CN113893655A - Low-temperature drying system for carbon capture - Google Patents
Low-temperature drying system for carbon capture Download PDFInfo
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- CN113893655A CN113893655A CN202111319284.7A CN202111319284A CN113893655A CN 113893655 A CN113893655 A CN 113893655A CN 202111319284 A CN202111319284 A CN 202111319284A CN 113893655 A CN113893655 A CN 113893655A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- 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
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
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- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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Abstract
The invention discloses a low-temperature drying system for carbon capture, which comprises a flue gas treatment system, a brine circulating system, a refrigerant circulating system, a cooling water system and a steam system, and mainly comprises a drying tower, a concentration tower, a gas-liquid separation tank, a generator and a plurality of heat exchangers. The invention takes the water vapor partial pressure difference between the wet flue gas and the saline solution as the driving force, and realizes the moisture transfer by directly contacting and exchanging heat between the saline and the wet flue gas, thereby achieving the effect of drying the flue gas. The invention can effectively improve the blockage phenomenon of pipelines or separation equipment caused by moisture contained in the flue gas in the carbon capture liquefaction process stage. The invention can also adopt a single-stage drying mode and a two-stage drying mode to better adapt to the fluctuation of the smoke quantity caused by the peak value and the valley value of the electricity consumption. And a refrigerant circulating system is adopted to recover heat, so that the energy consumption of the system is reduced.
Description
Technical Field
The invention relates to a carbon capture system, in particular to a low-temperature drying system for carbon capture.
Background
Low temperature carbon capture is a promising, transformed post-combustion carbon capture technology. The low temperature carbon capture process can reduce 95% of carbon dioxide emissions.
The dehydration mode common in the low-temperature carbon capture process is low-temperature condensation dehydration, and the dehydration of the flue gas is realized by utilizing the principle that the water content in the flue gas is reduced along with the reduction of the temperature when the pressure is unchanged, but the dehydration method is only suitable for the rough separation of a large amount of water. In the actual carbon capture liquefaction process, the flue gas dried by the low-temperature condensation method still contains partial moisture, and the moisture in the flue gas is condensed on the surfaces of equipment such as pipelines, heat exchangers or throttle valves in the form of frost when the moisture is lower than zero, so that the blockage of pipelines and separation equipment can be caused. When carbon dioxide is conveyed, the existence of liquid water can also accelerate the corrosion to the pipe wall and the valve member, and reduce the service life of the pipeline. In order to avoid the blockage phenomenon caused by the existence of water in the liquid carbon dioxide, the flue gas needs to be further dried.
The low-temperature carbon capture technology is generally used for emission reduction of a power plant, the power supply of the power plant often has day and night peak-to-valley electricity difference, and the emission of carbon dioxide fluctuates along with fluctuation of the use amount of day and night users. How to ensure that the drying effect of the carbon capture drying system can adapt to the fluctuation of different flue gas quantities still needs to be solved.
The low-temperature brine direct contact drying is mainly used for improving the dryness of gas, the partial pressure difference of water vapor between wet flue gas and brine solution is used as a driving force, the migration of moisture is realized by making brine and wet flue gas directly contact for heat exchange, and the effect of drying flue gas is achieved. The brine is low in concentration after absorbing water, and can be recycled by being connected to a regeneration system for evaporation and concentration. The temperature of the concentrated brine after evaporation and concentration is about 110 ℃, the temperature of the concentrated brine is reduced to below minus 20 ℃ before the concentrated brine enters a dryer to dry gas, and the temperature difference between the concentrated brine and the gas reaches 130 ℃. The part of heat is generally cooled by a cooling medium, and the treatment mode of direct cooling not only causes waste of high-quality energy, but also increases the demand of the cooling medium. How to fully recycle the part of heat to reduce the energy consumption of the system is a problem which needs to be solved urgently at present.
Disclosure of Invention
The present invention has been made to solve the above-mentioned problems and disadvantages of the prior art, and an object of the present invention is to provide a low-temperature drying system for carbon capture.
The method can effectively improve the blockage phenomenon of pipelines or separation equipment caused by moisture contained in the flue gas in the carbon capture liquefaction process stage, is suitable for drying different flue gas quantities, and reasonably recycles the heat of the circulating brine.
In order to achieve the above purpose, the present invention is realized by the following technical scheme.
A low-temperature drying system for carbon capture, which comprises a flue gas treatment system, a brine circulating system, a refrigerant circulating system, a cooling water system and a steam system,
the flue gas treatment system comprises a first heat exchanger 19, a second drying tower 2, a second gas-liquid separation tank 6, a second heat exchanger 29, a first gas-liquid separation tank 5, a first drying tower 1,
the external wet flue gas is connected with the right end inlet of the first heat exchanger 19, the left end outlet of the first heat exchanger 19 is connected with the gas phase inlet of the second drying tower 2, the gas phase outlet of the second drying tower 2 is connected with the lower end inlet of the first heat exchanger 19, the upper end outlet of the first heat exchanger 19 is connected in parallel with two pipelines, respectively, the first pipeline is converged with the upper end outlet pipeline of the second heat exchanger 29, the second pipeline is connected with the inlet of the second gas-liquid separation tank 6, the gas phase outlet of the second gas-liquid separation tank 6 is connected with the right end inlet of the second heat exchanger 29, the liquid phase outlet of the second gas-liquid separation tank 6 is connected with an external condensed water collection system, the left end outlet of the second heat exchanger 29 is connected with the first gas-liquid separation tank 5, the liquid phase outlet of the first gas-liquid separation tank 5 is connected with an external condensed water collection system, and the gas phase outlet of the first gas-liquid separation tank 5 is connected with the gas phase inlet of the first drying tower 1, the gas phase outlet of the first drying tower 1 is connected with the inlet at the lower end of the second heat exchanger 29, the outlet at the upper end of the second heat exchanger 29 is connected with the first pipeline of the outlet at the upper end of the first heat exchanger 19 after being converged and then is connected to an external dry flue gas collecting system,
the brine circulating system comprises a brine tank 9, a first brine pump 12, a seventh heat exchanger 40, a third heat exchanger 35, a ninth heat exchanger 49, a first drying tower 1, a second brine pump 13, a fourth heat exchanger 36, a second drying tower 2, a fifth heat exchanger 38, a third brine pump 14, a first concentration tower 3, an eighth heat exchanger 41, a third gas-liquid separation tank 7, a fourth brine pump 15, a tenth heat exchanger 43, a second concentration tower 4, a fourth gas-liquid separation tank 8,
