CN111203086B - CO with low regeneration energy consumption and low pollutant emission2Trapping system - Google Patents
CO with low regeneration energy consumption and low pollutant emission2Trapping system Download PDFInfo
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- CN111203086B CN111203086B CN202010014499.7A CN202010014499A CN111203086B CN 111203086 B CN111203086 B CN 111203086B CN 202010014499 A CN202010014499 A CN 202010014499A CN 111203086 B CN111203086 B CN 111203086B
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2258/00—Sources of waste gases
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- B01D2258/0283—Flue gases
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- 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
- B01D53/1412—Controlling the absorption process
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- 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
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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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
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Abstract
The invention discloses flue gas CO with low regeneration energy consumption and low pollutant emission2A trapping device, the flue gas CO2The trapping device comprises a flue gas pretreatment unit, an absorption unit, a pollutant control unit, a rich solution shunting desorption unit and a low-pressure rich solution flash evaporation unit; the flue gas is evacuated after sequentially passing through the flue gas pretreatment unit, the absorption unit and the pollutant control unit, the absorbent rich liquid generated by the absorption unit is sequentially subjected to absorbent regeneration through the low-pressure rich liquid flash evaporation unit and the rich liquid shunting desorption unit, and the regenerated absorbent enters the absorption unit. The invention provides flue gas CO2The trapping device realizes the efficient recovery of heat during the operation of the system, reduces the energy consumption during the operation of the system and simultaneously achieves the aim of reducing the pollution emission.
Description
Technical Field
The invention relates to CO2The field of trapping, in particular to CO with low regeneration energy consumption and low pollutant emission2A capture system.
Background
Climate change is a serious challenge facing the world today, as CO2First discharge of CO from coal-fired power station and industrial boiler2Trapping is an important choice for realizing low-carbon development in China. In a plurality of CO2Among the trapping technologies, the chemical absorption and solid adsorption technologies are the most suitable for large-scale CO trapping at present due to high trapping efficiency and good adaptability2One of the potential technical routes.
However, CO2The capture system still faces the problems of investment and operation cost, pollution emission and the like:
1. in the traditional process, an absorption unit and a desorption tower usually use more than 10m of filler height to meet the requirements of a desorption rate and a desorption process, and high filler investment is needed;
2. the heat exchange efficiency of key equipment such as a lean-rich solution heat exchanger is low, the low-end-difference heat exchange below 5K is difficult to realize, the sensible heat recovery efficiency of an absorbent is low, wherein Chinese patent document with the publication number of CN102824818A discloses a method for reducing CO in flue gas2CO capture system energy consumption enhancement2The device for recovering the rate comprises a heat pump pipeline, a rich solution heat absorption and temperature rise pipeline and a lean solution heat dissipation and temperature reduction pipeline; the heat pump pipeline comprises a solution pump, an absorber connected with an inlet of the solution pump, a mixer, a solution heat exchanger, a generator connected with a mixer suction inlet and an inlet connected with an outlet of a shell of the solution heat exchanger, an absorber connected with an outlet of the mixer, a condenser connected with an upper outlet of the generator, a condensate tank connected with an outlet of the condenser, an evaporator connected with an outlet of the condensate tank, a working medium pump connected with an outlet of the evaporator, an evaporator spray pipe connected with an outlet of the working medium pump, and a vacuum pump connected with the evaporator and the condenser; the rich liquid heat absorption and temperature rise pipeline comprises a rich liquid incoming pipeline, a heat absorption coil, a condenser and a regeneration tower which are sequentially connected with the rich liquid incoming pipeline; the lean solution heat dissipation and cooling pipeline comprises a lean solution incoming pipeline and a heat dissipation coil connected with the lean solution incoming pipeline, and the heat dissipation coil is connected with the absorption tower;
3. a large amount of high-temperature steam along with CO at the top of the desorption tower2The product gas is discharged, and the recovery effect of the conventional graded-flow process on the top water vapor is not obvious, so that the latent heat loss is caused.
In addition, when the trapping system operates, a large amount of absorbent and degradation products thereof in the absorption unit are discharged along with the flue gas in the form of gas or aerosol, the consumption of the absorbent increases the operating cost of the system, and serious secondary environmental pollution is also brought. Therefore, it is highly desirable to develop a low energy consumption and low emission CO2The trapping system promotes the industrialization process of the trapping system.
Disclosure of Invention
The invention aims to provide flue gas CO with low regeneration energy consumption and low pollutant emission2The collecting device realizes the high-efficiency recovery of heat during the operation of the system and reduces the systemThe energy consumption is operated, and the aim of reducing the pollution emission is fulfilled.
