CN218047279U - Desorption tower and ammonia process decarbonization system - Google Patents
Desorption tower and ammonia process decarbonization system Download PDFInfo
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- CN218047279U CN218047279U CN202221691332.5U CN202221691332U CN218047279U CN 218047279 U CN218047279 U CN 218047279U CN 202221691332 U CN202221691332 U CN 202221691332U CN 218047279 U CN218047279 U CN 218047279U
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- 238000003795 desorption Methods 0.000 title claims abstract description 109
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 27
- 238000005262 decarbonization Methods 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 title abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 162
- 238000003860 storage Methods 0.000 claims abstract description 19
- 238000005261 decarburization Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 62
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- 238000005507 spraying Methods 0.000 claims description 22
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 10
- 239000003546 flue gas Substances 0.000 claims description 10
- 239000000945 filler Substances 0.000 claims description 9
- 238000012856 packing Methods 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 abstract description 19
- 230000008929 regeneration Effects 0.000 abstract 1
- 238000011069 regeneration method Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 115
- 239000000047 product Substances 0.000 description 24
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 20
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 11
- 239000001099 ammonium carbonate Substances 0.000 description 11
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 10
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 10
- 239000001569 carbon dioxide Substances 0.000 description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 description 10
- 239000002918 waste heat Substances 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000010793 Steam injection (oil industry) Methods 0.000 description 1
- 235000012501 ammonium carbonate Nutrition 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a desorption tower and ammonia process decarbonization system. The desorption tower comprises a tower body, a gas outlet is arranged at the top of the tower body, a liquid storage area, a first-stage desorption area and a second-stage desorption area are sequentially arranged in the tower body from the bottom to the top, a gas distributor is arranged between the first-stage desorption area and the liquid storage area, a tower tray is arranged between the first-stage desorption area and the second-stage desorption area, a steam inlet is arranged on a tower wall between the liquid storage area and the gas distributor, a barren liquid outlet is arranged on a tower wall of the liquid storage area, and a liquid collection area side wall on the tower tray is provided with a semi-barren liquid outlet. The ammonia process decarbonization system comprises a decarbonization tower and the utility model discloses a desorption tower. The desorption tower of the utility model adopts rich solution to carry out split desorption, recovers the heat of the product gas at the top of the tower, and reduces the temperature of the process gas at the outlet of the regeneration tower; correspondingly, the semi-barren solution and barren solution after rich solution desorption in the ammonia decarburization system respectively enter different positions of the absorption tower for graded absorption, so that the absorption efficiency is improved.
Description
Technical Field
The utility model belongs to the technical field of carbon entrapment and gas cleaning, concretely relates to steam jet formula ammonia process decarbonization desorber and desorption system.
Background
CO is developed under the aim of' carbon peak reaching and carbon neutralization 2 The capture and utilization are of great significance, the most widely applied carbon capture technology at present is a chemical absorption method, and ammonia water is widely applied as a potential absorbent.
Ammonia process for absorbing CO 2 The generated ammonium bicarbonate (namely decarbonization by ammonia process) can be heated and desorbed to produce CO 2 The main energy consumption of ammonia decarburization is desorption energy consumption, a packed tower or a plate tower is used as desorption equipment in a traditional desorption mode, high-grade steam is used for heating a solution at the bottom of the tower, and a steam and carbon dioxide mixed gas generated by a reboiler is in countercurrent contact with a rich solution for heat exchange, so that the rich solution desorbs carbon dioxide. The carbon dioxide desorbed by the prior desorption technology needs to be cooled, cooled and compressed to form CO 2 When the temperature of the desorbed gas is higher, a large amount of waste heat is dissipated.
SUMMERY OF THE UTILITY MODEL
To the defects or deficiencies of the prior art, one aspect of the present invention is to provide a desorber.