the outlet of the brine tank 9 is connected to the inlet of the first brine pump 12, the outlet of the first brine pump 12 is connected in parallel to two pipelines, respectively, the first pipeline is converged with the pipeline at the outlet of the right end of the third heat exchanger 35 and then connected to the inlet of the lower end of the fourth heat exchanger 36, the second pipeline is connected to the inlet of the right end of the seventh heat exchanger 40, the outlet of the left end of the seventh heat exchanger 40 is connected to the inlet of the lower end of the third heat exchanger 35, the outlet of the upper end of the third heat exchanger 35 is connected to the inlet of the lower end of the ninth heat exchanger 49, the outlet of the upper end of the ninth heat exchanger 49 is connected to the inlet of the liquid phase of the first drying tower 1, the outlet of the liquid phase of the first drying tower 1 is connected to the inlet of the second brine pump 13, the outlet of the second brine pump 13 is connected to the inlet of the left end of the third heat exchanger 35, the outlet of the right end of the third heat exchanger 35 is converged with the pipeline connected in parallel to the outlet of the first brine pump 12 and then connected to the inlet of the lower end of the fourth heat exchanger 36 A liquid phase outlet of the fourth heat exchanger 36 is connected with a liquid phase inlet of the second drying tower 2, a liquid phase outlet of the second drying tower 2 is connected with a left end inlet of the fifth heat exchanger 38, a right end outlet of the fifth heat exchanger 38 is connected with an inlet of the third brine pump 14, an outlet of the third brine pump 14 is connected with a left end inlet of the eighth heat exchanger 41, a right end outlet of the eighth heat exchanger 41 is connected with an inlet of the first concentrating tower 3, a gas phase outlet of the first concentrating tower 3 is connected with a lower end inlet of the eighth heat exchanger 41, an upper end outlet of the eighth heat exchanger 41 is connected with an inlet of the third gas-liquid separating tank 7, a gas phase outlet of the third gas-liquid separating tank 7 is connected with the outside, a liquid phase outlet of the third separating tank 7 is connected with an outside condensed water collecting system, and a liquid phase outlet of the first concentrating tower 3 is connected with an inlet of the fourth brine pump 15, the outlet of the fourth brine pump 15 is connected in parallel with two pipelines, respectively, the first pipeline is converged with the liquid phase outlet of the second concentration tower 4 and then is connected to the inlet of the brine tank 9, the second pipeline is connected with the left end inlet of the tenth heat exchanger 43, the right end outlet of the tenth heat exchanger 43 is connected with the inlet of the second concentration tower 4, the gas phase outlet of the second concentration tower 4 is connected with the lower end inlet of the tenth heat exchanger 43, the upper end outlet of the tenth heat exchanger 43 is connected with the inlet of the fourth gas-liquid separation tank 8, the gas phase outlet of the fourth gas-liquid separation tank 8 is connected with the outside, the liquid phase outlet of the fourth gas-liquid separation tank 8 is connected with an outside condensed water collection system, the liquid phase outlet of the second concentration tower 4 is converged with the first pipeline connected in parallel with the outlet of the fourth brine pump 15 and then is connected to the inlet of the brine tank 9,
the refrigerant circulating system comprises a refrigerant tank 10, a refrigerant pump 21, a fifth heat exchanger 38, a sixth heat exchanger 39, a seventh heat exchanger 40, a generator 11, a twenty-fourth valve 65, a twenty-first valve 70 and a thirtieth valve 58,
the outlet of the refrigerant tank 10 is connected with the inlet of the refrigerant pump 21, the outlet of the refrigerant pump 21 is connected with the inlet of the left end of the sixth heat exchanger 39, the outlet of the right end of the sixth heat exchanger 39 is connected with the inlet of the twenty-first valve 70, the outlet of the twenty-first valve 70 is connected with the inlet of the upper end of the seventh heat exchanger 40, the outlet of the lower end of the seventh heat exchanger 40 is connected in parallel with two pipelines, respectively, the first pipeline is connected with the inlet of the twenty-fourth valve 65, the second pipeline is connected with the inlet of the thirty-first valve 58, the outlet of the thirty-first valve 58 is connected with the inlet of the generator 11, the outlet of the generator 11 is connected with the inlet of the lower end of the sixth heat exchanger 39 after being converged with the outlet pipeline of the twenty-fourth valve 65, the outlet of the upper end of the sixth heat exchanger 39 is connected with the inlet of the lower end of the fifth heat exchanger 38, and the outlet of the upper end of the fifth heat exchanger 38 is connected with the inlet of the refrigerant tank 10,
the cooling water system comprises a ninth heat exchanger 49, a fourth heat exchanger 36, an eleventh valve 47 and a twelfth valve 48,
the cooling water inlet is connected in parallel with two pipelines, respectively, the first pipeline is connected with the inlet of the twelfth valve 48, the second pipeline is connected with the inlet of the eleventh valve 47, the outlet of the twelfth valve 48 is connected with the inlet of the left end of the ninth heat exchanger 49, the outlet of the eleventh valve 47 is connected with the inlet of the left end of the fourth heat exchanger 36, the outlet of the right end of the ninth heat exchanger 49 is converged with the outlet of the right end of the fourth heat exchanger 36 and then is connected to the cooling water outlet together,
the steam system includes a sixth one-way valve 55, a fifteenth valve 56, a fifth one-way valve 59, and a thirteenth valve 51,
the steam inlet is connected in parallel with two pipelines, respectively, the first pipeline is connected with an inlet of a sixth one-way valve 55, the second pipeline is connected with an inlet of a fifth one-way valve 59, an outlet of the sixth one-way valve 55 is connected with an inlet of a fifteenth valve 56, an outlet of the fifteenth valve 56 is connected with a steam inlet of the second concentrating tower 4, a steam outlet of the second concentrating tower 4 is connected with a steam outlet of the first concentrating tower 3 after being converged, an outlet of the fifth one-way valve 59 is connected with an inlet of a thirteenth valve 51, an outlet of the thirteenth valve 51 is connected with a steam inlet of the first concentrating tower 3, and a steam outlet of the first concentrating tower 3 is connected with a steam outlet of the second concentrating tower 4 after being converged.
Further preferably, a first valve 16, a first one-way valve 17 and a first pipeline filter 18 are sequentially arranged on a pipeline between the external wet flue gas and the inlet at the right end of the first heat exchanger 19, a third valve 24 is arranged on the pipeline of the first pipeline in a parallel pipeline at the outlet at the upper end of the first heat exchanger 19, a second one-way valve 25 and a thirty-way valve 74 are arranged on the pipeline between the second pipeline and the inlet at the right end of the second gas-liquid separation tank 6, a branch pipeline, a third one-way valve 28 and a twenty-way valve 71 which are connected with the outside through a fourth valve 27 are sequentially arranged on the pipeline between the gas phase outlet of the second gas-liquid separation tank 6 and the inlet at the right end of the second heat exchanger 29, a branch pipeline and a fourth one-way valve 32 which are connected with the outside through a fifth valve 31 are sequentially arranged on the pipeline between the gas phase outlet of the first gas-liquid separation tank 5 and the gas phase inlet of the first drying tower 1, and a twenty-sixth valve 26 is arranged on a pipeline at an outlet at the upper end of the second heat exchanger 29.
Preferably, a nineteenth valve 67 is arranged on a first pipeline connected in parallel with the outlet of the first brine pump 12, a twentieth valve 69 is arranged on a pipeline between the outlet at the left end of the seventh heat exchanger 40 and the inlet at the lower end of the third heat exchanger 35, a thirty-first valve 50 is arranged on a pipeline between the outlet at the upper end of the ninth heat exchanger 49 and the inlet at the liquid phase of the first drying tower 1, a second valve 22 is arranged on a pipeline between the outlet at the upper end of the fourth heat exchanger 36 and the inlet at the liquid phase of the second drying tower 2, a twenty-seventh valve 68 is arranged on a pipeline between the outlet of the third brine pump 14 and the inlet at the left end of the eighth heat exchanger 41, a seventeenth valve 62 is arranged on a pipeline connected with the gas phase outlet of the third gas-liquid separation tank 7 to the outside, and a fourteenth valve 52 is arranged on a first pipeline connected in parallel with the outlet of the fourth brine pump 15, a sixteenth valve 57 is arranged on the pipeline between the second path and the inlet at the left end of the tenth heat exchanger 43, an eighteenth valve 63 is arranged on the pipeline connecting the gas phase outlet of the fourth gas-liquid separation tank 8 with the outside, and a second temperature sensor 54, an eighth valve 44 and a branch pipeline connected with the outside through a ninth valve 45 are sequentially arranged on the pipeline close to the liquid phase outlet of the second concentration tower 4.
