CN114682042A - Ship tail gas treatment system and treatment method thereof - Google Patents
Ship tail gas treatment system and treatment method thereof Download PDFInfo
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- CN114682042A CN114682042A CN202210184246.3A CN202210184246A CN114682042A CN 114682042 A CN114682042 A CN 114682042A CN 202210184246 A CN202210184246 A CN 202210184246A CN 114682042 A CN114682042 A CN 114682042A
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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
- B01D53/002—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 condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D7/00—Sublimation
- B01D7/02—Crystallisation directly from the vapour phase
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
Abstract
The invention discloses a ship tail gas treatment system, which comprises a tail gas pretreatment system, a low-temperature desublimated carbon capture system, a melting pressurization system, a rectification purification system, a main cooling system and an isopentane circulating heat exchange system, wherein external flue gas is connected with the tail gas pretreatment system through a conveying pipeline, the tail gas pretreatment system and the melting pressurization system are respectively connected with the low-temperature desublimated carbon capture system, the rectification purification system and the isopentane circulating heat exchange system are respectively connected with the melting pressurization system, the rectification purification system is connected with the isopentane circulating heat exchange system, the low-temperature desublimated carbon capture system and the melting pressurization system are respectively connected with the main cooling system, and external clean air is connected with the low-temperature desublimated carbon capture system through the conveying pipeline. And its processing method are also disclosed. The invention can realize compact, efficient and economic carbon dioxide capture by combining the ship tail gas with the existing energy system, and has the advantages of small volume, high efficiency, low energy consumption, easy modification, low cost and the like.
Description
Technical Field
The invention relates to the technical field of ship tail gas and waste gas treatment, in particular to a ship tail gas treatment system and a treatment method thereof.
Background
A large amount of flue gas emission can be produced in the shipping and wharf shipping operations, and after the ship tail gas is subjected to desulfurization, denitrification and dehydration treatment, the tail gas contains a large amount of nitrogen, carbon dioxide, various hydrocarbon substances, oxygen, flue gas particulate matters and the like, and has complex components and huge treatment gas amount. Under the background of global coping with climate change, in order to achieve the preliminary strategic target of greenhouse gas emission reduction and the carbon neutralization target in 2060 years in China, the international society has deeply recognized the severe situation facing the emission reduction of the greenhouse gas in the shipping industry. CO in ship tail gas2The amount of concentrated discharge is enormous, and therefore, CO is developed2The carbon emission reduction scheme taking the large-scale utilization technology as the core can bring huge carbon emission reduction potential and economic benefit, but no mature scheme exists at present, and the problem to be solved urgently is solved.
Disclosure of Invention
The purpose of the invention is as follows: in view of the above problems, the present invention provides a ship tail gas treatment system to realize CO in ship tail gas2Large-scale emission reduction, economic benefit improvement and environmental friendliness. And provides a processing method thereof.
The technical scheme is as follows: the utility model provides a ship tail gas processing system, including tail gas pretreatment system, low temperature sublimation carbon entrapment system, the melting charge system, the rectification purification system, main cooling system, isopentane circulation heat transfer system, external flue gas passes through pipeline and tail gas pretreatment system is connected, tail gas pretreatment system, the melting charge system respectively with low temperature sublimation carbon entrapment headtotail, the rectification purification system, isopentane circulation heat transfer system respectively with melting charge headtotail, the rectification purification system is connected with isopentane circulation heat transfer system, low temperature sublimation carbon entrapment system, the melting charge system is connected with main cooling system respectively, external clean air passes through pipeline and low temperature sublimation carbon entrapment headtotail.
Further, the tail gas pretreatment system comprises a first pneumatic regulating valve, a flue gas blower, a precooler and a dryer, wherein an external flue gas conveying pipeline is connected with an inlet of the first pneumatic regulating valve, a first flow meter is arranged at the joint of the first pneumatic regulating valve and the first pneumatic regulating valve, an outlet of the first pneumatic regulating valve is connected with an inlet of the flue gas blower, an outlet of the flue gas blower is connected with a hot end inlet M-1 of the precooler, a hot end outlet M-2 of the precooler is connected with an inlet of the dryer, a cold end inlet M-3 of the precooler is connected with an outlet of an external refrigerant conveying pipeline, and a cold end outlet M-4 of the precooler is connected with an inlet of the external refrigerant conveying pipeline.
Further, the low-temperature desublimated carbon capturing system comprises a flue gas heat exchanger and a desublimated heat exchanger, wherein an inlet A-3 of the flue gas heat exchanger is connected with the tail gas pretreatment system, an outlet A-4 of the flue gas heat exchanger is connected with a gas phase inlet B-1 of the desublimated heat exchanger, a gas phase outlet B-2 of the desublimated heat exchanger is connected with an inlet A-1 of the flue gas heat exchanger, an outlet A-2 of the flue gas heat exchanger is communicated with an outlet of an external clean air conveying pipeline, a carbon dioxide gas detector is arranged between the outlet A-2 and the outlet B-1 of the desublimated heat exchanger, a slurry outlet B-4 of the desublimated heat exchanger is connected with a melting pressurization system, an inlet B-3 of the desublimated heat exchanger is connected with a main cooling system, and an inlet B-5 of the desublimated heat exchanger is connected with an isopentane circulating heat exchange system.
Further, the melting pressurization system comprises a slurry pump, a solid-liquid separator, a screw booster, a high-speed centrifugal pump, a condenser, an electric heater, a first three-way regulating valve and a second three-way regulating valve, wherein the inlet of the slurry pump is connected with the low-temperature desublimed carbon capture system, the outlet of the slurry pump is connected with the slurry inlet C-1 of the solid-liquid separator, the second outlet C-3 of the solid-liquid separator is connected with the first inlet F-1 of the screw booster, the outlet F-3 of the screw booster is connected with the inlet of the high-speed centrifugal pump, the outlet of the high-speed centrifugal pump is connected with the cold-end inlet G-1 of the condenser, the cold-end outlet G-2 of the condenser is connected with the inlet of the electric heater, the outlet of the electric heater is connected with the inlet of the second three-way regulating valve, the first outlet N-2 of the second three-way regulating valve is connected with the second inlet F-2 of the screw booster, and a second outlet N-3 of the second three-way regulating valve is connected with the rectification and purification system, a first outlet C-2 of the solid-liquid separator is connected with an inlet D-1 of the first three-way regulating valve, a first outlet D-2 of the first three-way regulating valve is connected with the main cooling system, and a second outlet D-3 of the first three-way regulating valve is connected with the isopentane circulating heat exchange system.
