CN221287430U - Hydraulic jet regeneration energy-saving system for organic amine solution - Google Patents
Hydraulic jet regeneration energy-saving system for organic amine solution Download PDFInfo
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- CN221287430U CN221287430U CN202321800263.1U CN202321800263U CN221287430U CN 221287430 U CN221287430 U CN 221287430U CN 202321800263 U CN202321800263 U CN 202321800263U CN 221287430 U CN221287430 U CN 221287430U
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- 230000008929 regeneration Effects 0.000 title claims abstract description 89
- 238000011069 regeneration method Methods 0.000 title claims abstract description 89
- 150000001412 amines Chemical class 0.000 title claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 94
- 239000007789 gas Substances 0.000 description 32
- 238000000034 method Methods 0.000 description 15
- 238000010521 absorption reaction Methods 0.000 description 9
- 239000002253 acid Substances 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000003723 Smelting Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002608 ionic liquid Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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- Gas Separation By Absorption (AREA)
Abstract
The utility model provides a hydraulic jet regeneration energy-saving system for an organic amine solution, wherein a rich liquid output end of a lean-rich liquid heat exchanger is communicated with a liquid inlet end of a gas-liquid heat exchanger, a liquid outlet end of the gas-liquid heat exchanger is communicated with a liquid inlet end of an upper part of a regeneration tower, an air outlet end of the top of the regeneration tower is communicated with an air inlet end of the gas-liquid heat exchanger, an air outlet end of the gas-liquid heat exchanger is communicated with an air inlet end of a regeneration gas condenser, a liquid outlet end of the bottom of the regeneration tower is communicated with a part of a liquid booster pump inlet, the other part of the liquid outlet end of the regeneration tower is communicated with a liquid inlet end of an upper part of a flash tank, a liquid outlet end of the lower part of the flash tank is communicated with a lean liquid inlet end of the lean-rich liquid heat exchanger, a steam reboiler is connected to the bottom of the regeneration tower, steam is connected to a reboiler inlet, and serves as a regeneration heat source, an outlet of the booster pump is connected with a power inlet end of an ejector, and a steam output end of the upper part of the flash tank is communicated with an input end of the ejector which is sucked. The system can reduce the heat consumption of the solution by 20-30% and improve the regeneration quality of the organic amine solution.
Description
Technical Field
The utility model relates to the technical field of CO 2 or SO 2 trapping, in particular to a hydraulic jet regeneration energy-saving system of an organic amine solution.
Background
Along with the serious environmental impact of SO 2 in industrial flue gas, flue gas desulfurization is a main technical means for controlling sulfur dioxide pollution, and renewable organic amine SO 2 trapping technology is more and more emphasized, but a large amount of steam is consumed for amine solution regeneration, SO that the application range is limited.
The basic reaction trapped by the amine method SO 2 is as follows:
SO2 + H2O + R2NH ←→ R2NH2HSO3 + Q (1)
As more and more CO 2 is emitted into the atmosphere, the resulting air pollution and greenhouse effect are severely threatening the environment in which humans survive, and the capture of CO 2 has become a global concern for "hot spots".
The trapping technology of CO 2 includes solvent absorption method, adsorption method, low-temperature separation method, membrane separation method, etc. Among them, the organic amine solvent absorption method is the most widely used CO 2 capturing method, mainly including Monoethanolamine (MEA) method, sterically hindered amine method, ionic liquid method, etc.
The basic reaction captured by Monoethanolamine (MEA) process CO 2 is as follows:
CO2 + 2HOCH2CH2NH2 + H2O ＝ HOCH2CH2HNCOO- + HOCH2CH2NH3 + + Q (2)
The basic reaction captured by the sterically hindered amine and ionic liquid method CO 2 is as follows:
CO2+H2O + R3N ←→ RNH.HCO3 + Q (3)
The three desulfurization and decarbonization processes relate to exothermic reaction processes with reduced gas volumes, the low-temperature and high-pressure environments are favorable for gas absorption, the high-temperature and low-pressure environments are favorable for solution regeneration, and the high-temperature and low-pressure environments cannot be achieved in the same regeneration tower.
