CN116550121A - Tail gas purifying treatment method for propane dehydrogenation device - Google Patents
Tail gas purifying treatment method for propane dehydrogenation device Download PDFInfo
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- CN116550121A CN116550121A CN202211367503.3A CN202211367503A CN116550121A CN 116550121 A CN116550121 A CN 116550121A CN 202211367503 A CN202211367503 A CN 202211367503A CN 116550121 A CN116550121 A CN 116550121A
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- flue gas
- temperature
- heat
- propane dehydrogenation
- tail gas
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- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 36
- 239000001294 propane Substances 0.000 title claims abstract description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 79
- 239000003546 flue gas Substances 0.000 claims abstract description 79
- 239000007789 gas Substances 0.000 claims abstract description 40
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 33
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- 238000001816 cooling Methods 0.000 claims abstract description 12
- 238000010438 heat treatment Methods 0.000 claims abstract description 8
- -1 methane hydrocarbons Chemical class 0.000 claims abstract description 6
- 229930195733 hydrocarbon Natural products 0.000 claims abstract 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 229910021529 ammonia Inorganic materials 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 6
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 2
- 230000003197 catalytic effect Effects 0.000 claims description 2
- 238000011143 downstream manufacturing Methods 0.000 claims description 2
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 claims description 2
- 150000002894 organic compounds Chemical class 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052717 sulfur Inorganic materials 0.000 abstract description 9
- 239000011593 sulfur Substances 0.000 abstract description 9
- 238000004134 energy conservation Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000011084 recovery Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- CQEYYJKEWSMYFG-UHFFFAOYSA-N butyl acrylate Chemical compound CCCCOC(=O)C=C CQEYYJKEWSMYFG-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/90—Injecting reactants
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a tail gas purifying treatment method of a propane dehydrogenation device, wherein high-temperature regenerated flue gas of the propane dehydrogenation device passes through a non-methane reactor to remove non-methane hydrocarbons in the tail gas; then the high-temperature regenerated flue gas enters a superheater to recover part of energy; the high-temperature regenerated flue gas after part of energy is recovered enters an air heater to further recover heat; then the regenerated flue gas enters an SCR reactor to remove nitrogen oxides in the tail gas; the purified flue gas meeting the emission requirements enters a flue gas cooling unit, and the heat of the purified flue gas is further recovered. The invention adopts the low-temperature sulfur-resistant SCR catalyst, the SCR reactor is arranged at the tail end of the process flow, and a single air heater is arranged for heating fresh air, so that the process flow is simplified; and the flue gas cooling unit is used for further recovering the heat of the purified flue gas, so that the heat energy is used for heat energy utilization equipment of a process device, the steam consumption is reduced, or the heat energy is used for producing steam and is sent to a steam pipe network, the energy utilization rate of the purified flue gas is greatly improved, and the purposes of energy conservation and consumption reduction are achieved.
Description
Technical Field
The invention belongs to the technical field of environmental protection energy, and particularly relates to a tail gas purifying treatment method of a propane dehydrogenation device.
Background
Propylene is an important industrial raw material, and the demand of propylene is continuously increasing along with the development of industries such as chemical industry and the like. With the development of propylene production technology and the extension of production facilities, the yield of propylene increases. In recent years, a propane dehydrogenation process with high market share has the advantages of low investment, high product yield, low production cost and the like, and has become a propylene synthesis process which is paid attention to at present.
In the existing tail gas treatment technology of propane dehydrogenation process devices, pressurized fresh air is preheated in two stages and then is sent to a heating furnace, and regenerated flue gas after heating and regeneration is directly discharged into the atmosphere after SCR and heat recovery.
In the existing propane dehydrogenation tail gas treatment technology, because the tail gas contains a small amount of sulfur, in order to avoid the blocking of an SCR catalyst pore path by ammonium bisulfate, an SCR reactor is arranged between two air heaters, and the temperature of the SCR inlet reactor is 300-320 ℃. The emission temperature of the purified flue gas is 120-140 ℃, and a large amount of recoverable energy exists in the purified flue gas. Therefore, the existing tail gas treatment system has the defects of complex flow, high operation difficulty, low energy utilization rate and the like.
In addition, a large amount of steam is needed in the production process of acrylic acid, acrylonitrile, butyl acrylate and other devices downstream of the propane dehydrogenation process and is used for heat energy utilization equipment, and part of the steam needs high-pressure or medium-pressure steam for being sent to the heat energy utilization equipment after being depressurized; when the steam is insufficient, outsourcing steam is needed to meet production requirements, so that energy waste is caused, and the running cost is increased. Along with the increasing national requirements on energy conservation, consumption reduction and carbon emission, the low-grade heat of the recovered flue gas is of great significance for heat energy utilization equipment of the whole plant.