Further preferably, a liquid phase outlet connected with the outside through a tenth valve 46 is arranged at the bottom of the brine tank 9, a third liquid level sensor 66 is arranged at the lower part of the barrel body of the brine tank 9, a liquid phase inlet connected with an outside brine supplementing system through a twenty-fifth valve 64 is arranged at the upper part of the barrel body of the brine tank 9, a control signal of the third liquid level sensor 66 is connected with the twenty-fifth valve 64 through a lead,
a branch pipeline connected with the outside through a sixth valve 34 is arranged on a pipeline between the liquid phase outlet of the first drying tower 1 and the inlet of the second brine pump 13,
a branch pipeline connected with the outside through a seventh valve 37 is arranged on a pipeline between the liquid phase outlet of the second drying tower 2 and the inlet at the left end of the fifth heat exchanger 38,
a first temperature sensor 53 and a branch line connected with the outside through a twentieth valve 42 are sequentially provided on a line between the liquid phase outlet of the first concentrating tower 3 and the inlet of the fourth brine pump 15,
a fifth pressure sensor 75 is arranged on the upper end socket of the first gas-liquid separation tank 5, a control signal of the fifth pressure sensor 75 is connected with the fifth valve 31 through a lead,
a sixth pressure sensor 76 is arranged at the upper end socket of the second gas-liquid separation tank 6, and a control signal of the sixth pressure sensor 76 is connected with the fourth valve 27 through a lead.
Further preferably, a fourth pressure sensor 60 is arranged at the upper end enclosure of the third gas-liquid separation tank 7, and a control signal of the fourth pressure sensor 60 is connected with the seventeenth valve 62 through a lead.
Further preferably, a second pressure sensor 61 is arranged at an upper end enclosure of the fourth gas-liquid separation tank 8, and a control signal of the second pressure sensor 61 is connected with the eighteenth valve 63 through a wire.
Further preferably, a second liquid level sensor 33 is disposed at the lower part of the cylinder of the first drying tower 1, and a control signal of the second liquid level sensor 33 is connected to the sixth valve 34 through a wire.
Further preferably, a first liquid level sensor 20 is disposed at the lower part of the cylinder of the second drying tower 2, and a control signal of the first liquid level sensor 20 is connected to the seventh valve 37 through a wire.
Preferably, an overpressure release port is formed in an upper seal head of the first drying tower 1, a third pressure sensor 30 and a twenty-eighth valve 72 are sequentially arranged on the overpressure release port, a control signal of the third pressure sensor 30 is connected with the twenty-eighth valve 72 through a lead, an overpressure release port is formed in an upper seal head of the second drying tower 2, a first pressure sensor 23 and a twenty-ninth valve 73 are sequentially arranged on the overpressure release port, and a control signal of the first pressure sensor 23 is connected with the twenty-ninth valve 73.
Further preferably, a control signal of the first temperature sensor 53 is connected to the thirteenth valve 51 by a wire, and a control signal of the second temperature sensor 54 is connected to the fifteenth valve 56 by a wire.
The invention has the advantages and beneficial effects that:
1. the principle of the invention is that the partial pressure difference of water vapor between wet flue gas and saline solution is used as the driving force, so that low-temperature saline and wet flue gas are directly contacted for heat exchange, the migration of moisture is realized, and the effect of drying the flue gas is achieved. The dew point of water in the flue gas is reduced along with the reduction of the water in the gas, the dew point of the water in the flue gas is low enough, and the drying effect is better, so that the water condensation and freezing of the gas and the formation of hydrates can be prevented when the carbon is trapped in a multistage compression heat exchange temperature reduction process. The vapor pressure of the salt water is far lower than the water vapor partial pressure of the smoke, so that the drying effect is better compared with the condensation method.
2. The invention can adopt a single-stage drying mode and a two-stage drying mode, and can better adapt to the fluctuation of the smoke quantity caused by the peak value and the valley value of the power consumption.
3. The refrigerant circulating system adopted by the invention can better recover the temperature difference from about 110 ℃ after evaporation and concentration to about-20 ℃ before drying gas, recover heat and reduce the energy consumption of the system. In addition, the flue gas at the inlet and the outlet of each stage of the dryer exchanges heat, and the strong brine in the brine storage tank exchanges heat with the weak brine at the outlet before entering each stage of the dryer, so that the energy is fully recovered. In the process of concentrating the light salt water, each level of light salt water exchanges heat with gas at a gas outlet of the evaporation tank before entering the evaporation tank, so that the effect of preheating is achieved. The process has the characteristics of simple process, low energy consumption and high drying efficiency.
Drawings
FIG. 1 is a schematic view of the present invention; wherein: 1. a first drying tower; 2. a second drying tower; 3. a first concentrating column; 4. a second concentrating tower; 5. a first gas-liquid separation tank; 6. a second knock-out pot; 7. a third gas-liquid separation tank; 8. a fourth gas-liquid separation tank; 9. a brine tank; 10. a refrigerant tank; 11. a generator; 12. a first brine pump; 13. a second brine pump; 14. a third brine pump 15, a fourth brine pump; 16. a first valve; 17. a first check valve; 18. a pipeline filter; 19. a first heat exchanger; 20. a first liquid level sensor; 21. a refrigerant pump; 22. a second valve; 23. a first pressure sensor; 24. a third valve; 25. a second one-way valve; 26. a twenty-sixth valve; 27. a fourth valve; 28. a third check valve; 29. a second heat exchanger; 30. a third pressure sensor; 31. a fifth valve; 32. a fourth check valve; 33. a second liquid level sensor; 34. a sixth valve; 35. a third heat exchanger; 36. a fourth heat exchanger; 37. a seventh valve; 38. a fifth heat exchanger; 39. a sixth heat exchanger; 40. a seventh heat exchanger; 41. an eighth heat exchanger; 42. a twenty-third valve; 43. a tenth heat exchanger; 44. an eighth valve; 45. a ninth valve; 46. a tenth valve; 47. an eleventh valve; 48. a twelfth valve; 49. a ninth heat exchanger; 50. a thirty-first valve; 51. a thirteenth valve; 52. a fourteenth valve; 53. a first temperature sensor; 54. a second temperature sensor; 55. a sixth check valve; 56. a fifteenth valve; 57. a sixteenth valve; 58. a thirtieth valve; 59. a fifth check valve; 60. a fourth pressure sensor; 61. a second pressure sensor; 62. a seventeenth valve; 63. an eighteenth valve; 64. a twenty-fifth valve; 65. a twenty-fourth valve; 66. a third liquid level sensor; 67. a nineteenth valve; 68. a twenty-seventh valve; 69. a twentieth valve; 70. a twenty-first valve; 71. a second twelve-valve; 72. a twenty-eighth valve; 73. a twenty-ninth valve; 74. a third twelve valve; 75. a fifth pressure sensor; 76. and a sixth pressure sensor.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the present invention, the following further provides a clear and complete description of the technical solution of the present invention with reference to the accompanying drawings.