The invention provides the following technical scheme:
flue gas CO with low regeneration energy consumption and low pollutant emission2A trapping device, the flue gas CO2The trapping device comprises a flue gas pretreatment unit, an absorption unit, a pollutant control unit, a rich solution shunting desorption unit and a low-pressure rich solution flash evaporation unit; the flue gas is emptied after sequentially passing through the flue gas pretreatment unit, the absorption unit and the pollutant control unit, the absorbent rich liquid generated by the absorption unit is regenerated by sequentially passing through the low-pressure rich liquid flash evaporation unit and the rich liquid shunting desorption unit, and the regenerated absorbent returns to the absorption unit.
The flue gas pretreatment unit comprises a flue gas cooling section and a desulfurization and denitrification section which are arranged from bottom to top, and the flue gas is sequentially cooled and dedusted in the flue gas cooling section and enters the lower part of the absorption unit after being desulfurized and denitrified in the desulfurization and denitrification section.
In the invention, the desulfurization and denitrification section is mainly formed by alkali liquor (NaOH and Na)2CO3) And (6) leaching.
In the invention, the flue gas cooling section and the desulfurization and denitrification section are arranged in a segmented manner, and condensed water generated when the flue gas is cooled by the flue gas cooling section is discharged, so that the flue gas cooling device has the advantages that: firstly, the condensate water can be prevented from entering the desulfurization and denitrification section along with the flue gas to dilute the concentration of alkali liquor in the desulfurization and denitrification section; secondly, when the flue gas is desulfurized through rough removal, the flue gas has SO3 2-With SO4 2-The condensed water can be treated to remove SO3 2-With SO4 2-And the condensed water can be reused for water replenishing of the whole system.
The absorption unit comprises a filler section and an interstage cooling device arranged in the middle section of the absorption unit, and the flue gas is subjected to CO removal after being in reverse contact with an absorbent in the filler section2Said removal of CO2The flue gas enters a pollutant control unit, and the absorbent enters a filling section after being cooled by an interstage cooling device.
The interstage cooling device comprises an upper liquid collector, a middle interstage cooler and a lower liquid redistributor, wherein the liquid collector collects part or all of the absorbent, the temperature of the absorbent is reduced by the interstage cooler, the absorbent is sent to the liquid redistributor, and the liquid redistributor sends the absorbent after temperature reduction to the filling section.
Specifically, if all the absorbent is collected, the absorbent is cooled to 40 ℃ and then sent to a liquid redistributor; if part of the absorbent is collected, the absorbent is cooled to 30-40 ℃ according to the liquid flow proportion, and then the absorbent is sent to a liquid redistributor, so that the effect of 40 ℃ on the whole absorbent can be achieved.
In the absorption unit, the flue gas enters from the lower part of the absorption unit and then reversely contacts with the absorbent which flows downwards in the top jet flow of the absorption unit at the filler section to generate chemical reaction to form weak link compounds, thereby realizing CO in the flue gas2And (4) removing. The interstage cooling device cools after partially or completely collecting the absorbent, and the cooled absorbent is used for reversely contacting with the flue gas, so that the reaction temperature can be reduced, and the CO is improved2I.e. increase the solubility of carbon dioxide in the absorbent.
The absorption unit also comprises a demisting device arranged at the upper part of the absorption unit.
The filler section includes that filler and filler skin set up prevent wall flow hoop, and the filler includes the stainless steel buckled plate of both sides and a plurality of layers of plastics buckled plate in the middle of, and adjacent plastics buckled plate is according to the mutual staggered arrangement of ripple direction, the micron porous structure has on the surface of plastics buckled plate. The plastic corrugated plate is prepared by adopting plastics such as polypropylene, polyethylene and the like as matrixes and adding 5-60 wt.% of hydrophilic modification materials such as polypropylene grafted maleic anhydride and the like.
The pollutant control unit comprises a water balance device and a secondary washing device which are arranged in series, and the flue gas is exhausted after being treated by the water balance device and the secondary washing device in sequence; the water balance device is provided with a water washing cooler, and the water washing cooler is used for controlling the temperature of the flue gas treated by the flue gas pretreatment unit to be consistent with the temperature of the flue gas treated by the primary water washing device.
The water balance device is used for coarseThe second-stage water washing device is used for fine removal, and CO is removed through the absorption unit2The flue gas passes through the water balance device and the secondary water washing device in sequence.