At present, for capturing SO 2 and CO 2 in flue gas, a general primary absorption-primary regeneration flow is adopted, a regeneration system is shown in figure 1, the regeneration system mainly comprises a regeneration tower 20, a lean-rich liquid heat exchanger 10, a regeneration gas condenser 30, a regeneration gas separator 40 and a steam reboiler 50, the process flow is simple, equipment is few, the temperature of rich liquid coming out of the lean-rich liquid heat exchanger is small in phase difference with the temperature of regenerated acid gas coming out of the top of the regeneration tower, heat of the regenerated acid gas cannot be utilized, a large amount of stripping steam and the regenerated acid gas are cooled by circulating water together, and the steam consumption is large.
Disclosure of utility model
In view of the above, the present utility model provides a hydraulic jet regeneration energy-saving system for an organic amine solution, which flashes out secondary steam from a hot lean solution by suction of a hydraulic jet ejector, and reduces the temperature of the lean solution entering a lean rich solution heat exchanger, thereby reducing the temperature of the rich solution exiting the lean rich solution heat exchanger, wherein the temperature of the rich solution is greatly different from the temperature of regenerated acid gas exiting the top of a regeneration tower, and the heat of the regenerated acid gas is reused by using a gas-liquid heat exchanger, so that the heat consumption of solution regeneration is greatly reduced.
The technical scheme of the utility model is as follows:
The utility model provides a hydraulic jet regeneration energy-saving system of an organic amine solution, which comprises a lean-rich liquid heat exchanger, a regeneration tower, a regeneration gas condenser, a regeneration gas separator, a steam reboiler, a flash tank, a hydraulic ejector, a gas-liquid heat exchanger and a booster pump, wherein the rich liquid output end of the lean-rich liquid heat exchanger is communicated with the liquid inlet end of the gas-liquid heat exchanger, the liquid outlet end of the gas-liquid heat exchanger is communicated with the liquid inlet end of the upper part of the regeneration tower, the gas outlet end of the gas-liquid heat exchanger is communicated with the gas inlet end of the regeneration gas condenser, the liquid outlet end of the bottom of the regeneration tower is partially communicated with a liquid booster pump inlet, the other part of the gas outlet end of the bottom of the regeneration tower is communicated with the lean liquid inlet end of the lean-rich liquid heat exchanger, the steam reboiler is connected to the bottom of the regeneration tower, the steam is connected to the inlet of the regeneration tower, the booster pump outlet is connected to the power inlet end of the ejector, the ejector is provided with power, the upper steam output end of the flash tank is communicated with the sucked input end of the ejector, and the output end of the ejector is communicated with the mixed steam input end of the regeneration tower.
The utility model has the beneficial effects that:
According to the hydraulic jet regeneration energy-saving system, the lean-rich liquid heat exchanger, the regeneration tower, the regenerated gas condenser, the regeneration gas separator, the steam reboiler, the flash tank, the hydraulic ejector, the gas-liquid heat exchanger and the booster pump are arranged to be matched, lean liquid from the regeneration tower enters the flash tank and is sucked by the hydraulic ejector, and secondary steam is steamed out to serve as a direct steam heat source of the regeneration tower; the temperature of the lean solution after the decompression flash evaporation is reduced by 10-20 ℃, the lean solution exchanges heat with the rich solution from the absorption system, and exchanges heat with the regenerated gas from the top of the regeneration tower, so that the energy of the regenerated gas is secondarily utilized. The hydraulic jet regeneration energy-saving system provided by the utility model is suitable for a primary absorption process, optimizes the traditional primary absorption-primary regeneration process, and can reduce the steam consumption by 20-30% on the premise of not increasing the power consumption.
The preferred embodiments of the present utility model and their advantageous effects will be described in further detail with reference to specific embodiments.
Drawings
The accompanying drawings are included to provide a further understanding of the utility model, and are incorporated in and constitute a part of this specification, illustrate the utility model and together with the description serve to explain the utility model. In the drawings of which there are shown,
FIG. 1 is a schematic diagram of a general (prior art) primary absorption-primary regeneration scheme;
Fig. 2 is a schematic diagram of the hydrojet regeneration energy saving system of the present utility model.