Further, the rectification purification system comprises a preheater, a rectification tower and CO2Liquid pump, gas-liquid separator and liquid CO2The Dewar flask, the second pneumatic control valve, the first seawater condenser, the separating tank and the tower kettle reboiler, a second outlet N-3 of the second three-way control valve is connected with a cold end inlet H-1 of the preheater, a cold end outlet H-2 of the preheater is connected with a feed inlet I-1 of the rectifying tower, an outlet I-2 of the rectifying tower is connected with an inlet of the first seawater condenser, an outlet of the first seawater condenser is connected with an inlet P-1 of the separating tank, a first outlet P-2 of the separating tank is connected with an inlet I-3 of the rectifying tower, a second outlet P-3 of the separating tank is connected with a melting pressurization system, and CO is mixed with the gas2The inlet of the liquid pump is connected with an isopentane circulating heat exchange system, and CO is2The liquid pump is connected with an inlet L-1 of the gas-liquid separator, an outlet L-2 of the gas-liquid separator is connected with a feed inlet I-4 of the rectifying tower, and an outlet L-3 of the gas-liquid separator is connected with the liquid CO through a second pneumatic regulating valve2The dewar bottle is connected, a second flowmeter is arranged between the gas-liquid separator and the second pneumatic regulating valve, an outlet I-5 of the rectifying tower is connected with an inlet Q-1 of the tower kettle reboiler, an outlet Q-2 of the tower kettle reboiler is connected with a feed inlet I-6 of the rectifying tower, an outlet Q-3 of the tower kettle reboiler is connected with an inlet H-3 at the hot end of the preheater, and an outlet H-4 at the hot end of the preheater is connected with an isopentane circulating heat exchange system.
Furthermore, the main cooling system comprises a main cooler, an external cold source system or an external cold source system II, an inlet E-3 of the cold end of the main cooler is connected with the external cold source system or an outlet of the external cold source system II, an outlet E-4 of the cold end of the main cooler is connected with the external cold source system or an inlet of the external cold source system II, an inlet E-1 of the main cooler is connected with the melting pressurization system, and an outlet E-2 of the main cooler is connected with the low-temperature desublimated carbon capture system.
Preferably, the external cold source system comprises an LNG storage tank, a check valve, an LNG transfer pump, a first one-way stop valve, a second one-way stop valve, a spray nozzle, a control valve, a seawater rewarming device and a marine engine host, the system comprises an air pump and an air flow regulating valve, the LNG storage tank stores LNG fuel, a spray nozzle is installed on the LNG storage tank, a check valve, an LNG delivery pump, a first one-way stop valve, a second one-way stop valve and the spray nozzle are sequentially connected to form a loop, a control valve is arranged between the first one-way stop valve and the second one-way stop valve and connected with a cold end inlet E-3 of a main cooler, a marine engine host is connected with a cold end outlet E-4 of the main cooler through a seawater rewarming device, the air pump is connected with the marine engine host through the air flow regulating valve, and flue gas combusted by the marine engine host enters a tail gas pretreatment system from an external flue gas delivery pipeline.
Preferably, the external cold source system II comprises a nitrogen expander, a nitrogen circulating heat exchanger, a nitrogen compressor and a second seawater condenser, wherein an outlet of the nitrogen expander is connected with an inlet E-5 of the main cooler, an inlet I-1 of the nitrogen circulating heat exchanger is connected with an outlet E-6 of the main cooler, an outlet I-2 of the nitrogen circulating heat exchanger is connected with an inlet of the nitrogen compressor, an outlet of the nitrogen compressor is connected with an inlet I-3 of the nitrogen circulating heat exchanger through the second seawater condenser, an inlet I-4 of the circulating heat exchanger is connected with a cold-end inlet E-3 of the main cooler, and a cold-end outlet E-4 of the main cooler is connected with an inlet of the nitrogen expander.
Preferably, the isopentane circulating heat exchange system comprises a cooler, an inlet J-1 and a hot end inlet J-3 of the cooler are respectively connected with the melting pressurization system, a hot end outlet J-4 of the cooler is connected with the rectification purification system, and the low-temperature desublimated carbon capture system is connected with an outlet J-2 of the cooler.