The water washing cooler can control the temperature of the flue gas cooled by the flue gas pretreatment unit and subjected to desulfurization and denitrification to be consistent with the temperature of the flue gas treated by the water balance device by increasing the circulating flow of the water washing liquid in the water balance device or reducing the temperature.
The water washing liquid in the water balance device is high amine water washing liquid, and the water washing liquid in the secondary water washing device is low amine water washing liquid; when the content of the amine in the exhausted flue gas is detected to be ultrahigh, the high-amine water washing liquid of the water balance device can be used as the supplementary water of the absorbent in the absorption unit, and meanwhile, the low-amine water washing liquid in the secondary water washing device is sent to the water balance device, so that the content of the amine is regulated and controlled.
The low-pressure rich liquid flash evaporation unit comprises an equal Reynolds number plate type lean and rich liquid heat exchanger unit, a gas-liquid separator and a heat recovery device, the absorbent rich liquid is sequentially heated by the equal Reynolds number plate type lean and rich liquid heat exchanger unit, the gas-liquid separator performs gas-liquid separation, the separated gas directly enters the rich liquid shunting desorption unit, and the separated liquid is further heated by the heat recovery device and then enters the rich liquid shunting desorption unit.
Wherein, the rich absorbent solution can generate CO when being heated by the equal Reynolds number plate type lean and rich solution heat exchanger unit2And water vapor, and meanwhile, when the Reynolds number plate type lean-rich liquid heat exchanger unit operates at low pressure, a certain gas-liquid separation effect is achieved, and further separation is carried out through a gas-liquid separator; and sending the separated gas into a rich liquid shunting desorption unit through a compressor. The gas-liquid separator may be a flash tank. The heat recovery device further exchanges heat with the rich absorbent solution through a reboiler, such as a plate-type falling film reboiler.
The equal Reynolds number plate type lean and rich liquid heat exchanger unit comprises an absorbent lean liquid side and an absorbent rich liquid side, and the operating pressure of the absorbent rich liquid side is 1.0-1.8 bar.
The flow number of the rich liquid side of the absorbent is larger than that of the lean side of the absorbent, and the equal Reynolds numbers of the rich liquid side of the absorbent and the lean liquid side of the absorbent are operated.
The invention increases the liquid phase flow rate of the absorbent through increasing the flow of the rich liquid side of the absorbent, further improves the Raynaud number Re and the convective heat transfer coefficient of the lean liquid side of the absorbent, and can avoid the thermal resistance caused by low flow and high viscosity of the rich liquid side of the absorbent.
The rich liquid shunting desorption unit comprises a diverter and a reducing desorption tower, the absorbent rich liquid is shunted into an absorbent rich liquid main flow and an absorbent rich liquid shunt under the action of the diverter, the absorbent rich liquid main flow sequentially passes through the low-pressure rich liquid flash evaporation unit and the rich liquid shunting desorption unit to regenerate the absorbent, and the absorbent rich liquid shunt directly enters the rich liquid shunting desorption unit to regenerate the absorbent.
Specifically, in the invention, the rich absorbent liquid is shunted and directly enters the reducing desorption tower, so that the temperature of the regenerated gas can be reduced, and the latent heat of vaporization can be recovered. The rich liquid diversion desorption unit further comprises a diverter, and the diverter can control the flow of the absorbent rich liquid diversion through a diverter pump. Wherein the flow rate of the divided absorbent rich solution is 5-15% of the main absorbent rich solution flow.
And desorbing the absorbent rich solution by a desorption section to generate absorbent barren solution and regenerated gas, wherein the absorbent barren solution enters an absorption unit, and the regenerated gas enters a regenerated gas heat recovery section.
The reducing desorption tower comprises a regenerated gas heat recovery section at the upper part and a desorption section at the lower part, the diameter of the regenerated gas heat recovery section is 40-85% of that of the desorption section, and the height of a filler in the reducing desorption tower is 1.5-5D (D is the inner diameter of the reducing absorption tower).
In the invention, the diameter-variable desorption tower is adopted, and the diameter variation is beneficial to the distribution of the rich liquid of the absorbent, thereby improving the heat transfer and mass transfer effects.
The rich liquid of the absorbent is heated in the desorption section to carry out reverse reaction to release CO2The regeneration gas also comprises CO generated by rich liquid of the absorbent when the equal Reynolds number plate type lean-rich liquid heat exchanger unit is heated2And water vapor. The rich liquid of the absorbent is changed by the reducing desorption tower to realize the regeneration of the absorbent, and the generated absorptionAnd the lean solution of the absorbent enters the lower part of the absorption unit after being cooled by the lean solution side of the absorption agent of the equal Reynolds number plate type lean and rich solution heat exchanger unit.
