CN112121632A - Process and device for recycling liquefied gas sweetening tail gas - Google Patents
Process and device for recycling liquefied gas sweetening tail gas Download PDFInfo
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- CN112121632A CN112121632A CN202011017741.2A CN202011017741A CN112121632A CN 112121632 A CN112121632 A CN 112121632A CN 202011017741 A CN202011017741 A CN 202011017741A CN 112121632 A CN112121632 A CN 112121632A
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- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000004064 recycling Methods 0.000 title claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 156
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 29
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 29
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 18
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 238000004880 explosion Methods 0.000 abstract description 9
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract description 8
- 239000012855 volatile organic compound Substances 0.000 abstract description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 7
- 239000003546 flue gas Substances 0.000 abstract description 7
- 150000003568 thioethers Chemical class 0.000 abstract description 6
- 238000006477 desulfuration reaction Methods 0.000 abstract description 4
- 230000023556 desulfurization Effects 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 2
- 238000011084 recovery Methods 0.000 abstract description 2
- 150000003467 sulfuric acid derivatives Chemical class 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000003502 gasoline Substances 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- CETBSQOFQKLHHZ-UHFFFAOYSA-N Diethyl disulfide Chemical compound CCSSCC CETBSQOFQKLHHZ-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 239000007832 Na2SO4 Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 2
- DNJIEGIFACGWOD-UHFFFAOYSA-N ethanethiol Chemical compound CCS DNJIEGIFACGWOD-UHFFFAOYSA-N 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- SUVIGLJNEAMWEG-UHFFFAOYSA-N propane-1-thiol Chemical compound CCCS SUVIGLJNEAMWEG-UHFFFAOYSA-N 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- NLOAOXIUYAGBGO-UHFFFAOYSA-N C.[O] Chemical compound C.[O] NLOAOXIUYAGBGO-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- KOYGZROXUOTUEE-UHFFFAOYSA-N butane;but-1-ene Chemical compound CCCC.CCC=C KOYGZROXUOTUEE-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- XLTBPTGNNLIKRW-UHFFFAOYSA-N methyldisulfanylethane Chemical compound CCSSC XLTBPTGNNLIKRW-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- JTXAHXNXKFGXIT-UHFFFAOYSA-N propane;prop-1-ene Chemical group CCC.CC=C JTXAHXNXKFGXIT-UHFFFAOYSA-N 0.000 description 1
- 239000011265 semifinished product Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 150000003573 thiols Chemical class 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—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
- B01D53/8678—Removing components of undefined structure
- B01D53/8687—Organic components
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/8603—Removing sulfur compounds
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention belongs to the technical field of VOC (volatile organic compound) treatment of petrochemical devices, and particularly relates to a process and a device for recycling liquefied gas sweetening tail gas. The tail gas containing hydrocarbons and sulfide is pressurized and explosion limit is controlled, and then is conveyed into a catalytic cracking regenerator, and the hydrocarbons and sulfide undergo high-temperature catalytic cracking reaction to produce CO2、SO2And SO3SO formed2、SO3And the flue gas enters a desulfurization device along with the flue gas to be desulfurized and then is discharged in an environment-friendly way. The invention can basically realize zero emission of the tail gas of mercaptan removal, reduce the emission of VOC, simultaneously fully utilize the existing matching device of an oil refinery, reduce the equipment investment and the operation energy consumption of other treatment modes,and moreover, the oxidation reaction of hydrocarbon organic matters in the tail gas is realized, the recovery of the heat value of hydrocarbons is realized, part of steam is generated as a byproduct, and meanwhile, sulfides can be converted into stable sulfates, so that the pollution of sulfide malodorous gas to the environment is avoided.
Description
Technical Field
The invention belongs to the technical field of VOC (volatile organic compound) treatment of petrochemical devices, and particularly relates to a process and a device for recycling liquefied gas sweetening tail gas.
Background
The petroleum refinery in petrochemical industry produces liquefied gas, gasoline, diesel oil and other products. The products are easy to volatilize, Volatile Organic Compounds (VOC) are formed and diffused into the atmosphere to cause pollution, and particularly, the products and semi-finished products contain hydrogen sulfide, methyl mercaptan, ethanethiol, dimethyl disulfide, diethyl disulfide, methyl ethyl disulfide, propanethiol, methyl sulfide, carbonyl sulfide and the like, and also cause sulfur pollution to the atmosphere.