The tail gas treatment method of the ship tail gas treatment system comprises the following steps:
step (a): the method comprises the following steps that external high-temperature flue gas enters a tail gas pretreatment system through a conveying pipeline, dynamic pressure of the flue gas is increased and precooled, the precooled flue gas is further dried in the tail gas pretreatment system and then enters a low-temperature desublimated carbon capture system, and cold energy is absorbed in the low-temperature desublimated carbon capture system;
step (b): the main cooling system sends the low-temperature liquid isopentane absorbing the cold energy of the cold source into a low-temperature desublimated carbon capture system, the isopentane exchanges heat with carbon dioxide in the flue gas in the low-temperature desublimated carbon capture system, and the carbon dioxide gas absorbing the cold energy is desublimated into carbon dioxide solid;
step (c): the decarbonized clean air flows out of the low-temperature desublimation carbon capture system after being reheated by the low-temperature desublimation carbon capture system, and is discharged out of the system after being reheated by a flue gas heat exchanger and the decarbonized tail gas is detected to reach the standard;
step (d): the mixed slurry of carbon dioxide solid and isopentane liquid in the low-temperature carbon sublimation capturing system flows into a melting pressurization system, part of the isopentane liquid enters a main cooling system through solid-liquid separation, returns to the low-temperature carbon sublimation capturing system after cold energy is absorbed through heat exchange, and part of the isopentane liquid enters an isopentane circulating heat exchange system and returns to the low-temperature carbon sublimation capturing system after the cold energy is released in the isopentane circulating heat exchange system;
a step (e): the carbon dioxide solid in the mixed slurry is gradually pressurized in the melting pressurization system and then is changed into carbon dioxide liquid, at the moment, a mixture of the residual isopentane liquid, the carbon dioxide liquid and the residual carbon dioxide solid exists in the melting pressurization system, wherein part of the mixed liquid is heated, refluxed and converged in the melting pressurization system to melt the residual carbon dioxide solid, the carbon dioxide solid of the residual undissolved fine particles is discharged from the melting pressurization system, and part of the mixed liquid is heated, heated and then enters a rectification and purification system;
a step (f): part of the mixed solution of the carbon dioxide and the isopentane is subjected to rectification reaction in a rectification purification system, the carbon dioxide liquid absorbs heat and then is vaporized, the purified carbon dioxide gas is liquefied again in the rectification purification system, the pure carbon dioxide gas which is not liquefied returns to a melting pressurization system, the ascending vapor phase and the descending liquid phase in the rectification purification system generate heat and mass transfer, the gas with higher temperature is partially liquefied, the liquid with lower temperature is partially vaporized, a small amount of isopentane component in the vapor phase enters the bottom of the rectification purification system, the carbon dioxide component in the liquid phase enters the vapor phase and reaches the top of the rectification purification system, in the process, the concentration of carbon dioxide at the top part is higher and higher, part of isopentane liquid with a small amount of carbon dioxide liquid in the rectification and purification system is rectified again, and the rest pure isopentane liquid flows out to enter a low-temperature desublimated carbon capture system after absorbing part of cold energy in the rectification and purification system;
step (g): the pure carbon dioxide gas absorbs cold energy in the melting pressurization system and then enters the isopentane circulating heat exchange system again to absorb the cold energy, part of the carbon dioxide gas is liquefied, after the carbon dioxide gas is pressurized by the rectification purification system, formed carbon dioxide liquid is collected in the rectification purification system, and the carbon dioxide gas which is not liquefied is purified again in the rectification purification system continuously.
Has the advantages that: compared with the prior art, the invention has the advantages that:
(1) because the system method does not realize pressurization on ineffective components in the flue gas, such as nitrogen and the like, the ineffective compression work is avoided, and therefore, the system method has lower energy consumption and lower electric power cost.
(2) Compared with the existing tail gas desulfurization water washing (FGD) device, a NOX Selective Catalytic Reduction (SCR) device and an alcohol amine solution absorption carbon capture (MDEA) device with relatively mature process, the invention greatly reduces the construction cost, can reform the existing tail gas treatment equipment according to different occasions such as specific ship types, engines, tail gas treatment processes and the like, and saves the equipment space.
(3) The scheme can adapt to the tail gas treatment occasions of LNG power ships and traditional fuel oil power ships, and has strong adaptability.
(4) Due to the operations of liquefaction separation, rectification purification and the like, the capability of carbon capture efficiency far higher than the industrial standard (90%) can be realized, and the highest purity can realize high-purity CO of 99.99%2。
(5) The invention not only can replace the existing tail gas desulfurization water washing (FGD) device, NOX Selective Catalytic Reduction (SCR) device and alcohol amine solution absorption carbon capture (MDEA) device with relatively mature technology of the ship, and efficiently and intensively realize the carbon capture and pollutant treatment functions, but also can fully utilize the LNG gasification cold energy of the LNG power ship for separating and purifying CO in the tail gas of the ship2. The device has high carbon capture efficiency and recycled CO2High purity, low energy consumption, easy modification and the like, and the device isThe method has great significance in the aspects of energy conservation and emission reduction of the shipping industry.
Drawings
Fig. 1 is a schematic diagram of a system connection structure according to a first embodiment of the present invention;
fig. 2 is a schematic diagram of a system connection structure according to a second embodiment of the present invention.
Detailed Description
The present invention will be further illustrated with reference to the following figures and specific examples, which are to be understood as merely illustrative and not restrictive of the scope of the invention.
The first embodiment is as follows:
a ship tail gas treatment system is shown in figure 1 and comprises a tail gas pretreatment system, a low-temperature desublimation carbon capture system, a melting pressurization system, a rectification purification system, a main cooling system and an isopentane circulating heat exchange system.
The tail gas pretreatment system comprises a first pneumatic regulating valve 1, a flue gas blower 2, a precooler 3 and a dryer 4, the low-temperature desublimation carbon capture system comprises a flue gas heat exchanger 5 and a desublimation heat exchanger 6, the melting pressurization system comprises a slurry pump 7, a solid-liquid separator 8, a screw booster 9, a high-speed centrifugal pump 10, a condenser 11, an electric heater 12, a first three-way regulating valve 25 and a second three-way regulating valve 27, the rectification purification system comprises a preheater 13, a rectifying tower 14, a CO purifying system2Liquid pump 20, gas-liquid separator 21, liquid CO2The system comprises a Dewar flask 22, a second pneumatic regulating valve 28, a first seawater condenser 29, a separation tank 30 and a tower kettle reboiler 31, wherein the main cooling system comprises a main cooler 16 and an external cold source system, the external cold source system comprises an LNG (liquefied natural gas) storage tank 32, a check valve 33, an LNG (liquefied natural gas) delivery pump 34, a first one-way stop valve 35, a second one-way stop valve 36, a spray nozzle 37, a control valve 38, a seawater rewarming device 39, a marine engine main machine 40, an air pump 41 and an air flow regulating valve 42, and the isopentane circulating heat exchange system comprises a cooler 19.