Therefore, the desorption tower provided by the utility model comprises a tower body, the top of the tower body is provided with a gas outlet, a liquid storage area, a first-stage desorption area and a second-stage desorption area are sequentially arranged in the tower body from bottom to top, a gas distributor is arranged between the first-stage desorption area and the liquid storage area, a tower tray is arranged between the first-stage desorption area and the second-stage desorption area, a steam inlet is arranged on the tower wall between the liquid storage area and the gas distributor, a barren solution outlet is arranged on the tower wall of the liquid storage area, and a liquid collection area side wall on the tower tray is provided with a semi-barren solution outlet;
a first-stage rich liquid inlet is formed in the tower wall of the first-stage desorption area, a first-stage spraying device and first-stage packing are arranged in the first-stage desorption area, the first-stage spraying device is connected with the first-stage rich liquid inlet, and the first-stage spraying device is positioned above the first-stage packing;
and a second-stage rich liquid inlet is formed in the tower wall of the second-stage desorption area, a second-stage spraying device and a second-stage filler are arranged in the second-stage desorption area, the second-stage spraying device is connected with the second-stage rich liquid inlet, and the second-stage spraying device is positioned above the second-stage filler.
Further, the utility model discloses an analytic tower is still including the cooler, compressor and the vapour and liquid separator that connect gradually, the condenser with gas outlet connects.
Further, the utility model discloses a desorber still includes steam generator, steam jet installs the steam jet ware in the steam inlet department, steam generator with steam jet ware connects.
Further, the utility model discloses an analytic tower still includes the reboiler, the reboiler is connected with the stock solution district of tower body bottom.
Furthermore, a demister is arranged between the secondary desorption zone and the gas outlet and is used for intercepting liquid drops in the product gas; or a water washing spraying layer and a tower tray are arranged between the secondary desorption area and the gas outlet and are used for recovering ammonia in the product gas and reducing the temperature of the product gas.
The utility model discloses another aspect provides an ammonia process decarbonization system.
Therefore, the utility model provides an ammonia process decarbonization system includes decarbonization tower and desorber, decarbonization tower bottom is equipped with flue gas inlet and pregnant solution export, and decarbonization tower top is equipped with the flue gas export after the decarbonization, the decarbonization tower lateral wall is equipped with half barren solution entry and barren solution entry, and half barren solution entry is located the below of barren solution entry, the desorber adopts above-mentioned desorber;
a rich liquid outlet on the decarbonizing tower is connected with a primary rich liquid inlet and a secondary rich liquid inlet;
the semi-barren solution inlet is connected with a semi-barren solution outlet on the desorption tower;
and the barren solution inlet is connected with a barren solution outlet on the desorption tower.
Further, the lean liquid outlet is connected with the lean liquid inlet through a flash tank and a lean liquid pump, and the flash tank is connected with the steam inlet.
Further, the lean solution outlet is connected with the lean solution inlet through a lean and rich solution heat exchanger, the rich solution outlet is connected with the primary rich solution inlet through the lean and rich solution heat exchanger, and lean solution from the lean solution outlet to the lean solution inlet and rich solution from the rich solution outlet to the primary rich solution inlet exchange heat in the lean and rich solution heat exchanger, so that the temperature of the lean solution is reduced, and the temperature of the rich solution is increased.
Further, a gas outlet of the desorption tower is connected with a condenser; the rich liquid outlet is connected with the secondary rich liquid inlet through a condenser, and the rich liquid from the rich liquid outlet to the secondary rich liquid inlet and the gas discharged from the top of the desorption tower are subjected to heat exchange in the condenser, so that the temperature of the rich liquid is increased, and the temperature of the gas is reduced.
Further, the desorption tower is connected with a steam generator, the desorption tower adopts the desorption tower in the scheme, the condenser is connected between the cooler and the condenser, and condensed water generated in the condenser and the cooler is recycled to the steam generator.
Further, condensed water generated in the condenser and the cooler is connected with a steam generator through a semi-lean liquid cooler, the semi-lean liquid outlet is connected with a semi-lean liquid inlet on the desorption tower through the semi-lean liquid cooler, and semi-lean liquid and the condensed water from the semi-lean liquid outlet to the semi-lean liquid inlet are subjected to heat exchange in the semi-lean liquid cooler, so that the temperature of the semi-lean liquid is reduced, and the temperature of the condensed water is increased.
Further, condensed water generated in the condenser and the cooler is connected with the steam generator through a preheater, the lean solution outlet is connected with the lean solution inlet on the desorption tower through the preheater, and heat exchange between the lean solution from the lean solution outlet to the lean solution inlet and the condensed water occurs in the preheater, so that the temperature of the lean solution is reduced, and the temperature of the condensed water is increased.
Further, a lean liquid cooler is connected to the lean liquid inlet.