As shown in the attached figure 1, the low-temperature drying system for carbon capture comprises a flue gas treatment system, a brine circulating system, a refrigerant circulating system, a cooling water system and a steam system,
the flue gas treatment system comprises a first heat exchanger 19, a second drying tower 2, a second gas-liquid separation tank 6, a second heat exchanger 29, a first gas-liquid separation tank 5, a first drying tower 1,
the external wet flue gas is connected with the inlet at the right end of the first heat exchanger 19,
a first valve 16, a first one-way valve 17 and a first pipeline filter 18 are sequentially arranged on a pipeline between the outside wet flue gas and the inlet at the right end of the first heat exchanger 19,
the outlet at the left end of the first heat exchanger 19 is connected with the gas phase inlet of the second drying tower 2, the gas phase outlet of the second drying tower 2 is connected with the inlet at the lower end of the first heat exchanger 19, the outlet at the upper end of the first heat exchanger 19 is connected with two pipelines in parallel, respectively, the first pipeline is converged with the outlet pipeline at the upper end of the second heat exchanger 29, the second pipeline is connected with the inlet of the second gas-liquid separation tank 6,
in parallel pipelines at the outlet of the upper end of the first heat exchanger 19, a third valve 24 is arranged on a first pipeline, a second one-way valve 25 and a thirtieth valve 74 are arranged on a pipeline between a second pipeline and the inlet of the second gas-liquid separation tank 6,
the gas phase outlet of the second gas-liquid separation tank 6 is connected with the inlet at the right end of the second heat exchanger 29,
a branch pipeline connected with the outside through a fourth valve 27, a third one-way valve 28 and a twentieth valve 71 are sequentially arranged on a pipeline between the gas phase outlet of the second gas-liquid separation tank 6 and the inlet at the right end of the second heat exchanger 29,
a sixth pressure sensor 76 is arranged at the upper end socket of the second gas-liquid separation tank 6, and a control signal of the sixth pressure sensor 76 is connected with the fourth valve 27 through a lead.
The liquid phase outlet of the second gas-liquid separation tank 6 is connected with an external condensed water collection system, the outlet at the left end of the second heat exchanger 29 is connected with the first gas-liquid separation tank 5, the liquid phase outlet of the first gas-liquid separation tank 5 is connected with the external condensed water collection system, the gas phase outlet of the first gas-liquid separation tank 5 is connected with the gas phase inlet of the first drying tower 1,
a branch pipeline and a fourth one-way valve 32 which are connected with the outside through a fifth valve 31 are sequentially arranged on a pipeline between the gas-phase outlet of the first gas-liquid separation tank 5 and the gas-phase inlet of the first drying tower 1,
a fifth pressure sensor 75 is arranged on the upper end socket of the first gas-liquid separation tank 5, a control signal of the fifth pressure sensor 75 is connected with the fifth valve 31 through a lead,
the gas phase outlet of the first drying tower 1 is connected with the inlet at the lower end of the second heat exchanger 29, the outlet at the upper end of the second heat exchanger 29 is connected with the first pipeline of the outlet at the upper end of the first heat exchanger 19 after being converged and then is connected to an external dry flue gas collecting system,
and a twenty-sixth valve 26 is arranged on a pipeline at an outlet at the upper end of the second heat exchanger 29.
The brine circulating system comprises a brine tank 9, a first brine pump 12, a seventh heat exchanger 40, a third heat exchanger 35, a ninth heat exchanger 49, a first drying tower 1, a second brine pump 13, a fourth heat exchanger 36, a second drying tower 2, a fifth heat exchanger 38, a third brine pump 14, a first concentration tower 3, an eighth heat exchanger 41, a third gas-liquid separation tank 7, a fourth brine pump 15, a tenth heat exchanger 43, a second concentration tower 4, a fourth gas-liquid separation tank 8,
the outlet of the brine tank 9 is connected with the inlet of the first brine pump 12, the outlet of the first brine pump 12 is connected in parallel with two pipelines, respectively, the first pipeline is converged with the pipeline at the outlet of the right end of the third heat exchanger 35 and then is connected to the inlet of the lower end of the fourth heat exchanger 36,
a nineteenth valve 67 is arranged on the first pipeline connected with the outlet of the first brine pump 12 in parallel,
the second path is connected with the inlet at the right end of the seventh heat exchanger 40, the outlet at the left end of the seventh heat exchanger 40 is connected with the inlet at the lower end of the third heat exchanger 35,
a twentieth valve 69 is arranged on a pipeline between the outlet at the left end of the seventh heat exchanger 40 and the inlet at the lower end of the third heat exchanger 35,
an outlet at the upper end of the third heat exchanger 35 is connected with an inlet at the lower end of the ninth heat exchanger 49, an outlet at the upper end of the ninth heat exchanger 49 is connected with a liquid phase inlet of the first drying tower 1,
a thirty-one valve 50 is arranged on a pipeline between an outlet at the upper end of the ninth heat exchanger 49 and a liquid phase inlet of the first drying tower 1,
the liquid phase outlet of the first drying tower 1 is connected with the inlet of the second brine pump 13,
a branch pipeline connected with the outside through a sixth valve 34 is arranged on a pipeline between the liquid phase outlet of the first drying tower 1 and the inlet of the second brine pump 13,
a second liquid level sensor 33 is arranged at the lower part of the cylinder body of the first drying tower 1, and a control signal of the second liquid level sensor 33 is connected with the sixth valve 34 through a lead.
The outlet of the second brine pump 13 is connected with the inlet at the left end of the third heat exchanger 35, the outlet at the right end of the third heat exchanger 35 is merged with the second pipeline connected in parallel with the outlet of the first brine pump 12 and then is connected to the inlet at the lower end of the fourth heat exchanger 36, the outlet at the upper end of the fourth heat exchanger 36 is connected with the liquid phase inlet of the second drying tower 2,
a second valve 22 is arranged on a pipeline between the outlet at the upper end of the fourth heat exchanger 36 and the liquid phase inlet of the second drying tower 2,
the liquid phase outlet of the second drying tower 2 is connected with the inlet at the left end of the fifth heat exchanger 38,
a branch pipeline connected with the outside through a seventh valve 37 is arranged on a pipeline between the liquid phase outlet of the second drying tower 2 and the inlet at the left end of the fifth heat exchanger 38,
a first liquid level sensor 20 is arranged at the lower part of the cylinder of the second drying tower 2, and a control signal of the first liquid level sensor 20 is connected with the seventh valve 37 through a lead.
The outlet of the right end of the fifth heat exchanger 38 is connected with the inlet of the third brine pump 14, the outlet of the third brine pump 14 is connected with the inlet of the left end of the eighth heat exchanger 41,
a twenty-seventh valve 68 is arranged on a pipeline between the outlet of the third brine pump 14 and the inlet at the left end of the eighth heat exchanger 41,
an outlet at the right end of the eighth heat exchanger 41 is connected with an inlet of the first concentrating tower 3, a gas phase outlet of the first concentrating tower 3 is connected with an inlet at the lower end of the eighth heat exchanger 41, an outlet at the upper end of the eighth heat exchanger 41 is connected with an inlet of the third gas-liquid separation tank 7, a gas phase outlet of the third gas-liquid separation tank 7 is connected with the outside,
a seventeenth valve 62 is arranged on a pipeline connecting the gas phase outlet of the third gas-liquid separation tank 7 with the outside,
a fourth pressure sensor 60 is arranged at the upper end enclosure of the third gas-liquid separation tank 7, and a control signal of the fourth pressure sensor 60 is connected with the seventeenth valve 62 through a lead.