The flue gas CO2The trapping device also comprises a regeneration gas unit, wherein the regeneration gas enters the regeneration gas unit after being subjected to heat absorption through a regeneration gas heat recovery section and then is subjected to gas-liquid separation to generate CO2Condensing the product gas and the regeneration gas. CO after gas-liquid separation in regeneration gas unit2Sending the liquid into a subsequent treatment process, and sending the liquid back to the rich liquid grading flow through a condensate pump. When the content of amine in the evacuated flue gas is monitored to be ultrahigh, the low-amine water washing liquid in the secondary washing device is sent to the water balance device, and then the regenerated gas condensate water can be sent to the secondary washing device to be used as the washing liquid.
In the invention, the temperature of the flue gas at the outlet of the flue gas pretreatment unit is 30-50 ℃, the working temperature of the absorption unit is 30-70 ℃, and the working temperature of the desorption section is 100-130 ℃.
The invention mainly aims at the existing CO2The problems of overhigh energy consumption and secondary pollution emission of a capture system are solved, and the low-energy-consumption and low-emission CO is provided2A capture system. According to the system, the rich liquid shunting desorption unit and the low-pressure rich liquid flash evaporation unit are adopted, so that the high-efficiency recovery of heat during the operation of the system is realized, and the energy consumption during the operation of the system is reduced. Meanwhile, two-stage water washing and comprehensive utilization of the regenerated gas condensate water are combined, so that the aims of reducing pollution emission and maintaining the water balance of the system are fulfilled.
Compared with the prior art, the invention has the following beneficial effects:
1. flue gas is washed by two stages after being separated from the absorption unit, and the concentration of washing liquid amine in the two stages of washing towers is maintained at a lower level by matching with an amine regulation and control loop, so that the pollutant control effect can be obviously improved.
2. The flue gas pretreatment unit separates two processes of cooling dust removal and SOx/NOx control of flue gas, can effectively avoid the problem that alkali lye is diluted by moisture in the flue gas, can recycle moisture in the flue gas simultaneously.
3. In the absorption unit provided by the invention, the filler section adopts plastic filler as a hydrophilic material, and micron-sized porous knots are processed on the surfaceThe hydrophilicity of the filler is increased, and the wall flow prevention hoop is arranged on the outer layer of the filler to improve the liquid flow condition and further improve the mass transfer effect of the filler; meanwhile, the four layers of corrugated plates on the outer side are reinforced by stainless steel materials and through nails, so that the filler strength is ensured, and the filler investment cost is reduced by 50%. The interstage cooling device can reduce the reaction temperature and make CO2The reaction of the absorption process proceeds more thoroughly.
4. The rich liquid shunting desorption unit provided by the invention increases the liquid spraying density of the section of the filler and the air velocity of the empty tower by reducing the tower diameter of the section of the filler on the top of the tower, enhances the gas-liquid heat transfer effect and improves the recovery of the latent heat of moisture in the regenerated gas.
5. According to the low-pressure rich liquid flash evaporation unit provided by the invention, the gas after gas-liquid separation sweeps the desorption section through the compressor, so that the desorption process can be obviously promoted; meanwhile, the temperature of the rich liquid after gas-liquid separation is reduced, and more waste heat of the steam condensate water can be recovered.
6. Different processes are arranged on the hot side/cold side of the equal Reynolds number plate type lean and rich liquid heat exchanger unit, so that equal Reynolds numbers on two sides are guaranteed to operate, the heat exchange coefficient of the heat exchanger can be effectively improved, the heat exchange end difference is reduced, and the temperature of a rich liquid inlet is improved.