The utility model discloses a desorber adopts rich solution reposition of redundant personnel desorption, has retrieved the heat of top of the tower product gas, has reduced the temperature of regenerator column export technology gas, has reduced the system energy consumption.
The utility model discloses a half barren liquor and barren liquor after rich liquor desorption get into the different positions of absorption tower and absorb in grades respectively in the ammonia process decarbonization system, have improved absorption efficiency. In some schemes, the system adopts product gas to condense water to generate medium-high pressure steam, uses lean solution to flash to generate secondary steam, and mixes and sprays the secondary steam in a steam ejector to enter the bottom of a desorption tower, so that the consumption of high-grade steam of a reboiler is reduced. In some schemes, the heat of the product gas is recovered by adopting a condenser or/and a cooler, the water content and the ammonia concentration of the product gas are reduced, and the product gas concentration is improved. In a further scheme, waste heat is adopted to heat condensed water, so that the system economy is improved. In some other schemes, the liquid ammonia returns to the absorption tower after the product gas is compressed, so that the problem that the low-concentration ammonia water is difficult to recycle is avoided, the concentration of the absorbent is supplemented, and CO with higher pressure is obtained 2 And (5) producing the product.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
Unless otherwise specified, the terminology herein is to be understood in light of the knowledge of one of ordinary skill in the relevant art.
The directions or orientations of the upper part, the lower part, the bottom part, the top part, the side part, etc. described herein are consistent with the corresponding directions or orientations in the drawings, and it should be noted that the directions or orientations indicated in the drawings are a specific example of the present invention, and equivalent rotation and exchange performed by those skilled in the art based on the disclosure herein are within the scope of the present invention.
The rich, lean, and semi-lean solutions described herein are based on absorbing CO in the liquid 2 Characterised by the relative content, in contrast, of rich CO 2 The lean solution and the semi-lean solution are absorption solutions desorbed to different degrees, the desorption degrees of the absorption solutions are different, the desorption degree of the lean solution at the bottom of the tower is higher and is called lean solution, the desorption degree of the lean solution at the middle of the tower is not high, but the absorption solution still has absorption capacity and is called semi-lean solution.
The rich solution to be desorbed in the desorption tower adopts a split-flow desorption process, one part of the rich solution exchanges heat with the barren solution and then enters a first-stage rich solution inlet 5G of the desorption tower, and the other part of the rich solution exchanges heat with the product gas in a condenser and then enters a second-stage rich solution inlet 5E at the upper part of the desorption tower; and (3) condensing, cooling, compressing and carrying out gas-liquid separation on 5M product gas at a gas outlet of the desorption tower to form a carbon dioxide product. The following detailed description of the present invention will be made with reference to the accompanying drawings and examples.
Example 1:
referring to fig. 1, the desorption tower of the present invention comprises a tower body 5, a gas outlet 5M is provided at the bottom of the tower body, a liquid storage area, a first-stage desorption area and a second-stage desorption area are sequentially provided from the bottom to the top in the tower, a lean liquid outlet 5H is provided on the tower wall of the liquid storage area, a gas distributor 5A is provided between the liquid storage area and the first-stage desorption area, a tower tray 5C is provided between the first-stage desorption area and the second-stage desorption area, a steam inlet is provided on the tower wall between the liquid storage area and the gas distributor, and a half lean liquid outlet 5F is provided on the side wall of the liquid collection area above the tower tray; a first-stage rich liquid inlet 5G is formed in the tower wall of the first-stage desorption area, a first-stage spraying device and a first-stage filler 5B are arranged in the first-stage desorption area, and the first-stage spraying device is connected with the first-stage rich liquid inlet and is positioned above the first-stage filler; and a second-stage rich liquid inlet 5E is formed in the tower wall of the second-stage desorption area, a second-stage spraying device and a second-stage filler 5K are arranged in the second-stage desorption area, the second-stage spraying device is connected with the second-stage rich liquid inlet, and the second-stage spraying device is positioned above the second-stage filler.