The liquid phase outlet of the third gas-liquid separation tank 7 is connected with an external condensed water collecting system, the liquid phase outlet of the first concentrating tower 3 is connected with the inlet of the fourth brine pump 15,
a first temperature sensor 53 and a branch line connected with the outside through a twentieth valve 42 are sequentially provided on a line between the liquid phase outlet of the first concentrating tower 3 and the inlet of the fourth brine pump 15,
the outlet of the fourth brine pump 15 is connected in parallel with two pipelines, respectively, the first pipeline is converged with the liquid phase outlet of the second concentration tower 4 and then is connected to the inlet of the brine tank 9, the second pipeline is connected with the inlet at the left end of the tenth heat exchanger 43,
a fourteenth valve 52 is arranged on the first pipeline connected in parallel with the outlet of the fourth brine pump 15, a sixteenth valve 57 is arranged on the pipeline between the second pipeline and the inlet at the left end of the tenth heat exchanger 43,
an outlet at the right end of the tenth heat exchanger 43 is connected with an inlet of the second concentration tower 4, a gas-phase outlet of the second concentration tower 4 is connected with an inlet at the lower end of the tenth heat exchanger 43, an outlet at the upper end of the tenth heat exchanger 43 is connected with an inlet of the fourth gas-liquid separation tank 8, a gas-phase outlet of the fourth gas-liquid separation tank 8 is connected with the outside,
an eighteenth valve 63 is arranged on a pipeline connecting the gas phase outlet of the fourth gas-liquid separation tank 8 with the outside,
and a second pressure sensor 61 is arranged at the upper end enclosure of the fourth gas-liquid separation tank 8, and a control signal of the second pressure sensor 61 is connected with the eighteenth valve 63 through a lead.
The liquid phase outlet of the fourth gas-liquid separation tank 8 is connected with an external condensed water collecting system, the liquid phase outlet of the second concentration tower 4 is converged with a first pipeline which is connected with the outlet of the fourth brine pump 15 in parallel and then is connected with the inlet of the brine tank 9 together,
a second temperature sensor 54, an eighth valve 44 and a branch line connected to the outside through a ninth valve 45 are sequentially provided on the line near the liquid phase outlet of the second concentrating tower 4.
A liquid phase outlet connected with the outside through a tenth valve 46 is arranged at the bottom of the brine tank 9, a third liquid level sensor 66 is arranged at the lower part of the barrel body of the brine tank 9, a liquid phase inlet connected with an outside brine supplementing system through a twenty-fifth valve 64 is arranged at the upper part of the barrel body of the brine tank 9, a control signal of the third liquid level sensor 66 is connected with the twenty-fifth valve 64 through a lead,
an overpressure release port is formed in the upper end enclosure of the first drying tower 1, a third pressure sensor 30 and a twenty-eighth valve 72 are sequentially arranged on the overpressure release port, a control signal of the third pressure sensor 30 is connected with the twenty-eighth valve 72 through a lead, an overpressure release port is formed in the upper end enclosure of the second drying tower 2, a first pressure sensor 23 and a twenty-ninth valve 73 are sequentially arranged on the overpressure release port, and a control signal of the first pressure sensor 23 is connected with the twenty-ninth valve 73.
The refrigerant circulating system comprises a refrigerant tank 10, a refrigerant pump 21, a fifth heat exchanger 38, a sixth heat exchanger 39, a seventh heat exchanger 40, a generator 11, a twenty-fourth valve 65, a twenty-first valve 70 and a thirtieth valve 58,
the outlet of the refrigerant tank 10 is connected with the inlet of the refrigerant pump 21, the outlet of the refrigerant pump 21 is connected with the inlet of the left end of the sixth heat exchanger 39, the outlet of the right end of the sixth heat exchanger 39 is connected with the inlet of the twenty-first valve 70, the outlet of the twenty-first valve 70 is connected with the inlet of the upper end of the seventh heat exchanger 40, the outlet of the lower end of the seventh heat exchanger 40 is connected in parallel with two pipelines, respectively, the first pipeline is connected with the inlet of the twenty-fourth valve 65, the second pipeline is connected with the inlet of the thirty-first valve 58, the outlet of the thirty-first valve 58 is connected with the inlet of the generator 11, the outlet of the generator 11 is connected with the inlet of the lower end of the sixth heat exchanger 39 after being converged with the outlet pipeline of the twenty-fourth valve 65, the outlet of the upper end of the sixth heat exchanger 39 is connected with the inlet of the lower end of the fifth heat exchanger 38, and the outlet of the upper end of the fifth heat exchanger 38 is connected with the inlet of the refrigerant tank 10,
the cooling water system comprises a ninth heat exchanger 49, a fourth heat exchanger 36, an eleventh valve 47 and a twelfth valve 48,
the cooling water inlet is connected in parallel with two pipelines, respectively, the first pipeline is connected with the inlet of the twelfth valve 48, the second pipeline is connected with the inlet of the eleventh valve 47, the outlet of the twelfth valve 48 is connected with the inlet of the left end of the ninth heat exchanger 49, the outlet of the eleventh valve 47 is connected with the inlet of the left end of the fourth heat exchanger 36, the outlet of the right end of the ninth heat exchanger 49 is converged with the outlet of the right end of the fourth heat exchanger 36 and then is connected to the cooling water outlet together,
the steam system includes a sixth one-way valve 55, a fifteenth valve 56, a fifth one-way valve 59, and a thirteenth valve 51,
the steam inlet is connected in parallel with two pipelines, respectively, the first pipeline is connected with an inlet of a sixth one-way valve 55, the second pipeline is connected with an inlet of a fifth one-way valve 59, an outlet of the sixth one-way valve 55 is connected with an inlet of a fifteenth valve 56, an outlet of the fifteenth valve 56 is connected with a steam inlet of the second concentrating tower 4, a steam outlet of the second concentrating tower 4 is connected with a steam outlet of the first concentrating tower 3 after being converged, an outlet of the fifth one-way valve 59 is connected with an inlet of a thirteenth valve 51, an outlet of the thirteenth valve 51 is connected with a steam inlet of the first concentrating tower 3, and a steam outlet of the first concentrating tower 3 is connected with a steam outlet of the second concentrating tower 4 after being converged.
A control signal of the first temperature sensor 53 is connected to the thirteenth valve 51 by a wire, and a control signal of the second temperature sensor 54 is connected to the fifteenth valve 56 by a wire.
The working method of the low-temperature drying system for carbon capture comprises a primary drying mode and a secondary drying mode. When the power plant is at the power utilization valley value, the flue gas amount is less, and a primary drying mode is adopted; when the power plant is at the peak value of electricity utilization, the smoke gas amount is large, and a secondary drying mode is adopted.