An external flue gas inlet X is connected with an inlet of a first pneumatic regulating valve 1, an outlet of the first pneumatic regulating valve 1 is connected with an inlet of a flue gas blower 2, an outlet of the flue gas blower 2 is connected with a hot end inlet M-1 of a precooler 3, and a hot end outlet M-2 of the precooler 3 is connected with an inlet of a dryer 4; the cold end inlet M-3 of the precooler 3 is connected with the external refrigerant outlet, and the cold end outlet M-4 of the precooler 3 is connected with the external refrigerant inlet. An inlet A-3 at the upper end of the flue gas heat exchanger 5 is connected with an outlet of the dryer 4, and an outlet A-4 at the lower end of the flue gas heat exchanger 5 is connected with a gas phase inlet B-1 at the lower end of the desublimation heat exchanger 6; the gas phase outlet B-2 at the upper end of the desublimation heat exchanger 6 is connected with the inlet A-1 at the right side of the flue gas heat exchanger 5, and the outlet A-2 at the left side of the flue gas heat exchanger 5 is connected with the clean air outlet Y.
A slurry outlet B-4 at the lower end of the desublimation heat exchanger 6 is connected with an inlet of a slurry pump 7, an outlet of the slurry pump 7 is connected with a slurry inlet C-1 of a solid-liquid separator 8, a second outlet C-3 of the solid-liquid separator 8 is connected with a first inlet F-1 of a screw booster 9, an outlet F-3 of the screw booster 9 is connected with an inlet of a high-speed centrifugal pump 10, an outlet of the high-speed centrifugal pump 10 is connected with an inlet G-1 at the cold end of a condenser 11, and an outlet G-2 at the cold end of the condenser 11 is connected with an inlet of an electric heater 12; the outlet of the electric heater 12 is connected with the inlet of a second three-way regulating valve 27, the first outlet N-2 of the second three-way regulating valve 27 is connected with the second inlet F-2 of the screw supercharger 9, and the second outlet N-3 of the second three-way regulating valve 27 is connected with the rectification and purification system; a first outlet C-2 of the solid-liquid separator 8 is connected with an inlet D-1 of a first three-way regulating valve 25, a first outlet D-2 of the first three-way regulating valve 25 is connected with a hot end inlet E-1 of the main cooler 16, and a hot end outlet E-2 of the main cooler 16 is connected with a right inlet B-3 at the upper end of the desublimation heat exchanger 6; and a second outlet D-3 of the first three-way regulating valve 25 is connected with an isopentane circulating heat exchange system, and the isopentane circulating heat exchange system is connected with a right middle inlet B-5 of the desublimation heat exchanger 6.
A second outlet N-3 of a second three-way regulating valve 27 in the melting pressurization system is connected with a cold end inlet H-1 of the preheater 13; a cold end outlet H-2 of the preheater 13 is connected with a middle feed inlet I-1 at the right side of the rectifying tower 14, an upper end outlet I-2 of the rectifying tower 14 is connected with an inlet of a first seawater condenser 29, an outlet of the first seawater condenser 29 is connected with an upper end inlet P-1 of a separation tank 30, a first outlet P-2 of the separation tank 30 is connected with an upper end inlet I-3 at the left side of the rectifying tower 14, a second outlet P-3 of the separation tank 30 is connected with a hot end inlet G-3 of the condenser 11, a hot end outlet G-4 of the condenser 11 is connected with a hot end inlet J-3 of the cooler 19, and a hot end outlet J-4 of the cooler 19 is connected with CO2Inlet phase of liquid pump 20To CO2The liquid pump 20 is connected with an inlet L-1 at the bottom of the gas-liquid separator 21, an outlet L-2 at the top of the gas-liquid separator 21 is connected with a feed inlet I-4 at the middle part of the rectifying tower 14, and an outlet L-3 at the right side of the gas-liquid separator 21 is sequentially connected with a second pneumatic regulating valve 28 and liquid CO2A dewar 22; an outlet I-5 at the lower end of the left side of the rectifying tower 14 is connected with an inlet Q-1 at the left side of a tower kettle reboiler 31, an outlet Q-2 at the upper end of the tower kettle reboiler 31 is connected with a feed inlet I-6 at the bottom of the rectifying tower 14, an outlet Q-3 at the bottom of the tower kettle reboiler 31 is connected with an inlet H-3 at the hot end of the preheater 13, and an outlet H-4 at the hot end of the preheater 13 is connected with an isopentane circulating heat exchange system.
A second outlet D-3 of a first three-way regulating valve 25 in the melting pressurization system is connected with an inlet J-1 at the right side of the cooler 19; and a pipeline at the J-2 position of the left outlet of the cooler 19 and a pipeline at the H-4 position of the hot end outlet of the preheater 13 are converged and then are connected to the right inlet B-5 of the desublimation heat exchanger 6.
The LNG storage tank 32 stores LNG fuel, a spray nozzle 37 is installed on the LNG storage tank 32, a check valve 33, an LNG transfer pump 34, a first one-way stop valve 35, a second one-way stop valve 36 and the spray nozzle 37 are sequentially connected to form a loop, a control valve 38 is arranged between the first one-way stop valve 35 and the second one-way stop valve 36, the control valve 38 is connected with an inlet E-3 at the cold end of the main cooler 16, a marine engine main machine 40 is connected with an outlet E-4 at the cold end of the main cooler 16 through a seawater rewarming device 39, an air pump 41 is connected with the marine engine main machine 40 through an air flow regulating valve 42, and flue gas combusted by the marine engine main machine 40 enters the tail gas pretreatment system from an external flue gas transfer pipeline.
The LNG fuel flows out from the LNG storage tank 32, enters the LNG transfer pump 34 after passing through the check valve 33, is pumped out by the LNG transfer pump 34 and flows through the first one-way stop valve 35, a part of LNG flowing out from the first one-way stop valve flows through the second one-way stop valve 36 and enters the spray nozzle 37 in the LNG storage tank 32, wherein the pressure in the LNG storage tank 32 is pressurized by a part of LNG and then is sprayed into the tank by the spray nozzle 37 to realize regulation, the other part of LNG flows out from the first one-way stop valve and then enters the main cooler 16 through the control valve 38 to exchange heat with isopentane, the natural gas after releasing cold energy enters the seawater rewarming device 39 to be rewarming and then is combusted with air entering from the air pump 41 by the marine engine main engine 40, and the combusted flue gas enters the system from the flue gas inlet X to form circulation.