In operation, the ammonium bicarbonate slurry to be desorbed (i.e., the absorbed solute-containing gas)Bulk CO 2 Rich solution with higher concentration) enters a primary spraying device and a secondary spraying device through a primary rich solution inlet and a secondary rich solution inlet respectively and is sprayed into the tower; meanwhile, the hot steam introduced from the steam inlet heats the rich liquid from top to bottom in the tower, the rich liquid is in countercurrent contact with the hot steam to perform sufficient gas-liquid heat and mass transfer, the filler can increase the gas-liquid contact area in the process and strengthen the mass transfer effect, the ammonium bicarbonate in the liquid phase is continuously decomposed and releases carbon dioxide in the heating process, and the CO absorbed in the rich liquid is subjected to the action of steam stripping 2 Releasing to regenerate rich ammonium bicarbonate solution to obtain CO 2 The carbon dioxide concentration in the gas phase is continuously enriched, and the carbon dioxide product gas with higher concentration obtained at the tower top is discharged or recovered through a gas outlet; at the same time, the rich solution is reduced to low CO 2 The loaded barren solution is fully contacted with hot steam, the concentration of carbon dioxide in the liquid phase is continuously reduced in the process that the pregnant solution falls from top to bottom, barren solution with lower concentration of carbon dioxide is obtained at the bottom of the tower, and is stored in a liquid storage area and discharged through a barren solution port after being stored for a certain amount; in the desorption process, because the temperature (50-75 ℃) of the secondary desorption area at the upper part in the tower is lower than the temperature (75-85 ℃) of the primary desorption area, the rich liquid forms semi-lean liquid after being desorbed by the secondary desorption area, and most of the semi-lean liquid is collected by the tray, gathered above the tray and discharged through a lean liquid outlet. In the specific process, the temperature in the desorption tower is 60-120 ℃, preferably 70-85 ℃, and the pressure in the desorption tower is 0.1-1MPa.
In a further scheme, a product gas recovery device is connected to the position of a gas outlet 5M at the top of the tower, and the product gas recovery device specifically comprises a cooler 12, a compressor 13 and a gas-liquid separation tank 14 which are connected in sequence, wherein a condenser is connected with the gas outlet. The product gas is cooled by the cooler and then is compressed by the compressor, and then is cooled and liquefied and gas-liquid separated in the gas-liquid separation tank, the temperature in the tank is controlled below the liquefaction temperature of liquid ammonia, the generated gas is carbon dioxide, the liquid is liquid ammonia, the product gas is discharged from the top of the tank, and the liquid ammonia is stored in the tank and can be discharged from the bottom of the tank.
In still some further schemes, the tower body is externally connected with a steam generator 17 (such as a boiler and the like), a steam ejector 18 is installed at a steam inlet, the steam generator is connected with the steam ejector 18 and supplies hot steam to the tower, and the steam ejector can increase the pressure of the ejection fluid without directly consuming mechanical energy.
In some schemes, a reboiler 6 is externally connected to a liquid storage area at the bottom of the tower body, the reboiler is used for providing desorption heat when the amount of externally input hot steam is small, and is used for reaction heat of desorption, heat of water temperature rise and the like, and a heat source of the reboiler can adopt heat sources such as steam, medium-high temperature waste heat and the like.
In still other schemes, a demister is arranged between the secondary desorption zone and the gas outlet in the tower and is used for intercepting liquid drops in the product gas. Or a water washing spraying layer and a tower tray are arranged between the secondary desorption area and the gas outlet and are used for recovering ammonia in the product gas and reducing the temperature of the gas.
Example 2:
the embodiment is an ammonia decarburization system comprising a desorption tower 5 and an absorption tower 2 in embodiment 1, wherein the bottom of the absorption tower is provided with a flue gas inlet 1A and a rich liquid outlet 1F, the top of the tower is provided with a decarbonized flue gas outlet 1B, the side wall of the tower is provided with a semi-lean liquid inlet 1D and a lean liquid inlet 1C, and the semi-lean liquid inlet is positioned below the lean liquid inlet;
the rich liquid outlet is connected with a first-stage rich liquid inlet and a second-stage rich liquid inlet on the desorption tower, and the rich liquid to be desorbed can be conveyed to the first-stage rich liquid inlet and the second-stage rich liquid inlet in two ways by connecting a rich liquid pump 3 in the specific scheme;
the semi-barren liquor inlet is connected with the semi-barren liquor outlet;
the lean solution inlet is connected with the lean solution outlet.