Primary drying mode:
starting up: firstly, after all the valves are determined to be closed, the twenty-fifth valve 64 is opened, the concentrated brine in the brine tank 9 is added to a certain liquid level, the first brine pump 12, the nineteenth valve 67, the second valve 22, the third brine pump 14, the twenty-seventh valve 68, the fourteenth valve 52 and the thirteenth valve 51 are opened, and the brine circulation system and the steam system are opened to preheat the brine. Next, the eleventh valve 47 is opened, and the cooling water system is opened to pre-cool the brine entering the second drying tower 2. Finally, the first valve 16 and the third valve 24 are opened, and the wet flue gas is introduced into the second drying tower 2 for drying.
Stopping the machine: firstly, closing the first valve 16 and stopping introducing external wet flue gas; secondly, closing the thirteenth valve 51, the first temperature sensor 53 and the third liquid level sensor 66, and stopping introducing the steam; thirdly, when the temperature of the brine is reduced to about 50 ℃, closing the eleventh valve 47 and stopping introducing the cooling water; finally, all valves and the instrument control system are closed.
When the primary drying mode is normally operated, the control method of the system is as follows:
when the liquid level in the second drying tower 2 is too high, the seventh valve 37 is opened to discharge according to the signal value of the first liquid level sensor 20; when the liquid level in the brine tank 9 is too low, the seventh valve 37 is opened to replenish the brine tank 9 in the system based on the signal value of the third liquid level sensor 66; when the pressure in the second drying tower 2 is too high, the twenty-ninth valve 73 is opened to release overpressure according to the signal value of the first pressure sensor 23; when the pressure in the third gas-liquid separation tank 7 is too high, the seventeenth valve 62 is opened to release overpressure based on the signal value of the fourth pressure sensor 60. When the temperature of the liquid phase outlet of the first concentrating tower 3 is too low, the opening of the thirteenth valve 51 is increased to increase the steam flow rate by using the signal value of the first temperature sensor 53 as the adjustment basis.
Secondary drying mode:
starting up: firstly, after all the valves are determined to be closed, the twenty-fifth valve 64 is opened, the brine tank 9 is filled with the concentrated brine to a certain liquid level, the first brine pump 12, the twentieth valve 69 and the thirty-first valve 50 are opened, the second brine pump 13, the second valve 22, the third brine pump 14, the twenty-seventh valve 68, the fourth brine pump 15, the sixteenth valve 57, the eighth valve 44, the thirteenth valve 51 and the fifteenth valve 56 are opened, and the brine circulation system and the steam system are opened to preheat the brine. Secondly, the eleventh valve 47, the twelfth valve 48 and the cooling water system are opened to pre-cool the brine entering the first drying tower 1 and the second drying tower 2, and the twenty-fourth valve 65, the refrigerant pump 21 and the twenty-first valve 70 are opened to open the refrigerant circulating system. And finally, opening the first valve 16, the third twelfth valve 74, the twentieth valve 71 and the twenty-sixth valve 26, introducing wet flue gas to the first drying tower 1 and the second drying tower 2 for drying, closing the twenty-fourth valve 65, opening the thirtieth valve 58 and the generator 11 for waste heat recovery and power generation.
Stopping the machine: firstly, closing the first valve 16 to stop introducing the external wet flue gas; secondly, stopping introducing steam by the thirteenth valve 51, the first temperature sensor 53, the fifteenth valve 56 and the second temperature sensor 54; thirdly, when the temperature of the brine is reduced to about 50 ℃, closing the eleventh valve 47 and the twelfth valve 48 and stopping introducing the cooling water; finally, all valves and the instrument control system are closed.
When the secondary drying mode is normally operated, the control method of the system is as follows:
when the pressure in the first gas-liquid separation tank 5 is too high, the fifth valve 31 is opened to release overpressure according to the signal value of the fifth pressure sensor 75; and when the pressure of the second gas-liquid separation tank 6 is too high, the fourth valve 27 is opened for overpressure relief by taking the signal value of the sixth pressure sensor 76 as a regulating basis. And according to the signal value of the third pressure sensor 30 as a regulating basis, when the pressure in the first drying tower 1 is overhigh, the twenty-eighth valve 72 is opened for overpressure relief. Taking the signal value of the second pressure sensor 61 as a regulation basis, when the pressure in the fourth gas-liquid separation tank 8 is too high, opening the eighteenth valve 63 for overpressure relief; when the liquid phase outlet temperature of the second concentrating tower 4 is too low, the opening of the fifteenth valve 56 is increased to increase the steam flow rate based on the signal value of the second temperature sensor 54. The remaining control sections are identical to the control system in the normal operation primary drying mode.
In practice, the relevant equipment should be added to eliminate entrainment of the drying gas at the gas outlet of the dryer, since if the entrainment in the drying gas is too high, on the one hand, when heated by the wet flue gas in the first heat exchanger 19 or the second heat exchanger 29, the moisture in the entrainment increases with the temperature increase, directly affecting the drying quality of the gas. On the other hand, as the water evaporates, salt in the mist also crystallizes out, and there is a risk of clogging pipes or equipment. The related measures comprise that a demister (such as a stainless steel wire mesh and the like) is arranged at a gas outlet of the dryer to increase the demisting effect, and a standby heat exchanger is arranged to be switched to use or a molecular sieve dryer is arranged.
The brine can be selected from water solutions of lithium bromide, lithium chloride, calcium chloride, triethylene glycol and the like, the principle of selecting the brine is the cost and greenness of the brine, the price of the brine is lower, the safety is higher, the influence on the environment is smaller, and the property is stable and non-toxic.
The structural design of the dryer directly influences the heat and mass transfer effect of drying, and the reasonable dryer structure has an important effect on the drying effect. The dryer adopts a direct contact phase change dryer, adopts a spraying (mist) structure, atomizes the solution in the tower by using the atomizing nozzle, increases the gas-liquid contact area, and leads the gas-liquid phase to carry out the heat and mass transfer process on the surface, and has better drying effect, simpler structure, lower manufacturing cost and smaller resistance. In the practical use process, multi-stage spraying can be considered, or a serpentine spraying pipe is arranged in the dryer to optimize the distribution effect of the liquid phase in the dryer.
The foregoing is only a preferred embodiment of the present invention. It should be noted that, for those skilled in the art, various modifications and improvements can be made without departing from the principle of the present invention, and such modifications and improvements should be considered as falling within the scope of the claims of the present invention.