A pressure sensor 24 is arranged on a pipeline connecting the flue gas heat exchanger 5 and the desublimation heat exchanger 6, and a control signal of the pressure sensor 24 is connected with the first pneumatic regulating valve 1 through a lead. The right end of the flue gas inlet X is provided with a first flowmeter 23, and a second flowmeter 26 is arranged on a connecting pipeline of the gas-liquid separator 21 and a second pneumatic regulating valve 28. And a carbon dioxide gas detector is arranged on a pipeline connecting the cold end outlet A-2 of the flue gas heat exchanger 5 with the external clean air outlet Y.
The precooler 3 is preferably a shell and tube or coil heat exchanger, the flue gas in the duct is cooled by water cooling, and the dryer 4 is preferably a dryer containing a molecular sieve desiccant. The desublimation heat exchanger 6 is preferably a spray type direct contact heat exchanger, and the refrigerant for heat and mass exchange with the flue gas in the heat exchanger is liquid isopentane. The desublimation heat exchanger 6 can adopt active modes such as vibration knocking and centrifugal removal or passive modes such as parallel connection of a plurality of heat exchangers and gas purging at rewarming to realize the removal of the snowflake-shaped dry ice from the tube wall. The slurry pump 7 is preferably a magnetically coupled external gear pump with the addition of sight glasses and instrumentation ports in the electric heater 12 to provide more signals about liquid level and gas space in the electric heater 12. And heat insulation layers are arranged on connecting pipelines and equipment of the low-temperature desublimated carbon capturing system, the melting pressurization system, the rectification purification system, the isopentane circulating heat exchange system and the cold source main cooling system.
Example two:
the embodiment is basically the same as the first embodiment, and the differences are that: as shown in fig. 2, the main cooling system includes a main cooler 16 and an external cold source system ii, the external cold source system ii includes a nitrogen expander 43, a nitrogen circulating heat exchanger 44, a nitrogen compressor 45, and a second seawater condenser 46, an outlet of the nitrogen expander 43 is connected to an inlet E-5 of the main cooler 16, an inlet I-1 of the nitrogen circulating heat exchanger 44 is connected to an outlet E-6 of the main cooler 16, an outlet I-2 of the nitrogen circulating heat exchanger 44 is connected to an inlet of the nitrogen compressor 45, an outlet of the nitrogen compressor 45 is connected to an inlet I-3 of the nitrogen circulating heat exchanger 44 through the second seawater condenser 46, an outlet I-4 of the circulating heat exchanger 44 is connected to a cold inlet E-3 of the main cooler 16, and an outlet E-4 of the cold end of the main cooler 16 is connected to an inlet of the nitrogen expander 43.
After being expanded and cooled by the nitrogen expander 43, the high-pressure nitrogen enters the main cooler 16 from a third inlet E-5 of the main cooler 16 as a cold source to exchange heat with isopentane, the nitrogen after releasing cold energy flows out from a third outlet E-6 of the main cooler 16, and flows in from a first inlet I-1 of the nitrogen circulating heat exchanger 44, flows out from a first outlet I-2 of the nitrogen circulating heat exchanger 44 after heat exchange, enters a nitrogen compressor 45 for pressurization, the pressurized nitrogen enters a second seawater condenser 46 for heat exchange with seawater, enters the nitrogen circulating heat exchanger 44 from a second inlet I-3 of the nitrogen circulating heat exchanger 44, enters the main cooler 16 from a second inlet E-3 of the main cooler 16 after exchanging heat with nitrogen flowing in from a first inlet I-1 of a nitrogen circulating heat exchanger 44 to absorb cold energy, the nitrogen which flows in the main cooler 16 and the third inlet E-5 exchanges heat to continuously absorb cold energy and then enters the nitrogen expansion machine 43 to form circulation.
The main cooling system can utilize the self-cooling energy of the low-temperature fluid and an active refrigeration mode to supply cold, for example, the self-cooling energy of the low-temperature fluid such as liquefied natural gas and liquid nitrogen, or the active refrigeration modes such as nitrogen expansion cycle refrigeration and Stirling refrigeration are utilized to realize cold supply.
The tail gas treatment method of the ship tail gas treatment system comprises the following steps:
step (a): high-temperature flue gas enters the system from an inlet, the total flue gas flow entering the system is measured by a first flow meter 23, the flow is regulated by a first pneumatic regulating valve 1, the pressure of the flue gas entering from a flue gas inlet is increased after the flue gas passes through a flue gas blower 2, the flue gas is precooled in a precooler 3, the precooled flue gas is dried by a dryer 4 and then enters a flue gas heat exchanger 5 from a hot end inlet A-3 of the flue gas heat exchanger 5, and the flue gas enters a desublimation heat exchanger 6 from a lower left side inlet B-1 of the desublimation heat exchanger 6 after cold energy is absorbed in the flue gas heat exchanger 5.
Step (b): the low-temperature liquid isopentane absorbing cold energy of the cold source flows out of a hot end outlet E-2 of the main cooler 16 and enters the desublimation heat exchanger 6 from a right inlet B-3 at the upper end of the desublimation heat exchanger 6, the isopentane exchanges heat with carbon dioxide in flue gas in the desublimation heat exchanger 6, and the carbon dioxide gas after absorbing the cold energy is desublimated into carbon dioxide solid;
step (c): clean air after heat exchange flows out from an outlet B-2 at the left side of the upper end of the desublimation heat exchanger 6, the clean air flowing out enters the smoke heat exchanger 5 from an inlet A-1 at the cold end of the smoke heat exchanger 5, the clean air exchanges heat with smoke entering from an inlet A-3 at the hot end of the smoke heat exchanger 5, the clean air after cold energy release passes through a carbon dioxide gas detector arranged on an outlet A-2 at the cold end of the smoke heat exchanger 5, and the carbon dioxide gas detector detects that the decarburized tail gas reaches the standard and then is discharged out of the system.