Drawings
FIG. 1 shows CO provided by the present invention2A schematic structural diagram of the capture system;
the system comprises a flue gas pretreatment unit, a cold water pump, a lye pump, a condensate water cooler, an absorption unit, a semi-rich liquid pump, a 7 interstage cooler, a 8 water balance device, a 9 water balance water washing pump, a 10 water washing cooler, a 11 secondary water washing device, a 12 secondary water washing pump, a 13 graded flow pump, a 14 flash tank, a 15 compressor, a 16 desorption section, a 17 regeneration gas heat recovery section, a 18 plate-type falling film reboiler, a 19 rich liquid pump, a 20 heat recovery device, a 21 equal Reynolds number plate-type lean and rich liquid heat exchanger unit, a 22 lean liquid pump, a 23 regeneration gas cooler, a 24 regeneration gas separator, a 25, a regeneration gas condensate water pump, a 26 fan, a 1001 power plant flue gas inlet, a 1002 decarbonization flue gas outlet, a 1003 regeneration gas, 1004, CO, a CO gas inlet and a heat recovery device, wherein the regeneration gas heat recovery device is connected with the heat recovery device, and the regeneration gas heat2Product gas, 1005, rich liquidFractional flow, 1006, rich liquid main flow, 1007, steam inlet, 1008, steam condensate outlet, 1009 water cooling tower water replenishing outlet, 1010, absorbent barren liquid, 1011, high amine water washing liquid, 1012, low amine water washing liquid, 1013, regeneration gas condensate.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail with reference to the accompanying drawings and examples. It should be understood that the detailed description and specific examples, while indicating the scope of the invention, are intended for purposes of illustration only and are not intended to limit the scope of the invention.
As shown in figure 1, the flue gas CO provided by the invention2The trapping system includes: the device comprises a flue gas pretreatment unit 1, an absorption unit 5, a pollutant control unit, a rich solution shunting desorption unit and a low-pressure rich solution flash evaporation unit; the flue gas is evacuated after sequentially passing through the flue gas pretreatment unit, the absorption unit and the pollutant control unit, the absorbent rich liquid generated by the absorption unit is sequentially subjected to low-pressure rich liquid flash evaporation unit and rich liquid shunting desorption unit to regenerate the absorbent, and the regenerated absorbent enters the absorption unit.
The flue gas pretreatment unit 1 includes: the flue gas cooling section and SOx/NOx control section that set up from bottom to top, the flue gas is at flue gas cooling section cooling and dust removal in proper order, enters into the lower part of absorption unit after SOx/NOx control section carries out SOx/NOx control. Wherein, the desulfurization and denitrification section is mainly formed by alkali liquor (NaOH and Na)2CO3) And (6) leaching. Specifically, a cold water pump 2, a cooler 4 and a cold water tower water supplement outlet 1009 are arranged at the lower part of the flue gas pretreatment unit 1, and condensed water generated at the flue gas cooling section is cooled by the cold water cooler 4 and then is recycled by the cold water pump 2 or is discharged by the cold water pump water supplement outlet 1009.
The flue gas pretreated by the flue gas pretreatment unit 1 is sent to the lower part of the absorption unit 5 by a fan 26.
The absorption unit 5 includes: a filler section and an interstage cooling device arranged at the middle section of the absorption unit, wherein the flue gas is subjected to CO removal after being in reverse contact with the absorbent at the filler section2Removing CO2The flue gas enters a pollutant control unit, and an absorbent is cooled by an interstage cooling deviceThen enters the packing section to reversely contact with the flue gas. The absorption unit 5 further comprises a demister arranged at the upper part of the absorption unit.
The interstage cooling device comprises an upper liquid collector, a middle interstage cooler and a lower liquid redistributor, wherein the liquid collector collects part or all of the absorbent, the liquid collector cools the absorbent through the interstage cooler and then sends the absorbent into the liquid redistributor, and the liquid redistributor fills the cooled absorbent into a section. The liquid collector pumps the absorbent (absorbent absorbing part of carbon dioxide, which can be called absorbent semi-rich liquid) into the interstage cooler 7 through the semi-rich liquid to cool, and then the absorbent is sent into the liquid redistributor after cooling, and the absorbent is sent into the filling section again through the liquid redistributor to reduce the reaction temperature and improve the CO in the flue gas2The absorption capacity of (1).
Wherein, the filler section includes the filler and prevents the wall flow hoop that the outer layer of filler set up, and the filler includes the stainless steel buckled plate of both sides and a plurality of layers of plastics buckled plate in the middle of, and adjacent plastics buckled plate is according to the mutual staggered arrangement of ripple direction, and the surface of plastics buckled plate has micron porous structure. The plastic corrugated plate is prepared by taking plastics such as polypropylene, polyethylene and the like as a substrate and adding 5-60 wt.% of hydrophilic modification materials such as polypropylene grafted maleic anhydride and the like.