Claims (10)
1. A low-temperature drying system for carbon capture is characterized by comprising a flue gas treatment system, a brine circulating system, a refrigerant circulating system, a cooling water system and a steam system,
the flue gas treatment system comprises a first heat exchanger (19), a second drying tower (2), a second gas-liquid separation tank (6), a second heat exchanger (29), a first gas-liquid separation tank (5) and a first drying tower (1),
the external wet flue gas is connected with the inlet at the right end of the first heat exchanger (19), the outlet at the left end of the first heat exchanger (19) is connected with the gas-phase inlet of the second drying tower (2), the gas-phase outlet of the second drying tower (2) is connected with the inlet at the lower end of the first heat exchanger (19), the outlet at the upper end of the first heat exchanger (19) is connected with two pipelines in parallel, respectively, the first pipeline is converged with the outlet pipeline at the upper end of the second heat exchanger (29), the second pipeline is connected with the inlet of the second gas-liquid separation tank (6), the gas-phase outlet of the second gas-liquid separation tank (6) is connected with the inlet at the right end of the second heat exchanger (29), the liquid-phase outlet of the second gas-liquid separation tank (6) is connected with an external condensed water collecting system, the outlet at the left end of the second heat exchanger (29) is connected with the first gas-liquid separation tank (5), and the liquid-phase outlet of the first gas-liquid separation tank (5) is connected with the external condensed water collecting system, the gas phase outlet of the first gas-liquid separation tank (5) is connected with the gas phase inlet of the first drying tower (1), the gas phase outlet of the first drying tower (1) is connected with the lower end inlet of the second heat exchanger (29), the upper end outlet of the second heat exchanger (29) is connected to an external dry flue gas collecting system after being converged with the first pipeline of the upper end outlet of the first heat exchanger (19),
the brine circulating system comprises a brine tank (9), a first brine pump (12), a seventh heat exchanger (40), a third heat exchanger (35), a ninth heat exchanger (49), a first drying tower (1), a second brine pump (13), a fourth heat exchanger (36), a second drying tower (2), a fifth heat exchanger (38), a third brine pump (14), a first concentration tower (3), an eighth heat exchanger (41), a third gas-liquid separation tank (7), a fourth brine pump (15), a tenth heat exchanger (43), a second concentration tower (4) and a fourth gas-liquid separation tank (8),
the outlet of the brine tank (9) is connected with the inlet of the first brine pump (12), the outlet of the first brine pump (12) is connected in parallel with two pipelines, respectively, the first pipeline is converged with the pipeline at the outlet of the right end of the third heat exchanger (35) and then is connected to the inlet of the lower end of the fourth heat exchanger (36), the second pipeline is connected with the inlet of the right end of the seventh heat exchanger (40), the left end outlet of the seventh heat exchanger (40) is connected with the inlet of the lower end of the third heat exchanger (35), the upper end outlet of the third heat exchanger (35) is connected with the inlet of the lower end of the ninth heat exchanger (49), the upper end outlet of the ninth heat exchanger (49) is connected with the liquid phase inlet of the first drying tower (1), the liquid phase outlet of the first drying tower (1) is connected with the inlet of the second brine pump (13), the outlet of the second brine pump (13) is connected with the inlet of the left end of the third heat exchanger (35), an outlet at the right end of the third heat exchanger (35) is converged with a second pipeline with an outlet of the first brine pump (12) connected in parallel and then is connected to an inlet at the lower end of the fourth heat exchanger (36), an outlet at the upper end of the fourth heat exchanger (36) is connected with an inlet at the liquid phase of the second drying tower (2), an outlet at the liquid phase of the second drying tower (2) is connected with an inlet at the left end of the fifth heat exchanger (38), an outlet at the right end of the fifth heat exchanger (38) is connected with an inlet of the third brine pump (14), an outlet of the third brine pump (14) is connected with an inlet at the left end of the eighth heat exchanger (41), an outlet at the right end of the eighth heat exchanger (41) is connected with an inlet of the first concentration tower (3), a gas phase outlet of the first concentration tower (3) is connected with an inlet at the lower end of the eighth heat exchanger (41), an outlet at the upper end of the eighth heat exchanger (41) is connected with an inlet of the third gas-liquid separation tank (7), the gas phase outlet of the third gas-liquid separation tank (7) is connected with the outside, the liquid phase outlet of the third gas-liquid separation tank (7) is connected with an outside condensed water collecting system, the liquid phase outlet of the first concentration tower (3) is connected with the inlet of a fourth brine pump (15), the outlet of the fourth brine pump (15) is connected with two pipelines in parallel, respectively, the first pipeline is converged with the liquid phase outlet of the second concentration tower (4) and then is connected to the inlet of the brine tank (9), the second pipeline is connected with the left end inlet of the tenth heat exchanger (43), the right end outlet of the tenth heat exchanger (43) is connected with the inlet of the second concentration tower (4), the gas phase outlet of the second concentration tower (4) is connected with the lower end inlet of the tenth heat exchanger (43), the upper end outlet of the tenth heat exchanger (43) is connected with the inlet of the fourth gas-liquid separation tank (8), the gas phase outlet of the fourth gas-liquid separation tank (8) is connected with the outside, the liquid phase outlet of the fourth gas-liquid separation tank (8) is connected with an outside condensed water collecting system, the liquid phase outlet of the second concentration tower (4) and the first pipeline which is connected with the outlet of the fourth brine pump (15) in parallel are converged and then are connected to the inlet of the brine tank (9) together,
the refrigerant circulating system comprises a refrigerant tank (10), a refrigerant pump (21), a fifth heat exchanger (38), a sixth heat exchanger (39), a seventh heat exchanger (40), a generator (11), a twenty-fourth valve (65), a twenty-first valve (70) and a thirty-first valve (58),
an outlet of the refrigerant tank (10) is connected with an inlet of the refrigerant pump (21), an outlet of the refrigerant pump (21) is connected with an inlet at the left end of the sixth heat exchanger (39), an outlet at the right end of the sixth heat exchanger (39) is connected with an inlet of the twenty-first valve (70), an outlet of the twenty-first valve (70) is connected with an inlet at the upper end of the seventh heat exchanger (40), an outlet at the lower end of the seventh heat exchanger (40) is connected with two pipelines in parallel, namely, a first pipeline is connected with an inlet of the twenty-fourth valve (65), a second pipeline is connected with an inlet of the thirty-third valve (58), an outlet of the thirty-third valve (58) is connected with an inlet of the generator (11), an outlet of the generator (11) and an outlet pipeline of the twenty-fourth valve (65) are converged and then connected with an inlet at the lower end of the sixth heat exchanger (39), an outlet at the upper end of the sixth heat exchanger (39) is connected with an inlet at the lower end of the fifth heat exchanger (38), an outlet at the upper end of the fifth heat exchanger (38) is connected with an inlet of the refrigerant tank (10),
the cooling water system comprises a ninth heat exchanger (49), a fourth heat exchanger (36), an eleventh valve (47) and a twelfth valve (48),
the cooling water inlet is connected with two pipelines in parallel, wherein the first pipeline is connected with an inlet of a twelfth valve (48), the second pipeline is connected with an inlet of an eleventh valve (47), an outlet of the twelfth valve (48) is connected with an inlet of the left end of a ninth heat exchanger (49), an outlet of the eleventh valve (47) is connected with an inlet of the left end of the fourth heat exchanger (36), an outlet of the right end of the ninth heat exchanger (49) is converged with an outlet of the right end of the fourth heat exchanger (36) and then is connected with a cooling water outlet together,
the steam system comprises a sixth one-way valve (55), a fifteenth valve (56), a fifth one-way valve (59) and a thirteenth valve (51),
the steam inlet is connected in parallel with two pipelines, the first pipeline is connected with the inlet of the sixth one-way valve (55), the second pipeline is connected with the inlet of the fifth one-way valve (59), the outlet of the sixth one-way valve (55) is connected with the inlet of the fifteenth valve (56), the outlet of the fifteenth valve (56) is connected with the steam inlet of the second concentrating tower (4), the steam outlet of the second concentration tower (4) is merged with the steam outlet pipeline of the first concentration tower (3) and then is connected to the steam outlet together, the outlet of the fifth one-way valve (59) is connected with the inlet of the thirteenth valve (51), the outlet of the thirteenth valve (51) is connected with the steam inlet of the first concentrating tower (3), and the steam outlet of the first concentrating tower (3) and the steam outlet pipeline of the second concentrating tower (4) are converged and then are connected to the steam outlet together.