A step (d): the mixed slurry of carbon dioxide solids and isopentane liquid flowing out from the right outlet B-4 at the lower end of the self-sublimation heat exchanger 6 enters the solid-liquid separator 8 after passing through the slurry pump 7, part of the isopentane liquid flows out from the first outlet C-2 of the solid-liquid separator 8, enters the first three-way regulating valve 25, flows out from the first outlet D-2 of the first three-way regulating valve 25, enters the hot end inlet E-1 of the main cooler 16, exchanges heat with the main cooling system in the main cooler 16 to absorb cold energy and then returns to the sublimation heat exchanger 6, and part of the isopentane flows out from the second outlet D-3 of the first three-way regulating valve 25, enters the cooler 19, releases the cold energy in the cooler 19 and then returns to the right inlet B-5 of the sublimation heat exchanger 6.
A step (e): the mixed slurry of carbon dioxide solid and isopentane liquid flowing out from the second outlet C-3 of the solid-liquid separator 8 enters a screw supercharger 9, most of the carbon dioxide solid in the mixed slurry is gradually supercharged by the screw supercharger 9 to become carbon dioxide liquid, the mixture of isopentane, carbon dioxide liquid and the rest of a small amount of carbon dioxide solid enters an electric heater 12 after passing through a mixing chamber of the screw supercharger 9, a high-speed centrifugal pump 10 and a condenser 11, part of the mixed solution of carbon dioxide and isopentane heated by the electric heater 12 flows out through a first outlet N-2 of the second three-way regulating valve 27 to enter the mixing chamber of the screw supercharger 9, wherein the mixed solution of liquid carbon dioxide and isopentane is heated to melt the rest of carbon dioxide solid, and the carbon dioxide solid of the rest of fine particles is separated by the high-speed centrifugal pump 10 and discharged from a lower outlet if the carbon dioxide solid of the rest of fine particles is not completely melted, the mixed solution of carbon dioxide and isopentane flows out through the high-speed centrifugal pump 10 and then enters the condenser 11, the cold energy is released in the condenser 11 and then flows out through a cold end outlet G-2 of the condenser 11, and the mixed solution of carbon dioxide and isopentane flowing out through the cold end outlet G-2 of the condenser 11 enters the second three-way regulating valve 27 through the electric heater 12.
Step (f): part of the mixed solution of the carbon dioxide and the isopentane enters the preheater 13 through a second three-way regulating valve 27, the mixed solution of the carbon dioxide and the isopentane absorbs heat in the preheater 13 and flows out from a cold end outlet H-2 and then enters the rectifying tower 14, a tower kettle reboiler 31 heats the mixed solution of the carbon dioxide and the isopentane, the carbon dioxide liquid absorbs heat and then is vaporized, vapor-phase carbon dioxide moves from the tower bottom to the tower top, carbon dioxide gas flows out from a top outlet I-2 of the rectifying tower 14 and then enters a first seawater condenser 29, the carbon dioxide gas is partially liquefied and flows out from the first seawater condenser 29 and then enters a separation tank 30, the liquefied carbon dioxide gas flows out from a first outlet P-2 at the right end of the separation tank 30 and flows back into the rectifying tower 14 and flows from the tower top to the tower bottom, and non-liquefied pure carbon dioxide gas enters the condenser 11 from a second outlet P-3 at the lower end of the separation tank 30, the ascending vapor phase and the descending liquid phase in the rectifying tower 14 generate heat and mass transfer, the gas with higher temperature is partially liquefied, the liquid with lower temperature is partially vaporized, a small amount of isopentane component in the vapor phase enters the liquid phase and returns to the bottom of the tower, the carbon dioxide component in the liquid phase enters the vapor phase and reaches the top of the tower, in the process, the concentration of carbon dioxide at the top of the tower is higher and higher, isopentane liquid flowing out from an outlet I-5 at the left side of the lower end of the rectifying tower 14 enters the tower bottom reboiler 31, part of isopentane with a small amount of carbon dioxide liquid flows back to the rectifying tower 14 from a first outlet Q-2 of the tower bottom reboiler 31 for rectification again, the rest pure isopentane liquid flows out from a first outlet Q-3 of the tower bottom reboiler and enters the preheater 13, after absorbing part of cold energy in the preheater 13, the cold energy flows out from a hot end outlet H-4 of the preheater 13 and enters the desublimation heat exchanger 6.
Step (g): the pure carbon dioxide gas absorbs cold in the condenser 11 and then enters the cooler 19 again to absorb cold, part of the carbon dioxide gas is liquefied, and the mixture of carbon dioxide liquid and carbon dioxide gas passes through the cooler 19 and then enters the cooler 19Into CO2Pumping 20 liquid through CO2The liquid pump 20 is pressurized and then enters the gas-liquid separator 21, and the carbon dioxide liquid flows out from the second outlet L-3 of the gas-liquid separator 21, passes through the second flowmeter 26 and the second pneumatic regulating valve 28 and is collected in the liquid CO2The carbon dioxide gas which is not liquefied in the dewar 22 is discharged from the first outlet L-2 of the gas-liquid separator 21 and enters the rectifying tower 14 for further purification.
Claims (10)
1. A ship tail gas treatment system is characterized in that: including tail gas pretreatment systems, low temperature carbon gathering system that sublimes, the melting pressure charge system, rectification purification system, main cooling system, isopentane circulation heat transfer system, external flue gas passes through pipeline and tail gas pretreatment systems connection, tail gas pretreatment systems, the melting pressure charge system respectively with low temperature carbon gathering system connection that sublimes, rectification purification system, isopentane circulation heat transfer system respectively with melting pressure charge system connection, rectification purification system and isopentane circulation heat transfer system connection, low temperature carbon gathering system that sublimes, the melting pressure charge system respectively with main cooling system connection, external clean air passes through pipeline and low temperature carbon gathering system connection that sublimes.