At the beginning of the work, containing CO 2 Flue gas enters a decarbonizing tower through a flue gas cooler 1, the flue gas and ammonia water introduced from a barren solution inlet and a semi-barren solution inlet in the decarbonizing tower are in countercurrent contact reaction to generate ammonium bicarbonate solution, the ammonium bicarbonate solution is stored at the bottom of the decarbonizing tower, the temperature in the decarbonizing tower is 20-40 ℃, the pressure in the decarbonizing tower is 0.1-1MPa, when the ammonium bicarbonate solution (namely rich solution) at the bottom of the decarbonizing tower reaches a certain amount, ammonium bicarbonate slurry enters a desorption tower through a rich solution pump 3, a primary rich solution inlet and a secondary rich solution inlet in two ways to generate barren solution and semi-barren solution, and the barren solution and the semi-barren solution are sent into the decarbonizing towerThe liquid is subjected to countercurrent contact reaction for decarbonization to produce ammonium bicarbonate solution, the ammonium bicarbonate solution is circularly sent into a desorption tower for desorption, the decarbonized absorption liquid is recycled, after the system is stable, the barren solution and the semi-barren solution form a circular absorption liquid mainly containing ammonium carbonate, ammonia and the like, and a proper amount of ammonia can be supplied according to the absorption capacity of the barren solution and the semi-barren solution in the process.
In order to fully utilize the heat energy, in some schemes, the barren liquor outlet is connected with the barren liquor inlet through a flash tank 7, specifically, the barren liquor outlet is connected with the barren liquor inlet through the flash tank 7 and a barren liquor pump 8, the flash tank is connected with the steam inlet, and secondary steam generated by the flash tank 7 is used in the desorption tower. In a further scheme, the steam inlet is connected with a steam jet nozzle 18 provided with a primary steam inlet and a secondary steam inlet, and the secondary steam inlet is positioned at the rear end of the primary steam inlet in the airflow direction; when the steam generator works, steam at the primary steam inlet comes from the steam generator and is high-pressure steam, steam at the secondary steam inlet comes from the flash tank, the secondary steam in the flash tank enters the nozzle through the secondary steam inlet at lower pressure, the high-pressure steam and the low-pressure steam are mixed and then enter the mixing chamber in the nozzle, the pressure is further increased at the diffusion section of the nozzle along with pressure increase while the speed is balanced, and therefore the steam pressure can be increased without directly consuming mechanical energy. In the specific scheme, the primary steam pressure is 0.1-0.5MPa, the secondary steam pressure is 0.01-0.3MPa, and the compression ratio (the ratio of the static pressure at the outlet of the ejector to the static pressure at the inlet of the secondary steam) is 1.5-5, preferably 1.8-2.2; the entrainment ratio (ratio of secondary steam mass flow to primary steam mass flow) is preferably 0.4.
In order to improve the utilization rate of the heat energy of the system, in some schemes, the lean solution outlet is connected with the lean solution inlet through the lean-rich solution heat exchanger 10, the rich solution outlet is connected with the primary rich solution inlet through the lean-rich solution heat exchanger 10, and the lean solution from the lean solution outlet to the lean solution inlet and the rich solution from the rich solution outlet to the primary rich solution inlet exchange heat in the lean-rich solution heat exchanger, so that the temperature of the lean solution is reduced, and the temperature of the rich solution is increased. In a further scheme, the lean solution inlet is connected with the lean solution inlet through a flash tank 7, a lean solution pump 8 and a lean-rich solution heat exchanger 10 in sequence.
In order to provide the waste liquid utilization rate, in some schemes, a gas outlet of the desorption tower is connected with a condenser 4, a rich liquid outlet is connected with a secondary rich liquid inlet through the condenser 4, and during work, the rich liquid and product gas entering the condenser are subjected to heat exchange, so that the temperature of the rich liquid is increased, and the temperature of the product gas is reduced. In a further scheme, condensed water generated in the condenser 4 is recycled to the steam generator to generate steam for the desorption tower to use. In a further scheme, for the desorption tower provided with a product gas recovery device, the condenser 4 is connected between a gas outlet and the cooler, and condensed water generated in the condenser 4 and the cooler 2 is recovered to the steam generator to generate steam for the desorption tower to use. In the specific scheme, cooling water outlets of the condenser and the cooler are connected with the steam generator through a waste heat exchanger 16, the waste heat exchanger is used for heating condensed water, and waste heat can adopt medium-high temperature waste hot water, medium-low pressure waste steam and the like. In a preferred embodiment, the heat in the desorber is from injected steam, wherein the primary steam is generated from condensed water in the overhead product gas and the secondary steam is formed from the lean bottoms liquid by flash evaporation in a flash drum.