Disclosure of Invention
Aiming at the problems of complex flow, high operation difficulty and insufficient heat recovery in the existing tail gas treatment system of the propane dehydrogenation device, according to the embodiment of the invention, the tail gas purification treatment method of the propane dehydrogenation device is hoped to be provided, a low-temperature sulfur-resistant SCR catalyst is adopted, an SCR reactor is arranged at the tail end of the process flow, a single air heater is adopted for heating fresh air, the process flow is simplified, the operation is flexible, the equipment investment is saved, the heat of purified flue gas is further recovered by adopting a flue gas cooling unit, the energy utilization rate of the purified flue gas is greatly improved, and the purposes of energy conservation and consumption reduction are achieved.
According to the embodiment, according to the tail gas purification treatment method for the propane dehydrogenation device, the high-temperature regenerated flue gas of the propane dehydrogenation device passes through the non-methane reactor to remove non-methane alkane in the tail gas; then the high-temperature regenerated flue gas enters a superheater to recover part of energy; the high-temperature regenerated flue gas after part of energy is recovered enters an air heater to further recover heat; then the regenerated flue gas enters an SCR reactor to remove nitrogen oxides in the tail gas; the purified flue gas meeting the emission requirements enters a flue gas cooling unit, and the heat of the purified flue gas is further recovered, wherein:
the flue gas cooling unit comprises a cooler, a compressor and a pressure reducing valve which are sequentially connected, wherein the low-temperature heat conduction working medium recovers heat in the cooler, the high-temperature heat conduction working medium obtained after passing through the compressor is sent to heat energy utilization equipment of a downstream process device, and the low-temperature heat conduction working medium is decompressed into low-temperature heat conduction working medium for recycling after being liquefied by the pressure reducing valve.
According to one embodiment, in the method for purifying the tail gas of the propane dehydrogenation device, the non-methyl reactor is provided with a VOC catalyst reaction bed layer, and the catalytic oxidation reaction is carried out on the catalyst reaction bed layer to remove harmful substances such as non-methyl alkane and the like in the flue gas.
According to one embodiment, in the method for purifying and treating the tail gas of the propane dehydrogenation device, the air heater is used for heating fresh air, the temperature of high-temperature flue gas is reduced from 540-570 ℃ to 100-300 ℃, and regenerated air is preheated from 60-110 ℃ to 400-540 ℃.
According to one embodiment, in the aforementioned method for purifying the tail gas of a propane dehydrogenation unit according to the present invention, the air heater is preferably selected from a tubular heat exchanger or a plate heat exchanger.
According to one embodiment, in the method for purifying and treating the tail gas of the propane dehydrogenation device, the SCR reactor is provided with a low-temperature sulfur-resistant SCR catalyst reaction bed layer, and the flue gas and the ammonia source perform catalytic reduction reaction on the catalytic reaction bed layer to remove nitrogen oxides in the flue gas.
According to one embodiment, in the aforementioned method for purifying the tail gas of a propane dehydrogenation unit, the inlet flue gas temperature of the SCR reactor is preferably 100-300 ℃, more preferably 130-240 ℃.
According to one embodiment, in the method for purifying and treating the tail gas of the propane dehydrogenation device, the heat-conducting working medium is an organic compound with an atmospheric boiling point lower than 100 ℃ and stable properties.
According to one embodiment, in the aforementioned method for purifying the tail gas of a propane dehydrogenation unit according to the present invention, the compressor outlet pressure is preferably 200 to 3000kpa g, more preferably 500 to 2500kpa g.
According to one embodiment, in the method for purifying and treating the tail gas of the propane dehydrogenation device, the temperature of the low-temperature heat-conducting working medium at the outlet of the pressure reducing valve is preferably less than 100 ℃, and more preferably 0-85 ℃.
Compared with the prior art, the invention has the beneficial effects that: the adoption of the low-temperature sulfur-resistant SCR catalyst can avoid SO from being generated on the catalyst by sulfide 3 Thereby avoiding blocking catalyst pore channels by ammonium bisulfate generated by reaction with ammonia, arranging an SCR reactor after an air heater, and setting a single air heaterThe device is used for heating fresh air, simplifies the process flow, is flexible to operate and saves equipment investment; the flue gas cooling unit is adopted to further recycle the heat of the purified flue gas, so that the energy utilization rate of the purified flue gas is greatly improved, and the method has good economic and social benefits.