The pollutant control unit comprises a primary water washing device 8 and a secondary water washing device 11 which are arranged in series, and the flue gas is treated by the water balance device 8 and the secondary water washing device 11 in sequence and then is emptied; the water balance device is provided with a water washing cooler 10, and the water washing cooler 10 can be used for controlling the temperature of the flue gas cooled by the flue gas pretreatment unit 1 and subjected to desulfurization and denitrification to be consistent with the temperature of the flue gas treated by the water balance device 8 by increasing the circulating flow rate or reducing the temperature of the water washing liquid in the water balance device 8.
The water washing liquid in the water balance device 8 is high amine water washing liquid, and the water washing liquid in the secondary water washing device 11 is low amine water washing liquid; when the content of amine in the exhausted flue gas is detected to be ultrahigh, the high amine water washing liquid 1011 of the water balance device 8 can be used as supplementary water of the absorbent in the absorption unit 5 through the water balance washing pump 9, and meanwhile, the low amine water washing liquid 1012 in the secondary washing device 11 is sent to the secondary washing device 11 through the secondary washing pump 12, so that the content of amine can be regulated and controlled.
The low pressure rich liquid flash unit comprises: the equal reynolds number plate type lean and rich liquid heat exchanger unit 21, the gas-liquid separator (specifically the flash tank 14) and the heat recovery device 20 (including the plate falling film reboiler 18), the absorbent rich liquid is sequentially heated by the equal reynolds number plate type lean and rich liquid heat exchanger unit 21, the gas-liquid separator performs gas-liquid separation, the separated gas is sent to the rich liquid shunting desorption unit through the compressor 15, and the separated liquid enters the rich liquid shunting desorption unit after further heat exchange through the heat recovery device 20. The operation pressure of the rich liquid side of the absorbent is 1.0-1.8 bar, and the flow number of the rich liquid side of the absorbent is larger than that of the lean side of the absorbent.
The rich liquid shunting and desorbing unit comprises a splitter and a reducing desorbing tower, the absorbent rich liquid is shunted into an absorbent rich liquid main stream 1006 and an absorbent rich liquid shunting stream 1005 under the action of the splitter (such as a graded flow pump 13), the absorbent rich liquid main stream 1006 passes through the low-pressure rich liquid flash evaporation unit and the rich liquid shunting and desorbing unit in sequence to regenerate the absorbent, and the absorbent rich liquid shunting stream 1005 directly enters the rich liquid shunting and desorbing unit. Wherein, the flow rate of the absorbent rich liquid shunt 1005 is 5-15% of the absorbent rich liquid main flow 1006. The diameter-variable desorption tower comprises a regenerated gas heat recovery section 17 at the upper part and a desorption section 16 at the lower part, the diameter of the regenerated gas heat recovery section 17 is 40-85% of the diameter of the desorption section 16, and the height of a filler in the diameter-variable desorption tower is 1.5-5D.
Flue gas CO2The trapping device also comprises a regeneration gas unit, wherein the regeneration gas enters the regeneration gas unit after being subjected to heat absorption through a regeneration gas heat recovery section 17 and then is subjected to gas-liquid separation to generate CO2Product gas and regeneration gas condensate (specifically, through regeneration gas cooler 23 and regeneration gas separator 24). CO after gas-liquid separation in regeneration gas unit2The liquid is sent to the subsequent treatment process, and the liquid is sent back to the rich liquid graded flow 1005 by a regeneration gas condensate pump 25. When the content of amine in the exhausted flue gas is detected to be ultrahigh, the low-amine water washing liquid in the secondary water washing device 11 is sent to the primary water washing device 8, and then the regenerated gas condensed water 1013 is sent to the secondary water washing device to be used as a water washing liquid.
The invention provides flue gas CO2The operation of the trapping system is as follows:
flue gas flow: the high-temperature wet saturated flue gas 1001 firstly enters the flue gas pretreatment unit 1, is cooled in the flue gas cooling section and then contacts with alkali liquor for desulfurization and denitrification, and then is dragged by the fan 26 to be sent into the absorption unit 5, the flue gas enters from the lower part of the absorption unit 5, and the filler section in the absorption unit 5 is in reverse contact with the absorbent which flows downwards in a jet flow manner from the top of the absorption unit. CO in flue gas2Chemically reacting with absorbent to form weak bonded compound and remove CO2The flue gas is discharged from the upper part of the absorption unit, and passes through a water balance device 8 and a secondary water washing device 11 in sequence, so that the absorbent and the degradation products thereof carried in the flue gas are recovered, and finally the decarbonized flue gas 1002 is emptied.