At present, the liquefied gas and the gasoline are generally subjected to mercaptan removal by adopting a mercaptan removal device, and tail gas in the mercaptan removal device of the liquefied gas and the gasoline contains hydrocarbons, mercaptan and sulfide, has pungent odor and is toxic. At present, common treatment measures are that the waste gas is discharged at a high point on the spot or is led to a chimney to be diluted and then discharged, the problem of environmental protection discharge is not solved essentially, and tail gas discharged at high altitude is easily ignited when the waste gas is discharged in the thunderstorm weather in summer, so that a fire disaster is caused. The main components of the tail gas are air, a small amount of hydrocarbons and sulfides, and a special device and a new technology adopting an adsorbent adsorption or condensation method are also provided at present, but the device has huge investment and high energy consumption, and simultaneously forms new hazardous wastes such as the adsorbent.
Therefore, how to solve the problem of tail gas emission of the existing liquefied gas and gasoline sweetening, eliminate environmental pollution and potential safety hazard caused by tail gas emission, effectively utilize hydrocarbons in tail gas, reduce the tail gas treatment cost and energy consumption of the device and become important technical problems to be solved by professionals in the field.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the process and the device for recycling the tail gas generated by removing the mercaptan from the liquefied gas can realize zero emission of the tail gas and effectively utilize hydrocarbons in the tail gas.
The invention is realized by adopting the following technical scheme:
the liquefied gas sweetening tail gas recycling process comprises the following steps:
(1) introducing purified air into the exhausted liquefied gas sweetening tail gas to dilute the tail gas;
(2) pressurizing the tail gas diluted by purified air, and performing high-temperature catalytic cracking reaction to generate CO2、SO2And SO3；
(3) Adding SO2And SO3Reacts with alkali to generate sulfate.
The flow rate of the liquefied gas sweetening tail gas discharged in the step (1) is 14-16Nm3And h, the concentration of the liquefied gas in the tail gas is 2-10%.
The air quantity ratio of the purified air to the exhausted liquefied gas sweetening tail gas in the step (1) is 5-10: 1.
And (3) the concentration of the liquefied gas in the tail gas diluted by the purified air in the step (2) is less than 1.5 v%. The explosion limit of liquefied gas is 1.5-9.5 v%, and in order to attain the goal of safe transportation, the tail gas pipeline is injected with purified air, and the tail gas is diluted by purified air, so that the concentration of liquefied gas in the tail gas is lower than the lower explosion limit, and can be safely transported.
And (3) pressurizing the tail gas diluted by the purified air in the step (2) to 0.3-0.5 MPa.
The high-temperature catalytic cracking reaction in the step (2) is carried out under the oxygen-containing condition of 600-800 ℃, hydrocarbons and sulfides in the tail gas are oxidized at high temperature and then enter the subsequent original desulfurization unit along with the flue gas for further treatment.
The device used in the liquefied gas sweetening tail gas recycling process comprises a sweetening device, wherein the top of the sweetening device is connected with a catalytic cracking regenerator through a tail gas pipeline, the top of the catalytic cracking regenerator is connected with a desulphurization device, a tail gas compressor is arranged on the tail gas pipeline, the tail gas pipeline in front of the inlet of the tail gas compressor is connected with a purified air pipeline, an air volume adjusting valve is arranged on the purified air pipeline, a hydrocarbon analyzer is arranged at the outlet of the tail gas compressor, and the concentration of diluted tail gas is detected on line.
Preferably, in order to ensure the safety of the tail gas conveying system, the pipeline of the tail gas conveying system adopts a stainless steel pipeline, so that the generation of conveying static electricity is reduced.
Preferably, a gas-liquid separator, a flame arrester and an exhaust pressure gauge are arranged on a tail gas pipeline at an exhaust port at the top of the mercaptan removal device, the gas-liquid separator can recover condensed hydrocarbon substances, and the flame arrester can prevent impact waves caused by pipeline explosion from influencing the mercaptan removal device.
Preferably, the air volume regulating valve, the tail gas compressor and the hydrocarbon analyzer are electrically connected with the control system, and the air volume regulating valve air volume ratio interlock and the hydrocarbon analyzer high-limit shutdown interlock are arranged on the tail gas compressor through the control system, so that liquefied gas in the tail gas is always within the explosion lower limit.
Preferably, the outlet of the tail gas compressor is provided with a pressurization pressure gauge.