2. The marine exhaust gas treatment system according to claim 1, wherein: the tail gas pretreatment system comprises a first pneumatic regulating valve (1), a flue gas blower (2), a precooler (3) and a dryer (4), wherein an external flue gas conveying pipeline is connected with an inlet of the first pneumatic regulating valve (1), a first flow meter (23) is arranged at the joint of the first pneumatic regulating valve and the first pneumatic regulating valve, an outlet of the first pneumatic regulating valve (1) is connected with an inlet of the flue gas blower (2), an outlet of the flue gas blower (2) is connected with a hot end inlet M-1 of the precooler (3), a hot end outlet M-2 of the precooler (3) is connected with an inlet of the dryer (4), a cold end inlet M-3 of the precooler (3) is connected with an outlet of an external refrigerant conveying pipeline, and a cold end outlet M-4 of the precooler (3) is connected with an inlet of the external refrigerant conveying pipeline.
3. The marine exhaust gas treatment system according to claim 1, wherein: the low-temperature desublimated carbon capture system comprises a flue gas heat exchanger (5), the system comprises a desublimation heat exchanger (6), an inlet A-3 of a flue gas heat exchanger (5) is connected with a tail gas pretreatment system, an outlet A-4 of the flue gas heat exchanger (5) is connected with a gas phase inlet B-1 of the desublimation heat exchanger (6), a gas phase outlet B-2 of the desublimation heat exchanger (6) is connected with an inlet A-1 of the flue gas heat exchanger (5), an outlet A-2 of the flue gas heat exchanger (5) is communicated with an outlet of an external clean air conveying pipeline, a carbon dioxide gas detector is arranged between the outlet A-1 and the outlet B-2, a slurry outlet B-4 of the desublimation heat exchanger (6) is connected with a melting pressurization system, an inlet B-3 of the desublimation heat exchanger (6) is connected with a main cooling system, and an inlet B-5 of the desublimation heat exchanger (6) is connected with an isopentane circulating heat exchange system.
4. The marine exhaust gas treatment system according to claim 1, wherein: the melting pressurization system comprises a slurry pump (7), a solid-liquid separator (8), a screw booster (9), a high-speed centrifugal pump (10), a condenser (11), an electric heater (12), a first three-way regulating valve (25) and a second three-way regulating valve (27), wherein the inlet of the slurry pump (7) is connected with the low-temperature desublimated carbon capture system, the outlet of the slurry pump (7) is connected with the slurry inlet C-1 of the solid-liquid separator (8), the second outlet C-3 of the solid-liquid separator (8) is connected with the first inlet F-1 of the screw booster (9), the outlet F-3 of the screw booster (9) is connected with the inlet of the high-speed centrifugal pump (10), the outlet of the high-speed centrifugal pump (10) is connected with the cold-end inlet G-1 of the condenser (11), and the cold-end outlet G-2 of the condenser (11) is connected with the inlet of the electric heater (12), an outlet of the electric heater (12) is connected with an inlet of a second three-way regulating valve (27), a first outlet N-2 of the second three-way regulating valve (27) is connected with a second inlet F-2 of the screw supercharger (9), a second outlet N-3 of the second three-way regulating valve (27) is connected with the rectification and purification system, a first outlet C-2 of the solid-liquid separator (8) is connected with an inlet D-1 of a first three-way regulating valve (25), a first outlet D-2 of the first three-way regulating valve (25) is connected with the main cooling system, and a second outlet D-3 of the first three-way regulating valve (25) is connected with the isopentane circulating heat exchange system.
5. The marine exhaust gas treatment system according to claim 1, wherein: the rectification and purification system comprises a preheater (13), a rectifying tower (14) and CO2Liquid pump (20) A gas-liquid separator (21), liquid CO2A Dewar flask (22), a second pneumatic regulating valve (28), a first seawater condenser (29), a separating tank (30) and a tower kettle reboiler (31), wherein a second outlet N-3 of a second three-way regulating valve (27) is connected with a cold end inlet H-1 of a preheater (13), a cold end outlet H-2 of the preheater (13) is connected with a feed inlet I-1 of a rectifying tower (14), an outlet I-2 of the rectifying tower (14) is connected with an inlet of the first seawater condenser (29), an outlet of the first seawater condenser (29) is connected with an inlet P-1 of the separating tank (30), a first outlet P-2 of the separating tank (30) is connected with an inlet I-3 of the rectifying tower (14), a second outlet P-3 of the separating tank (30) is connected with a melting pressurization system, and CO is introduced into the molten metal in the Condenser (CO) and the rectifying tower (14)2The inlet of the liquid pump (20) is connected with an isopentane circulating heat exchange system, and CO is introduced2The liquid pump (20) is connected with an inlet L-1 of the gas-liquid separator (21), an outlet L-2 of the gas-liquid separator (21) is connected with a feed inlet I-4 of the rectifying tower (14), and an outlet L-3 of the gas-liquid separator (21) is connected with liquid CO through a second pneumatic regulating valve (28)2A Dewar flask (22) is connected, a second flowmeter (26) is arranged between the gas-liquid separator (21) and the second pneumatic regulating valve (28), an outlet I-5 of the rectifying tower (14) is connected with an inlet Q-1 of a tower kettle reboiler (31), an outlet Q-2 of the tower kettle reboiler (31) is connected with a feed inlet I-6 of the rectifying tower (14), an outlet Q-3 of the tower kettle reboiler (31) is connected with a hot end inlet H-3 of the preheater (13), and a hot end outlet H-4 of the preheater (13) is connected with an isopentane circulating heat exchange system.
6. The marine exhaust gas treatment system according to claim 1, wherein: the main cooling system comprises a main cooler (16), an external cold source system or an external cold source system II, a cold end inlet E-3 of the main cooler (16) is connected with the external cold source system or an outlet of the external cold source system II, a cold end outlet E-4 of the main cooler (16) is connected with the external cold source system or an inlet of the external cold source system II, an inlet E-1 of the main cooler (16) is connected with the melting pressurization system, and an outlet E-2 of the main cooler (16) is connected with the low-temperature desublimated carbon capturing system.