Drawings
FIG. 1 is a process flow diagram of a method for purifying the tail gas of a propane dehydrogenation unit according to the present invention.
Wherein: 1-non-A reactor, 2-superheater, 3-air heater, 4-SCR reactor, 5-cooler, 6-compressor, 7-pressure reducing valve.
Detailed Description
The invention is further illustrated in the following, in conjunction with the accompanying drawings and detailed embodiments. These examples should be construed as merely illustrative of the present invention and not limiting the scope of the present invention. Various changes and modifications to the present invention may be made by one skilled in the art after reading the description herein, and such equivalent changes and modifications are intended to fall within the scope of the present invention as defined in the appended claims.
Example 1
As shown in fig. 1, the high-temperature regenerated flue gas of the propane dehydrogenation device passes through a non-methane reactor to remove non-methane alkane in the tail gas; then the high-temperature regenerated flue gas enters a superheater to recover part of energy; the high-temperature flue gas enters an air heater to heat fresh air, the air heater adopts a plate heat exchanger, the temperature of the high-temperature flue gas is reduced from 555-565 ℃ to 130-140 ℃, and the regenerated air is preheated from 90 ℃ to 525-535 ℃; and then, the 130-140 ℃ regenerated flue gas enters an SCR reactor to remove nitrogen oxides in the tail gas, the SCR reactor is provided with a low-temperature sulfur-resistant SCR catalyst reaction bed layer, and the flue gas and an ammonia source perform catalytic reduction reaction on the catalytic reaction bed layer to remove the nitrogen oxides in the flue gas. The purified flue gas with the temperature of 130-140 ℃ enters a cooler to further recover heat, the low-temperature heat-conducting working medium with the temperature of 75 ℃ is gasified after recovering heat in the cooler, the pressure of the high-temperature heat-conducting working medium obtained after entering a compressor is 1210KpaG, the temperature is 133 ℃, and the low-temperature heat-conducting working medium with the temperature of 75 ℃ is recycled after being liquefied by a steam device in a pressure reducing valve. The temperature of the flue gas after heat recovery by the flue gas cooling unit is 90 ℃.
Example 2
Removing non-methane in tail gas from the high-temperature regenerated flue gas of the propane dehydrogenation device through a non-methane reactor; then the high-temperature regenerated flue gas enters a superheater to recover part of energy; the high-temperature flue gas enters an air heater to heat fresh air, the air heater adopts a plate heat exchanger, the temperature of the high-temperature flue gas is reduced from 555-565 ℃ to 210-220 ℃, and the regenerated air is preheated from 90 ℃ to 450-460 ℃; and then, the regenerated flue gas at 210-220 ℃ enters an SCR reactor to remove nitrogen oxides in the tail gas, the SCR reactor is provided with a low-temperature sulfur-resistant SCR catalyst reaction bed layer, and the flue gas and an ammonia source perform catalytic reduction reaction on the catalytic reaction bed layer to remove the nitrogen oxides in the flue gas. The purified flue gas at 210-220 ℃ enters a cooler to further recover heat, the low-temperature heat-conducting working medium at 75 ℃ is gasified after recovering heat in the cooler, the pressure of the high-temperature heat-conducting working medium obtained after entering a compressor is 1210KpaG, the temperature is 133 ℃, and the low-temperature heat-conducting working medium with the pressure reduced to 75 ℃ in a pressure reducing valve is recycled after being liquefied by a steam device. The temperature of the flue gas after heat recovery by the flue gas cooling unit is 90 ℃.
Example 3
Removing non-methane in tail gas from the high-temperature regenerated flue gas of the propane dehydrogenation device through a non-methane reactor; then the high-temperature regenerated flue gas enters a superheater to recover part of energy; the high-temperature flue gas enters an air heater to heat fresh air, the air heater adopts a plate heat exchanger, the temperature of the high-temperature flue gas is reduced from 555-565 ℃ to 210-220 ℃, and the regenerated air is preheated from 90 ℃ to 450-460 ℃; and then, the regenerated flue gas at 210-220 ℃ enters an SCR reactor to remove nitrogen oxides in the tail gas, the SCR reactor is provided with a low-temperature sulfur-resistant SCR catalyst reaction bed layer, and the flue gas and an ammonia source perform catalytic reduction reaction on the catalytic reaction bed layer to remove the nitrogen oxides in the flue gas. The purified flue gas at 210-220 ℃ enters a cooler to further recover heat, the low-temperature heat-conducting working medium at 55 ℃ is gasified after recovering heat in the cooler, the pressure of the high-temperature heat-conducting working medium obtained after entering a compressor is 2200KpaG, the temperature is 132 ℃, and the low-temperature heat-conducting working medium with the pressure reduced to 55 ℃ in a pressure reducing valve is recycled after being liquefied by a steam device. The temperature of the flue gas after heat recovery by the flue gas cooling unit is 70 ℃.