And (3) circulation of an absorbent: the absorbent barren solution 1010 is conveyed to the top of the absorption unit 5, is sent to an interstage cooler 7 by a semi-rich solution pump 6 for cooling after reacting with the flue gas at the upper part of the absorption unit 5, and then is sent to the absorption unit 5 at the lower part, and the bottom of the absorption unit 5 is rich in CO2The absorbent flows out in two ways under the pressure of the absorption unit, the graded flow 1005 of the rich liquid of the absorbent directly enters the top of the desorption section 16 through the graded flow pump 13, the main flow 1006 of the rich liquid of the absorbent is preheated by the equal Reynolds number plate type lean rich liquid heat exchanger 21 and then flashed in the flash tank 14, the flashed gas is sent to the tower bottom of the desorption section 16 through the compressor 15, the rich liquid after flashing is further subjected to heat exchange in the heat recovery device 20 through the rich liquid pump 19 (the heat recovery device 20 is provided with a steam condensate water outlet 1008), and then the rich liquid is sent to the desorption section 16 for regeneration. The tower kettle of the desorption section is heated by a plate-type falling film reboiler 18 (a steam inlet 1007 is arranged on the plate-type falling film reboiler 18), and rich liquid is heated in the desorption section 16 to carry out reverse reaction to release CO2The absorbent regenerated at the bottom of the desorption section 16 is cooled by the equal reynolds number plate type lean-rich liquid heat exchanger 21 under the action of the lean liquid pump 22 and then returns to the top of the absorption unit 5, and one-time absorbent circulation is completed.
Pretreatment tower and water washing circulation: the upper filling section of the group flue gas pretreatment unit 1 is used for leaching alkali liquor, the alkali liquor finishes self-circulation through an alkali liquor pump 3, the lower part of the group flue gas pretreatment unit is used for washing, cooling and spraying driven by a cooling water pump 2, and cooling condensate water in flue gas is used as make-up water 1009 of a cooling tower; the washing liquid in the water balance device 8 completes self-circulation through a first-stage washing pump 9 and a washing cooler 10; the washing liquid in the secondary washing device 11 completes self circulation through a secondary washing pump 12.
A regeneration gas flow path: the regeneration gas generated in the desorption section 16 is directly contacted with the cold absorbent rich liquid graded flow 1005 for temperature reduction in the regeneration gas heat recovery section 17, and then is further cooled by the regeneration gas cooler 23, the cooled regeneration gas 1003 is subjected to gas-liquid separation in the regeneration gas separator 24, and CO is separated from the gas2The product gas 1004 is sent to the subsequent treatment process, and the regenerated gas condensate is sent back to the absorbent rich liquid fractional flow 1005 by the condensate pump 25.
Amine regulation: when the content of the amine in the outlet flue gas is detected to be ultrahigh, starting the high amine water washing liquid of the water balance device 8 to flow back 1011 to be used as absorbent supplementing water; then, the secondary washing device 11 is started to return 1012 the low-amine washing liquid and send the low-amine washing liquid into the water balance device 8; and after the supplement is finished, the regenerated gas condensate water regulating and controlling loop is opened, and the regenerated gas condensate water 1013 is used as washing liquid of the secondary washing device 11 for supplement.
The above-mentioned embodiments are intended to illustrate the technical solutions and advantages of the present invention, and it should be understood that the above-mentioned embodiments are only the most preferred embodiments of the present invention, and are not intended to limit the present invention, and any modifications, additions, equivalents, etc. made within the scope of the principles of the present invention should be included in the scope of the present invention.
