sensor (12.9) is arranged in CO2The bottom end leakage fluid dram of generating apparatus (9) again
(9.6) on the pipeline between the rich solution input port (10.2) of reboiler (10).
4. the CO according to claim 1 based on heat pipe intensified recuperation of heat2Chemical absorbing system, it is characterised in that: it is also wrapped
It includes humidity sensor (13), gaseous phase outlet of humidity sensor (13) setting in gas-liquid gravity type heat pipe heat exchanger (8)
(8.5) in.
5. the CO according to claim 1 based on heat pipe intensified recuperation of heat2Chemical absorbing system, it is characterised in that: the liquid
Rich solution temperature range in the low temperature rich solution entrance (5.1) of liquid gravity type heat pipe heat exchanger (5) is 40~60 DEG C, liquid liquid gravity type
Rich solution temperature range in the high temperature rich solution outlet (5.2) of heat exchange of heat pipe (5) is 90~110 DEG C, and liquid liquid gravity type heat pipe changes
Lean solution temperature range in the low-temperature barren liquor outlet (5.4) of hot device (5) is 50~60 DEG C, liquid liquid gravity type heat pipe heat exchanger (5)
High-temperature barren liquor entrance (5.3) in lean solution temperature range be 100~120 DEG C.
6. the CO according to claim 1 based on heat pipe intensified recuperation of heat2Chemical absorbing system, it is characterised in that: described
CO2The top exhaust outlet (2.1) of absorption equipment (2) is for being discharged removing CO2Residual gas afterwards.
7. the CO according to claim 6 based on heat pipe intensified recuperation of heat2Chemical absorbing system, it is characterised in that: work as purification
When gas is biogas, CO is removed2The above are methane for percent by volume 95% in residual gas afterwards, are desulfurization fumes when purifying gas,
Remove CO2Residual gas afterwards is nitrogen.
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| CN201821103111.5U CN208771134U (en) | 2018-07-12 | 2018-07-12 | CO based on heat pipe intensified recuperation of heat2Chemical absorbing system |
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| CN201821103111.5U CN208771134U (en) | 2018-07-12 | 2018-07-12 | CO based on heat pipe intensified recuperation of heat2Chemical absorbing system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108744893A (en) * | 2018-07-12 | 2018-11-06 | 华中农业大学 | CO based on heat pipe intensified recuperation of heat2Chemical absorbing System and method for |
| CN110152457A (en) * | 2019-05-16 | 2019-08-23 | 中石化石油工程技术服务有限公司 | The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery |
| CN111203073A (en) * | 2020-01-07 | 2020-05-29 | 浙江大学 | Flue gas CO2Desorption device of trapping system |
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2018
- 2018-07-12 CN CN201821103111.5U patent/CN208771134U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108744893A (en) * | 2018-07-12 | 2018-11-06 | 华中农业大学 | CO based on heat pipe intensified recuperation of heat2Chemical absorbing System and method for |
| CN108744893B (en) * | 2018-07-12 | 2024-02-27 | 华中农业大学 | CO based on heat pipe enhanced heat recovery 2 Chemical absorption system and method |
| CN110152457A (en) * | 2019-05-16 | 2019-08-23 | 中石化石油工程技术服务有限公司 | The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery |
| CN110152457B (en) * | 2019-05-16 | 2024-06-04 | 中石化石油工程技术服务有限公司 | Chemical absorption method carbon dioxide trapping system based on waste heat recycling |
| CN111203073A (en) * | 2020-01-07 | 2020-05-29 | 浙江大学 | Flue gas CO2Desorption device of trapping system |
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