7. The marine exhaust gas treatment system according to claim 6, wherein: the external cold source system comprises an LNG storage tank (32), a check valve (33), an LNG transfer pump (34), a first one-way stop valve (35), a second one-way stop valve (36), a spray nozzle (37), a control valve (38), a seawater rewarming device (39), a marine engine main unit (40), an air pump (41) and an air flow regulating valve (42), the LNG storage tank (32) stores LNG fuel, the LNG storage tank (32) is provided with the spray nozzle (37), the LNG storage tank (32), the check valve (33), the LNG transfer pump (34), the first one-way stop valve (35), the second one-way stop valve (36) and the spray nozzle (37) are sequentially connected to form a loop, a control valve (38) is arranged between the first one-way stop valve (35) and the second one-way stop valve (36), the control valve (38) is connected with a cold end inlet E-3 of a main cooler (16), and the marine engine main unit (40) is connected with a cold end outlet E-4 of the main cooler (16) through the seawater rewarming device (39) And the air pump (41) is connected with the marine engine main machine (40) through the air flow regulating valve (42), and the flue gas combusted by the marine engine main machine (40) enters the tail gas pretreatment system from an external flue gas conveying pipeline.
8. The marine exhaust gas treatment system according to claim 6, wherein: and the external cold source system II comprises a nitrogen expander (43), a nitrogen circulating heat exchanger (44), a nitrogen compressor (45) and a second seawater condenser (46), wherein the outlet of the nitrogen expander (43) is connected with the inlet E-5 of the main cooler (16), the inlet I-1 of the nitrogen circulating heat exchanger (44) is connected with the outlet E-6 of the main cooler (16), the outlet I-2 of the nitrogen circulating heat exchanger (44) is connected with the inlet of the nitrogen compressor (45), the outlet of the nitrogen compressor (45) is connected with the inlet I-3 of the nitrogen circulating heat exchanger (44) through the second seawater condenser (46), the outlet I-4 of the circulating heat exchanger (44) is connected with the cold-end inlet E-3 of the main cooler (16), and the cold-end outlet E-4 of the main cooler (16) is connected with the inlet of the nitrogen expander (43).
9. The marine exhaust gas treatment system according to claim 1, wherein: the isopentane circulating heat exchange system comprises a cooler (19), an inlet J-1 and a hot end inlet J-3 of the cooler (19) are respectively connected with a melting pressurization system, a hot end outlet J-4 of the cooler (19) is connected with a rectification purification system, and a low-temperature desublimation carbon capture system is connected with an outlet J-2 of the cooler (19).
10. An exhaust gas treatment method of a ship exhaust gas treatment system according to any one of claims 1 to 9, comprising the steps of:
step (a): the method comprises the following steps that external high-temperature flue gas enters a tail gas pretreatment system through a conveying pipeline, dynamic pressure of the flue gas is increased and precooled, the precooled flue gas is further dried in the tail gas pretreatment system and then enters a low-temperature desublimated carbon capture system, and cold energy is absorbed in the low-temperature desublimated carbon capture system;
step (b): the main cooling system sends the low-temperature liquid isopentane absorbing the cold energy of the cold source into a low-temperature desublimated carbon capture system, the isopentane exchanges heat with carbon dioxide in the flue gas in the low-temperature desublimated carbon capture system, and the carbon dioxide gas absorbing the cold energy is desublimated into carbon dioxide solid;
step (c): the decarbonized clean air flows out of the low-temperature desublimation carbon capture system after being reheated by the low-temperature desublimation carbon capture system, and is discharged out of the system after being reheated by a flue gas heat exchanger and the decarbonized tail gas is detected to reach the standard;
step (d): the mixed slurry of carbon dioxide solid and isopentane liquid in the low-temperature carbon sublimation capturing system flows into a melting pressurization system, part of the isopentane liquid enters a main cooling system through solid-liquid separation, returns to the low-temperature carbon sublimation capturing system after cold energy is absorbed through heat exchange, and part of the isopentane liquid enters an isopentane circulating heat exchange system and returns to the low-temperature carbon sublimation capturing system after the cold energy is released in the isopentane circulating heat exchange system;
a step (e): the carbon dioxide solid in the mixed slurry is gradually pressurized in the melting pressurization system and then is changed into carbon dioxide liquid, at the moment, a mixture of the residual isopentane liquid, the carbon dioxide liquid and the residual carbon dioxide solid exists in the melting pressurization system, wherein part of the mixed liquid is heated, refluxed and converged in the melting pressurization system to melt the residual carbon dioxide solid, the carbon dioxide solid of the residual undissolved fine particles is discharged from the melting pressurization system, and part of the mixed liquid is heated, heated and then enters a rectification and purification system;
step (f): part of the mixed solution of the carbon dioxide and the isopentane is subjected to rectification reaction in a rectification purification system, the carbon dioxide liquid absorbs heat and then is vaporized, the purified carbon dioxide gas is liquefied again in the rectification purification system, the pure carbon dioxide gas which is not liquefied returns to a melting pressurization system, the ascending vapor phase and the descending liquid phase in the rectification purification system generate heat and mass transfer, the gas with higher temperature is partially liquefied, the liquid with lower temperature is partially vaporized, a small amount of isopentane component in the vapor phase enters the bottom of the rectification purification system, the carbon dioxide component in the liquid phase enters the vapor phase and reaches the top of the rectification purification system, in the process, the concentration of carbon dioxide at the top part is higher and higher, part of isopentane liquid with a small amount of carbon dioxide liquid in the rectification and purification system is rectified again, and the rest pure isopentane liquid flows out to enter a low-temperature desublimated carbon capture system after absorbing part of cold energy in the rectification and purification system;
step (g): the pure carbon dioxide gas absorbs cold energy in the melting pressurization system and then enters the isopentane circulating heat exchange system again to absorb the cold energy, part of the carbon dioxide gas is liquefied, after the carbon dioxide gas is pressurized by the rectification purification system, formed carbon dioxide liquid is collected in the rectification purification system, and the carbon dioxide gas which is not liquefied is purified again in the rectification purification system continuously.
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