In still other embodiments, the condensed water generated in the condenser 4 and the cooler 2 is connected to the steam generator through a semi-lean liquid cooler 15, a semi-lean liquid outlet 5F is connected to a semi-lean liquid inlet on the desorption tower through the semi-lean liquid cooler, and the semi-lean liquid and the condensed water from the semi-lean liquid outlet to the semi-lean liquid inlet are subjected to heat exchange in the semi-lean liquid cooler, so that the semi-lean liquid temperature is lowered and the condensed water temperature is raised.
In other schemes, condensed water generated in the condenser and the cooler is connected with a steam generator through a preheater 9, a barren solution outlet is connected with a barren solution inlet on the desorption tower through the preheater 9, and barren solution from the barren solution outlet to the barren solution inlet is subjected to heat exchange with the condensed water in the preheater, so that the temperature of the barren solution is reduced, and the temperature of the condensed water is increased. The preheater 9 heats the condensate of the condenser and the cooler by utilizing the energy of waste heat to generate primary steam, the barren solution at the tower bottom generates secondary low-pressure steam through flash evaporation, the grade of the secondary steam is improved in a steam injection mode, and the energy consumption of a system is reduced.
In a further scheme, condensed water generated in the condenser 4 and the cooler 2 is connected with a steam generator sequentially through the semi-lean liquid cooler 15 and the preheater 9. In still some further arrangements, the lean liquor outlet is connected to the lean liquor inlet sequentially through a flash drum 7, a preheater 9 and a lean-rich liquor heat exchanger 10.
In still other embodiments, the liquid ammonia in the gas-liquid separation tank 14 is returned to the decarbonizing column 2 via a pipeline to supplement the absorbent concentration.
On the basis of the scheme, in order to ensure that the temperature requirement in the absorption tower is met when the barren solution enters the absorption tower in the further scheme, a barren solution cooler 11 is connected at a barren solution inlet, and the barren solution entering the barren solution inlet is introduced into the absorption tower after being further cooled by the barren solution cooler.
The above description and drawings of this embodiment represent the preferred embodiments of the present invention, and can be adjusted according to the flue gas parameters, the construction site conditions, and the like during actual operation.
Claims (13)
1. A desorption tower comprises a tower body and is characterized in that a gas outlet is formed in the top of the tower body, a liquid storage area, a first-stage desorption area and a second-stage desorption area are sequentially arranged in the tower body from bottom to top, a gas distributor is arranged between the first-stage desorption area and the liquid storage area, a tower tray is arranged between the first-stage desorption area and the second-stage desorption area, a steam inlet is formed in the tower wall between the liquid storage area and the gas distributor, a barren solution outlet is formed in the tower wall of the liquid storage area, and a semi-barren solution outlet is formed in the side wall of the liquid collection area on the tower tray;
a first-stage rich liquid inlet is formed in the tower wall of the first-stage desorption area, a first-stage spraying device and first-stage packing are arranged in the first-stage desorption area, the first-stage spraying device is connected with the first-stage rich liquid inlet, and the first-stage spraying device is positioned above the first-stage packing;
and a second-stage rich liquid inlet is formed in the tower wall of the second-stage desorption area, a second-stage spraying device and a second-stage filler are arranged in the second-stage desorption area, the second-stage spraying device is connected with the second-stage rich liquid inlet, and the second-stage spraying device is positioned above the second-stage filler.
2. The desorption column according to claim 1, further comprising a cooler, a compressor and a gas-liquid separator connected in this order, the cooler being connected to the gas outlet.
3. The desorption column according to claim 1, further comprising a steam generator, wherein a steam ejector is installed at the steam inlet, and the steam generator is connected to the steam ejector.
4. The desorber as recited in claim 1 further comprising a reboiler connected to the liquid storage zone at the bottom of the tower.
5. A desorption tower as claimed in claim 1, wherein a demister is arranged between said secondary desorption zone and the gas outlet for intercepting liquid droplets in the product gas; or a water washing spraying layer and a tower tray are arranged between the secondary desorption area and the gas outlet and are used for recovering ammonia in the product gas and reducing the temperature of the product gas.