The liquefied gas or gasoline sweetening tail gas mainly contains air, hydrocarbons and sulfides, wherein the hydrocarbons and sulfides can be decomposed into CO in the presence of high-temperature air2、SO2、SO3. A catalytic cracking unit is commonly arranged in an oil refinery, in a regenerator of the catalytic cracking unit, a large amount of external air with the temperature of about 220 ℃ and spent catalyst are subjected to oxidation and coking reaction at the high temperature of about 700 ℃, and the main reaction is CnHx+O2＝CO2+H2O、S+O2＝SO2+SO3. The flue gas formed after the high-temperature reaction of air and catalyst in the regenerator of the catalytic cracking device is finally removed from the desulfurization and denitrification device to remove SO2、SO3The post-environmental protection is discharged, and the main reaction is NaOH + SO3＝Na2SO4+H2O。
The invention conveys the tail gas containing hydrocarbon and sulfide to a catalytic cracking regenerator by pressurizing and controlling the explosion limit, and the hydrocarbon and sulfide undergo high-temperature oxidation reaction, wherein the main reaction is CnHx+CS2+ RSH (thiol) + H2S+O2＝CO2+S O2+SO3. Generated SO2、SO3The flue gas enters a desulfurizing device along with the flue gas to be desulfurized and then is discharged in an environment-friendly way, and SO is discharged2And SO3Reacts with alkali to generate sulfate.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention can basically realize zero emission of the tail gas of mercaptan removal, simultaneously fully utilizes the existing matching device of an oil refinery, reduces equipment investment and operation energy consumption of other treatment modes, realizes the oxidation reaction of hydrocarbon organic matters in the tail gas, realizes the recovery of hydrocarbon heat value and produces partial steam as a byproduct.
2. The invention can recover 8605.8Nm of liquefied gas all the year round3The emission of VOC is reduced by about 384kg of liquefied gas, and meanwhile, sulfide can be converted into stable sulfate, so that the pollution of sulfide malodorous gas to the environment is avoided.
Drawings
FIG. 1 is a schematic view of an apparatus of the present invention;
in the figure: 1. a mercaptan removal device; 2. a gas-liquid separator; 3. an exhaust gas pipeline; 4. a flame arrestor; 5. an exhaust pressure gauge; 6. purifying the air pipeline; 7. an air volume adjusting valve; 8. a tail gas compressor; 9. a hydrocarbon analyzer; 10. a pressure-increasing pressure gauge; 11. a catalytic cracking regenerator; 12. a desulfurization device.
Detailed Description
The invention is further described below with reference to the accompanying drawings and examples.
Example 1
As shown in fig. 1, liquefied gas sweetening tail gas recycle device, including sweetening device 1, sweetening device 1 top is connected with catalytic cracking regenerator 11 through tail gas pipeline 3, catalytic cracking regenerator 11 top is connected with desulphurization unit 12, be equipped with tail gas compressor 8 on the tail gas pipeline 3, tail gas pipeline 3 of the front portion of tail gas compressor 8 entry is connected with purification wind pipeline 6, be equipped with air regulation valve 7 on the purification wind pipeline 6, the tail gas compressor 8 export is equipped with the tail gas concentration after two hydrocarbon analyzer 9 on-line measuring dilutions.
A tail gas pipeline 3 at an exhaust port at the top of the mercaptan removal device 1 is provided with a gas-liquid separator 2, a flame arrester 4 and an exhaust pressure gauge 5.
The air volume regulating valve 7, the tail gas compressor 8 and the hydrocarbon analyzer 9 are electrically connected with the control system.
A pressure-increasing pressure gauge 10 is arranged at the outlet of the tail gas compressor 8.
The tail gas after the mercaptan removal of the mercaptan removal device 1 is discharged to a gas-liquid separator 2, the tail gas is cooled to recover condensed hydrocarbon substances, and the condensed and recovered tail gas comprises the following components:
| components | Hydrogen gas | Methane | Oxygen gas | Nitrogen gas | Ethane (III) | Propane | Propylene (PA) | Butane | Butene (butylene) | Carbon five |
| Content (v%) | 0.19 | 0 | 9.88 | 83.1 | 0.1 | 1.54 | 3.49 | 1.01 | 0.62 | 0.07 |
The explosion limit of the liquefied gas is 1.5-9.5 v%, and the tail gas flow is 15Nm3H, the concentration of liquefied gas in tail gas components is 6.83 v%, in the explosion limit range, purified air is introduced into the tail gas through a purified air pipeline 6, purified air with the flow of 6 times of tail gas is injected into a tail gas pipeline 3 through an air volume adjusting valve 7, the concentration of the liquefied gas after dilution is 0.76 v%, the liquefied gas is lower than the explosion lower limit and can be safely conveyed, the discharged 0.26MPa tail gas is diluted by the purified air and then is safely conveyed to a tail gas compressor 8, the tail gas is compressed to 0.35MPa through the tail gas compressor 8, two hydrocarbon analyzers 9 are arranged at the outlet of the tail gas compressor 8, the concentration of the diluted tail gas is detected on line, the pressurized tail gas enters a catalytic cracking regenerator 11, and under the condition of high temperature oxygen containing at 680 ℃, hydrocarbons and sulfides in the tail gas are oxidized at high temperature to generate CO2、SO2And SO3Then enters the subsequent original desulphurization device 12 along with the flue gas for further treatment, and SO is treated2And SO3Reaction with NaOH to produce Na2SO4And the tail gas reaching the standard is discharged in an environment-friendly way. The concentration of liquefied gas hydrocarbons in the final tail gas is less than 60 ppm.