2. The carbon capture cryogenic drying system of claim 1, a first valve (16), a first one-way valve (17) and a first pipeline filter (18) are sequentially arranged on a pipeline between the external wet flue gas and an inlet at the right end of the first heat exchanger (19), in parallel pipelines at the outlet of the upper end of the first heat exchanger (19), a third valve (24) is arranged on a first pipeline, a second one-way valve (25) and a third twelve-way valve (74) are arranged on a pipeline between a second pipeline and the inlet of the second gas-liquid separation tank (6), a third check valve (28) and a twelfth valve (71) are sequentially arranged on a pipeline between one pipeline and the inlet at the right end of the second heat exchanger (29) in two parallel pipelines at the gas phase outlet of the second gas-liquid separation tank (6), and the other pipeline is connected with the outside through a fourth valve (27); a fourth one-way valve (32) is arranged on a pipeline between one pipeline and a gas phase inlet of the first drying tower (1) in two parallel pipelines at a gas phase outlet of the first gas-liquid separation tank (5), and the other pipeline is connected with the outside through a fifth valve (31); and a twenty-sixth valve (26) is arranged on a pipeline at an outlet at the upper end of the second heat exchanger (29).
3. The low-temperature drying system for carbon capture according to claim 1, wherein a nineteenth valve (67) is arranged on a first pipeline connected in parallel with an outlet of the first brine pump (12), a twentieth valve (69) is arranged on a pipeline between an outlet at the left end of the seventh heat exchanger (40) and an inlet at the lower end of the third heat exchanger (35), a thirty-first valve (50) is arranged on a pipeline between an outlet at the upper end of the ninth heat exchanger (49) and an inlet at the liquid phase of the first drying tower (1), a second valve (22) is arranged on a pipeline between an outlet at the upper end of the fourth heat exchanger (36) and an inlet at the liquid phase of the second drying tower (2), a twenty-seventh valve (68) is arranged on a pipeline between an outlet of the third brine pump (14) and an inlet at the left end of the eighth heat exchanger (41), a seventeenth valve (62) is arranged on a pipeline connecting a gas phase outlet of the third gas-liquid separation tank (7) and the outside, a fourteenth valve (52) is arranged on a first pipeline, the outlet of the fourth brine pump (15) is connected in parallel, a sixteenth valve (57) is arranged on a pipeline between the second pipeline and the inlet of the left end of the tenth heat exchanger (43), an eighteenth valve (63) is arranged on a pipeline, the gas phase outlet of the fourth gas-liquid separation tank (8) is connected with the outside, a second temperature sensor (54), an eighth valve (44) and a branch pipeline, which is connected with the outside through a ninth valve (45), are sequentially arranged on a pipeline, which is close to the liquid phase outlet of the second concentration tower (4).
4. The carbon capture cryogenic drying system of claim 1, wherein a liquid phase outlet connected with the outside through a tenth valve (46) is arranged at the bottom of the brine tank (9), a third liquid level sensor (66) is arranged at the lower part of the barrel of the brine tank (9), a liquid phase inlet connected with an outside supplementary brine system through a twenty-fifth valve (64) is arranged at the upper part of the barrel of the brine tank (9), a control signal of the third liquid level sensor (66) is connected with the twenty-fifth valve (64) through a lead wire,
a branch pipeline connected with the outside through a sixth valve (34) is arranged on a pipeline between the liquid phase outlet of the first drying tower (1) and the inlet of the second brine pump (13),
a branch pipeline connected with the outside through a seventh valve (37) is arranged on a pipeline between the liquid phase outlet of the second drying tower (2) and the inlet at the left end of the fifth heat exchanger (38),
a first temperature sensor (53) and a branch pipeline connected with the outside through a thirteenth valve (42) are sequentially arranged on a pipeline between the liquid phase outlet of the first concentration tower (3) and the inlet of the fourth brine pump (15),
a fifth pressure sensor (75) is arranged on the upper end socket of the first gas-liquid separation tank (5), a control signal of the fifth pressure sensor (75) is connected with the fifth valve (31) through a lead,
and a sixth pressure sensor (76) is arranged on the upper end socket of the second gas-liquid separation tank (6), and a control signal of the sixth pressure sensor (76) is connected with the fourth valve (27) through a lead.
5. The carbon capture low-temperature drying system as claimed in claim 1, wherein a fourth pressure sensor (60) is arranged at an upper head of the third gas-liquid separation tank (7), and a control signal of the fourth pressure sensor (60) is connected with the seventeenth valve (62) through a lead.
6. The carbon capture low-temperature drying system as claimed in claim 1, wherein a second pressure sensor (61) is arranged at the upper head of the fourth gas-liquid separation tank (8), and a control signal of the second pressure sensor (61) is connected with the eighteenth valve (63) through a lead.
7. The carbon capture cryogenic drying system of claim 1, wherein a second liquid level sensor (33) is arranged at the lower part of the cylinder of the first drying tower (1), and a control signal of the second liquid level sensor (33) is connected with the sixth valve (34) through a lead.
8. The carbon capture cryogenic drying system according to claim 1, wherein a first liquid level sensor (20) is arranged at the lower part of the cylinder of the second drying tower (2), and a control signal of the first liquid level sensor (20) is connected with the seventh valve (37) through a lead.
9. The carbon capture low-temperature drying system as claimed in claim 1, wherein an overpressure release port is arranged at an upper head of the first drying tower (1), a third pressure sensor (30) and a twenty-eighth valve (72) are sequentially arranged on the overpressure release port, a control signal of the third pressure sensor (30) is connected with the twenty-eighth valve (72) through a lead, an overpressure release port is arranged at an upper head of the second drying tower (2), a first pressure sensor (23) and a twenty-ninth valve (73) are sequentially arranged on the overpressure release port, and a control signal of the first pressure sensor (23) is connected with the twenty-ninth valve (73).
10. The carbon capture low-temperature drying system as set forth in claim 1, wherein a control signal of the first temperature sensor (53) is connected to the thirteenth valve (51) by a wire, and a control signal of the second temperature sensor (54) is connected to the fifteenth valve (56) by a wire.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111319284.7A CN113893655A (en) | 2021-11-09 | 2021-11-09 | Low-temperature drying system for carbon capture |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111319284.7A CN113893655A (en) | 2021-11-09 | 2021-11-09 | Low-temperature drying system for carbon capture |
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| CN113893655A true CN113893655A (en) | 2022-01-07 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115218610A (en) * | 2022-05-25 | 2022-10-21 | 江苏科技大学 | Efficient carbon capture system based on low-temperature liquefaction of hydrate method and operation method thereof |
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2021
- 2021-11-09 CN CN202111319284.7A patent/CN113893655A/en not_active Withdrawn
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115218610A (en) * | 2022-05-25 | 2022-10-21 | 江苏科技大学 | Efficient carbon capture system based on low-temperature liquefaction of hydrate method and operation method thereof |
| CN115218610B (en) * | 2022-05-25 | 2024-06-04 | 江苏科技大学 | High-efficiency carbon trapping system based on low-temperature liquefaction of hydrate method and operation method thereof |
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Application publication date: 20220107 |