Detailed Description
The following describes specific embodiments of the present utility model in detail with reference to the drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the utility model, are not intended to limit the utility model.
Referring to fig. 2, the utility model provides a hydraulic jet regeneration energy-saving system for an organic amine solution, which comprises a lean-rich liquid heat exchanger 1, a regeneration tower 2, a regeneration gas condenser 3, a regeneration gas separator 4, a steam reboiler 5, a flash tank 6, a hydraulic jet 7, a gas-liquid heat exchanger 8 and a booster pump 9. The rich liquid output end of the lean and rich liquid heat exchanger 1 is communicated with the liquid inlet end of the gas-liquid heat exchanger 8, the liquid outlet end of the gas-liquid heat exchanger 8 is communicated with the liquid inlet end at the upper part of the regeneration tower 2, the gas outlet end at the top end of the regeneration tower 2 is communicated with the gas inlet end of the gas-liquid heat exchanger 8, and the gas outlet end of the gas-liquid heat exchanger 8 is communicated with the gas inlet end of the regenerated gas condenser 3. The liquid outlet end of the bottom of the regeneration tower 2 is communicated with the liquid inlet end of the upper part of the flash tank 6 and the inlet of the booster pump 9, the liquid outlet end of the lower part of the flash tank 6 is communicated with the liquid inlet end of the lean and rich liquid heat exchanger 1, the steam reboiler 5 is connected to the bottom of the regeneration tower 2 and used as a regeneration heat source, the outlet of the booster pump 9 is connected with the power inlet end of the ejector 7 to provide power for the ejector 7, the steam output end of the upper part of the flash tank 6 is communicated with the sucked air input end of the ejector 7, and the output end of the ejector 7 is communicated with the mixed steam input end of the lower part of the regeneration tower 2.
According to the hydraulic jet regeneration energy-saving system for the organic amine solution, provided by the utility model, the lean-rich liquid heat exchanger 1, the regeneration tower 2, the regenerated gas condenser 3, the regeneration gas separator 4, the steam reboiler 5, the flash tank 6, the hydraulic jet 7, the gas-liquid heat exchanger 8 and the booster pump 9 are arranged to be matched, lean liquid after CO 2 or SO 2 is regenerated is discharged from the regeneration tower 2 and enters the flash tank 6, the temperature is reduced after steam is flashed, and then enters the lean-rich liquid heat exchanger 1, and the cooled lean liquid is sent to the absorption tower to continuously absorb CO 2 or SO 2. After the rich liquid from the absorption tower exchanges heat in the lean-rich liquid heat exchanger 1, the rich liquid enters the gas-liquid heat exchanger 8, enters the regenerated gas heater 8 from the top of the regeneration tower 2, and then enters the regeneration tower 2 for regeneration. The regenerated lean solution is used as power, a hydraulic injector 7 is adopted, the pressure of the flash tank 6 is reduced by 10-50 kPa, secondary steam is flashed out, and the secondary steam enters the lower part of the regeneration tower 2 for heating and regenerating the solution.
In this embodiment, the lean solution after a small portion of regeneration is used as power, the pressure of the flash tank 6 is reduced by 10-50 kPa by using the ejector 7, and the secondary steam is flashed out for solution heating regeneration.
In this example, the temperature of the lean solution entering the flash tank 6 is 105 to 120 ℃, and the temperature after flash evaporation is 85 to 105 ℃.
In this embodiment, the temperature of the rich liquid entering the gas-liquid heat exchanger 8 is 75 ℃ to 95 ℃, and after heat exchange with the acid gas at 95 ℃ to 118 ℃ coming out of the top end of the regeneration tower 2, the temperature is raised to 93 ℃ to 115 ℃ and enters the upper part of the regeneration tower 2.
In this example, the steam pressure as the motive power is 0.1 to 0.8MPa, and the pressure of the flash tank 6 is-0.04 to 0.01MPa.