Example 2
The same apparatus and process as in example 1 were used, except that: the concentration of liquefied gas in the tail gas components is 9.24 v%, purified air which is 9 times of the tail gas flow is injected into the tail gas pipeline 3 through the adjustment of the air quantity regulating valve 7, and finally the concentration of liquefied gas hydrocarbons in the tail gas is less than 80 ppm.
Of course, the foregoing is only a preferred embodiment of the invention and should not be taken as limiting the scope of the embodiments of the invention. The present invention is not limited to the above examples, and equivalent changes and modifications made by those skilled in the art within the spirit and scope of the present invention should be construed as being included in the scope of the present invention.
Claims (10)
1. A liquefied gas sweetening tail gas recycling process is characterized in that: the method comprises the following steps:
(1) introducing purified air into the exhausted liquefied gas sweetening tail gas to dilute the tail gas;
(2) pressurizing the tail gas diluted by purified air, and performing high-temperature catalytic cracking reaction to generate CO2、SO2And SO3；
(3) Adding SO2And SO3Reacts with alkali to generate sulfate.
2. The recycling process of liquefied gas sweetening tail gas according to claim 1, characterized in that: the flow rate of the liquefied gas sweetening tail gas discharged in the step (1) is 14-16Nm3And h, the concentration of the liquefied gas in the tail gas is 2-10%.
3. The liquefied gas sweetening tail gas recycling process according to claim 1 or 2, characterized in that: the air quantity ratio of the purified air to the exhausted liquefied gas sweetening tail gas in the step (1) is 5-10: 1.
4. The recycling process of liquefied gas sweetening tail gas according to claim 1, characterized in that: and (3) the concentration of the liquefied gas in the tail gas diluted by the purified air in the step (2) is less than 1.5 v%.
5. The recycling process of liquefied gas sweetening tail gas according to claim 1, characterized in that: and (3) pressurizing the tail gas diluted by the purified air in the step (2) to 0.3-0.5 MPa.
6. The recycling process of liquefied gas sweetening tail gas according to claim 1, characterized in that: the high-temperature catalytic cracking reaction in the step (2) is carried out under the oxygen-containing condition of 600-800 ℃.
7. A device used in the process for recycling the liquefied gas sweetening tail gas of any one of claims 1 to 6 is characterized in that: including sweetening device (1), sweetening device (1) top is connected with catalytic cracking regenerator (11) through tail gas pipeline (3), catalytic cracking regenerator (11) top is connected with desulphurization unit (12), be equipped with tail gas compressor (8) on tail gas pipeline (3), tail gas compressor (8) entry anterior tail gas pipeline (3) are connected with purification wind pipeline (6), be equipped with air regulation valve (7) on purification wind pipeline (6), tail gas compressor (8) export is equipped with hydrocarbon analyzer (9).
8. The device used in the process for recycling the tail gas generated in the mercaptan removal of liquefied gas according to claim 7 is characterized in that: a tail gas pipeline (3) at the exhaust port at the top of the mercaptan removal device (1) is provided with a gas-liquid separator (2), a flame arrester (4) and an exhaust pressure gauge (5).
9. The device used in the process for recycling the tail gas generated in the mercaptan removal of liquefied gas according to claim 7 is characterized in that: the air volume regulating valve (7), the tail gas compressor (8) and the hydrocarbon analyzer (9) are electrically connected with the control system.
10. The device used in the process for recycling the tail gas generated in the mercaptan removal of liquefied gas according to claim 7 is characterized in that: a pressure-increasing pressure gauge (10) is arranged at the outlet of the tail gas compressor (8).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114874805A (en) * | 2022-05-26 | 2022-08-09 | 大庆中蓝石化有限公司 | Tail gas emission and recovery system of gasoline sweetening production device |
Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114874805B (en) * | 2022-05-26 | 2023-12-05 | 大庆中蓝石化有限公司 | Tail gas emission recovery system of gasoline sweetening production device |
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