6. An ammonia decarburization system, which comprises a decarburization tower and a desorption tower, wherein the bottom of the decarburization tower is provided with a flue gas inlet and a rich liquid outlet, and the top of the decarburization tower is provided with a decarbonized flue gas outlet, and the decarburization tower is characterized in that the side wall of the decarburization tower is provided with a semi-barren liquid inlet and a barren liquid inlet, the semi-barren liquid inlet is positioned below the barren liquid inlet, and the desorption tower adopts the desorption tower in claim 1;
a rich solution outlet on the decarbonizing tower is connected with the primary rich solution inlet and the secondary rich solution inlet;
the semi-barren solution inlet is connected with a semi-barren solution outlet on the desorption tower;
the lean liquid inlet is connected with a lean liquid outlet on the desorption tower.
7. The ammonia decarbonization system of claim 6 wherein the lean liquid outlet is coupled to the lean liquid inlet via a flash tank and a lean liquid pump, and the flash tank is coupled to the steam inlet.
8. The ammonia decarburization system as set forth in claim 6, wherein the lean liquid outlet is connected to the lean liquid inlet through a lean-rich liquid heat exchanger, and the rich liquid outlet is connected to the primary rich liquid inlet through the lean-rich liquid heat exchanger, and the lean liquid from the lean liquid outlet to the lean liquid inlet and the rich liquid from the rich liquid outlet to the primary rich liquid inlet are subjected to heat exchange in the lean-rich liquid heat exchanger, so that the temperature of the lean liquid is lowered and the temperature of the rich liquid is raised.
9. The ammonia decarburization system as recited in claim 6, wherein a condenser is connected to the gas outlet of the desorption tower; the rich liquid outlet is connected with the secondary rich liquid inlet through a condenser, and the rich liquid from the rich liquid outlet to the secondary rich liquid inlet and the gas discharged from the top of the desorption tower are subjected to heat exchange in the condenser, so that the temperature of the rich liquid is increased, and the temperature of the gas is reduced.
10. The ammonia decarburization system as set forth in claim 9, wherein a steam generator is connected to the desorption tower, the desorption tower is the desorption tower as set forth in claim 2, the condenser is connected between a cooler and a condenser, and condensed water generated in the condenser and the cooler is recycled to the steam generator.
11. The ammonia decarburization system as recited in claim 10, wherein condensed water produced in the condenser and the cooler is connected to a steam generator through a semi-lean liquid cooler, the semi-lean liquid outlet is connected to a semi-lean liquid inlet on the desorption tower through the semi-lean liquid cooler, and the semi-lean liquid from the semi-lean liquid outlet to the semi-lean liquid inlet is heat exchanged with the condensed water in the semi-lean liquid cooler, so that the temperature of the semi-lean liquid is lowered and the temperature of the condensed water is raised.
12. The ammonia decarburization system as set forth in claim 10, wherein condensed water produced in the condenser and the cooler is connected to a steam generator through a preheater, the lean liquid outlet is connected to a lean liquid inlet on the desorption tower through the preheater, and heat exchange between the lean liquid from the lean liquid outlet to the lean liquid inlet and the condensed water occurs in the preheater, so that the temperature of the lean liquid is lowered and the temperature of the condensed water is raised.
13. The ammonia decarburization system as recited in any one of claims 6 to 12, wherein a lean liquid cooler is connected to the lean liquid inlet.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116422107A (en) * | 2023-04-27 | 2023-07-14 | 四川益能康生环保科技有限公司 | Energy-saving system and process for steam injection regeneration of organic amine solution |
| CN116603365A (en) * | 2023-05-15 | 2023-08-18 | 科貝森(沈阳)能源科技有限责任公司 | A skid-mounted coalbed methane MDEA deep decarbonization absorption device and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116422107A (en) * | 2023-04-27 | 2023-07-14 | 四川益能康生环保科技有限公司 | Energy-saving system and process for steam injection regeneration of organic amine solution |
| CN116603365A (en) * | 2023-05-15 | 2023-08-18 | 科貝森(沈阳)能源科技有限责任公司 | A skid-mounted coalbed methane MDEA deep decarbonization absorption device and method |
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