Taking a propane dehydrogenation device with the scale of 90 ten thousand tons/year as an example, a low-temperature sulfur-resistant SCR catalyst is adopted, an SCR reactor is arranged behind an air heater, a single air heater is arranged for heating fresh air, and the total heat exchange area of the air heater can be reduced by more than 16.5 percent.
The flue gas compositions at the inlet and outlet of the SCR reactor in examples 1-3 are shown in Table 1. A large amount of heat and byproduct equivalent low pressure steam can be recovered through the flue gas cooling unit, and the heat data and byproduct equivalent low pressure steam recovered in each example are shown in table 2.
Table 1: SCR reactor inlet and outlet flue gas composition
Table 2: heat recovery data
| Examples | Recovering heat | By-product equivalent low pressure steam |
| Example 1 | 25.9MW | 42.8t/h |
| Example 2 | 70.7MW | 116.9t/h |
| Example 3 | 93.5MW | 154.6t/h |
Claims (9)
1. A method for purifying and treating tail gas of a propane dehydrogenation device is characterized in that high-temperature regenerated flue gas of the propane dehydrogenation device passes through a non-methane reactor to remove non-methane hydrocarbons in the tail gas; then the high-temperature regenerated flue gas enters a superheater to recover part of energy; the high-temperature regenerated flue gas after part of energy is recovered enters an air heater to further recover heat; then the regenerated flue gas enters an SCR reactor to remove nitrogen oxides in the tail gas; the purified flue gas meeting the emission requirements enters a flue gas cooling unit, and the heat of the purified flue gas is further recovered, wherein:
the flue gas cooling unit comprises a cooler, a compressor and a pressure reducing valve which are sequentially connected, wherein the low-temperature heat conduction working medium recovers heat in the cooler, the high-temperature heat conduction working medium obtained after passing through the compressor is sent to heat energy utilization equipment of a downstream process device, and the low-temperature heat conduction working medium is decompressed into low-temperature heat conduction working medium for recycling after being liquefied by the pressure reducing valve.
2. The method for purifying tail gas of propane dehydrogenation unit according to claim 1, wherein the non-methyl reactor is provided with a VOC catalyst reaction bed layer, and the catalytic oxidation reaction is performed on the catalytic reaction bed layer to remove harmful substances such as non-methyl alkane in the flue gas.
3. The method for purifying tail gas of a propane dehydrogenation unit according to claim 1, wherein the air heater is used for heating fresh air, the temperature of high-temperature flue gas is reduced from 540-570 ℃ to 100-300 ℃, and regenerated air is preheated from 60-110 ℃ to 400-540 ℃.
4. The method for purifying an exhaust gas of a propane dehydrogenation unit according to claim 3, wherein the air heater is selected from a tubular heat exchanger and a plate heat exchanger.
5. The method for purifying tail gas of propane dehydrogenation unit according to claim 1, wherein the SCR reactor is provided with a low-temperature sulfur-tolerant SCR catalyst reaction bed layer, and the flue gas and the ammonia source undergo catalytic reduction reaction on the catalytic reaction bed layer to remove nitrogen oxides in the flue gas.
6. The method for purifying tail gas of propane dehydrogenation unit according to claim 5, wherein the temperature of flue gas at the inlet of the SCR reactor is 100-300 ℃.
7. The method for purifying tail gas of propane dehydrogenation unit according to claim 1, wherein the heat conducting working medium is an organic compound with an atmospheric boiling point lower than 100 ℃ and stable properties.
8. The method for purifying tail gas of propane dehydrogenation unit according to claim 1, wherein the outlet pressure of the compressor is 200 to 3000kpa g.
9. The method for purifying tail gas of propane dehydrogenation unit according to claim 1, wherein the temperature of the low-temperature heat conducting working medium at the outlet of the pressure reducing valve is less than 100 ℃.
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| CN2022111076776 | 2022-09-13 | ||
| CN202211107677 | 2022-09-13 |
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