Claims (3)
1. Flue gas CO with low regeneration energy consumption and low pollutant emission2A capture device, characterized in that the flue gas CO2The trapping device comprises a flue gas pretreatment unit, an absorption unit, a pollutant control unit, a rich solution shunting desorption unit and a low-pressure rich solution flash evaporation unit; the flue gas is evacuated after sequentially passing through a flue gas pretreatment unit, an absorption unit and a pollutant control unit, an absorbent rich solution generated by the absorption unit is regenerated by sequentially passing through a low-pressure rich solution flash evaporation unit and a rich solution shunting desorption unit, and the regenerated absorbent returns to the absorption unit;
the pollutant control unit comprises a water balance device and a secondary washing device which are arranged in series, and the flue gas is exhausted after being treated by the water balance device and the secondary washing device in sequence; the water balance device is provided with a water washing cooler, and the water washing cooler is used for controlling the temperature of the flue gas treated by the flue gas pretreatment unit to be consistent with the temperature of the flue gas treated by the primary water washing device;
the flue gas pretreatment unit comprises a flue gas cooling section and a desulfurization and denitrification section which are arranged from bottom to top, and the flue gas is sequentially cooled and dedusted in the flue gas cooling section and enters the lower part of the absorption unit after being desulfurized and denitrated in the desulfurization and denitrification section;
the rich liquid shunting desorption unit comprises a diverter and a reducing desorption tower, the absorbent rich liquid is shunted into an absorbent rich liquid main flow and an absorbent rich liquid shunt under the action of the diverter, the absorbent rich liquid main flow sequentially passes through the low-pressure rich liquid flash evaporation unit and the rich liquid shunting desorption unit to regenerate the absorbent, and the absorbent rich liquid shunt directly enters the rich liquid shunting desorption unit to regenerate the absorbent;
the reducing desorption tower comprises a regenerated gas heat recovery section at the upper part and a desorption section at the lower part, the diameter of the regenerated gas heat recovery section is 40-85% of that of the desorption section, the height of a filler in the reducing desorption tower is 1.5-5D, and D is the inner diameter of the reducing absorption tower;
the low-pressure rich liquid flash evaporation unit comprises an equal Reynolds number plate type lean and rich liquid heat exchanger unit, a gas-liquid separator and a heat recovery device, the absorbent rich liquid is sequentially heated by the equal Reynolds number plate type lean and rich liquid heat exchanger unit, the gas-liquid separator performs gas-liquid separation, the separated gas directly enters the rich liquid shunting desorption unit, and the separated liquid further exchanges heat by the heat recovery device and then enters the rich liquid shunting desorption unit;
the equal Reynolds number plate type lean and rich liquid heat exchanger unit comprises an absorbent lean liquid side and an absorbent rich liquid side, and the operating pressure of the absorbent rich liquid side is 1.0-1.8 bar;
the flow number of the rich liquid side of the absorbent is larger than that of the lean liquid side of the absorbent, and the equal Reynolds numbers of the rich liquid side of the absorbent and the lean liquid side of the absorbent are operated.
2. The flue gas CO with low regeneration energy consumption and low pollutant emission according to claim 12The capture device is characterized in that the absorption unit comprises a packing section and an interstage cooling device arranged in the middle section of the absorption unit, and the flue gas is subjected to CO removal after being in countercurrent contact with the absorbent in the packing section2Said removal of CO2The flue gas enters a pollutant control unit, and the absorbent enters a filling section after being cooled by an interstage cooling device.
3. The flue gas CO with low regeneration energy consumption and low pollutant emission according to claim 22The capture device is characterized in that the interstage cooling device comprises an upper liquid collector, a middle interstage cooler and a lower liquid redistributor, the liquid collector collects part or all of the absorbent, the absorbent is cooled by the interstage cooler and then is sent to the liquid redistributor, and the liquid redistributor sends the cooled absorbent to the filling section.
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| CN113877365A (en) * | 2020-07-03 | 2022-01-04 | 中石化石油工程技术服务有限公司 | CO2Trapping system and process |
| CN112774401A (en) * | 2021-01-05 | 2021-05-11 | 中国神华能源股份有限公司国华电力分公司 | Novel flue gas CO2Regeneration process of trapping system |
| CN113101786B (en) * | 2021-05-10 | 2022-06-28 | 浙江浙能技术研究院有限公司 | Flue gas carbon dioxide capture system and method based on organic solvent absorption-extraction regeneration cycle |
| CN113521966A (en) * | 2021-07-26 | 2021-10-22 | 浙江大学 | Partitioned multistage circulation CO based on mass transfer-reaction regulation2Trapping and concentrating method |
| DE102021214786A1 (en) | 2021-12-21 | 2023-06-22 | Thyssenkrupp Ag | Carbon Dioxide Separation Device |
| DE102021214785A1 (en) | 2021-12-21 | 2023-06-22 | Thyssenkrupp Ag | Carbon Dioxide Separation Device |
| BE1030055B1 (en) | 2021-12-21 | 2023-07-19 | Thyssenkrupp Ind Solutions Ag | Carbon Dioxide Separation Device |
| WO2023117705A1 (en) | 2021-12-21 | 2023-06-29 | Thyssenkrupp Industrial Solutions Ag | Carbon dioxide separation apparatus |
| WO2023117704A1 (en) | 2021-12-21 | 2023-06-29 | Thyssenkrupp Industrial Solutions Ag | Carbon dioxide separation device |
| BE1030056B1 (en) | 2021-12-21 | 2023-07-19 | Thyssenkrupp Ind Solutions Ag | Carbon Dioxide Separation Device |
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