Comparative example 1:
A nonferrous smelting plant is constructed with a set of 160000Nm 3/h desulfurization system, adopts a composite amine method SO 2 trapping technology, adopts a general (prior art) primary absorption-primary regeneration flow, and the regeneration flow is as follows:
As shown in fig. 1, the rich liquid at 42 ℃ after absorbing SO 2 enters the lean-rich liquid heat exchanger 10 from the bottom of the absorption tower through a pump, exchanges heat with the lean liquid at 115 ℃, and then rises to 90 ℃ and enters the upper part of the regeneration tower 20. The desorbed CO 2 and water vapor are cooled by a regenerated gas condenser 30 at about 105 ℃, and then separated to remove water, thus obtaining the product SO 2 gas with the purity of 99.5 percent for preparing acid. The bottom of the regenerator is supplied with heat by a steam reboiler 50. The steam consumption is 20t/h.
Inventive example 1:
After the flue gas desulfurization device of the nonferrous smelting plant runs for 1 year, the hydraulic jet regeneration energy-saving system adopting the organic amine solution is technically modified as follows:
As shown in fig. 2, the rich liquid at 42 ℃ after absorbing SO 2 enters a lean-rich liquid heat exchanger 1 from the bottom of the absorption tower through a pump, exchanges heat with the lean liquid at 95 ℃, then rises to 80 ℃, enters a gas-liquid heat exchanger 8, exchanges heat with SO 2 at about 105 ℃ and water vapor which are discharged from the top of a regeneration tower 2, rises to 100 ℃, and enters the upper part of the regeneration tower 2 for regeneration.
Lean liquid from the bottom of the regeneration tower 2 has a temperature of about 115 ℃, one part of the lean liquid is pressurized by a booster pump 9 and enters an ejector 7, the other part of the lean liquid enters a flash tank 6, the temperature of the lean liquid is reduced to 95 ℃ after the flash evaporation is pumped by the ejector 7, and the lean liquid enters the lean-rich liquid heat exchanger 1 for heat exchange. After transformation and casting, the total steam consumption is 14t/h.
According to the operation results of the table, the hydraulic jet regeneration energy-saving system provided by the utility model has the advantages that the solution regeneration heat consumption is reduced by about 30%, and the energy-saving and consumption-reducing effects are obvious.
Claims (1)
1. The hydraulic jet regeneration energy-saving system for the organic amine solution is characterized by comprising a lean-rich liquid heat exchanger (1), a regeneration tower (2), a regeneration gas condenser (3), a regeneration gas separator (4), a steam reboiler (5), a flash tank (6), a hydraulic ejector (7), a gas-liquid heat exchanger (8) and a booster pump (9), wherein the rich liquid output end of the lean-rich liquid heat exchanger (1) is communicated with the liquid inlet end of the gas-liquid heat exchanger (8), the liquid outlet end of the gas-liquid heat exchanger (8) is communicated with the liquid inlet end of the upper part of the regeneration tower (2), the gas outlet end of the top end of the regeneration tower (2) is communicated with the gas inlet end of the gas-liquid heat exchanger (8), the liquid outlet end of the bottom of the regeneration tower (2) is partially communicated with the inlet of the liquid booster pump, the other part of the liquid outlet end of the bottom of the regeneration tower (2) is communicated with the liquid inlet end of the upper part of the flash tank (6), the liquid outlet end of the lower part of the flash tank (6) is communicated with the liquid inlet end of the reboiler (5) of the rich liquid heat exchanger (1), the gas outlet end of the top of the regeneration tower (2) is connected with the power inlet end of the steam ejector (7) as the power inlet end of the regeneration tower (7), the output end of the ejector (7) is communicated with the mixed steam input end at the lower part of the regeneration tower (2).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321800263.1U CN221287430U (en) | 2023-07-10 | 2023-07-10 | Hydraulic jet regeneration energy-saving system for organic amine solution |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321800263.1U CN221287430U (en) | 2023-07-10 | 2023-07-10 | Hydraulic jet regeneration energy-saving system for organic amine solution |
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| CN221287430U true CN221287430U (en) | 2024-07-09 |
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| CN202321800263.1U Active CN221287430U (en) | 2023-07-10 | 2023-07-10 | Hydraulic jet regeneration energy-saving system for organic amine solution |
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| Country | Link |
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| CN (1) | CN221287430U (en) |
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2023
- 2023-07-10 CN CN202321800263.1U patent/CN221287430U/en active Active
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