CN113117520A - Device and method for processing VOCs - Google Patents
Device and method for processing VOCs Download PDFInfo
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- CN113117520A CN113117520A CN201911411021.1A CN201911411021A CN113117520A CN 113117520 A CN113117520 A CN 113117520A CN 201911411021 A CN201911411021 A CN 201911411021A CN 113117520 A CN113117520 A CN 113117520A
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- gas
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- riser reactor
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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
- B01D53/88—Handling or mounting catalysts
- B01D53/885—Devices in general for catalytic purification of waste gases
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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
- B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
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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
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
Abstract
The present disclosure relates to a device and a method for processing VOCs, the method comprising: and (3) pressurizing the VOCs gas, then sending the pressurized VOCs gas into a catalytic cracking riser reactor, and feeding the gas obtained by reaction into a separation and purification system of a catalytic cracking device along with catalytic cracking reaction oil gas. The method for recycling VOCs gas simply and efficiently by using the existing catalytic cracking unit riser reactor and the product separation and purification system thereof in the refinery adopts a reaction recycling method, does not need to additionally arrange a VOCs gas treatment device, and avoids the defects of high investment, heat waste, serious secondary pollution and the like of the traditional combustion method; the method can effectively remove impurities such as sulfur, nitrogen and the like in the VOCs gas, and can reduce the pre-lifting steam consumption of the riser reactor of the catalytic cracking device, thereby reducing the cooling water consumption of a fractionating tower in the oil-gas fractionation process and the discharged ammonia-containing sewage quantity of the device, and reducing the energy consumption and the operation cost of the device.
Description
Technical Field
The disclosure relates to the field of VOCs treatment in the petrochemical industry, in particular to a device and a method for treating VOCs.
Background
Since the Stockholm meeting of human environment in 1972, people are concerned about environmental problems, and environmental protection are important issues for scientific research in the present day.
With the rapid development of industry and the acceleration of urbanization process, the air quality in the world is generally seriously threatened. In the whole air pollutant system, except particulate pollutants such as smoke dust, fog, total suspended particles and the like, gaseous pollutants account for an important part and account for more than 75 percent of the pollutants of the atmosphere exhausted every year all over the world, wherein the pollutants are more in quantity and are sequentially CO and SO2NOx and hydrocarbons. The pollutants are divided into inorganic pollutants and organic pollutants, wherein the organic pollutants account for the majority. In the list of 25 toxic gas emissions listed in the national Environmental Protection Agency (EPA), 18 are organic substances, and most organic waste gases contain low-concentration Volatile Organic Compounds (VOCs) such as benzene, toluene, styrene, polycyclic aromatic hydrocarbons, and the like.
Volatile Organic compounds (vocs) are an important class of air pollutants, and generally refer to Organic compounds having a boiling point of 50-260 ℃ and a saturated vapor pressure of more than 133.32Pa at room temperature, and the main components of the volatile Organic compounds are hydrocarbons, halogenated hydrocarbons, nitrogen hydrocarbons, oxygen-containing hydrocarbons, sulfur hydrocarbons, low-boiling polycyclic aromatic hydrocarbons and the like. The wide application of chemical products such as paint, coating, lubricating oil and the like in surface coatings, the incineration of industrial wastes, the emission of motor vehicle exhaust, the wide application of novel building materials, heat insulation materials and interior decoration materials, and the application of cosmetics, deodorants, insecticides, herbicides and various detergents simultaneously causes a large amount of VOCs to be discharged into the atmosphere. VOCs have complex components, special odor which can cause various maladaptions to human bodies and have toxic, irritant and carcinogenic effects, and particularly benzene, toluene and formaldehyde can cause great harm to human health.
Disclosure of Invention
The device and the method can overcome the defects of high investment, heat waste, secondary pollution and the like of the traditional combustion method, recover useful hydrocarbon substances in VOCs gas, remove impurities such as sulfur, nitrogen and the like of the VOCs, reduce the pre-lifting steam consumption in a riser reactor of a catalytic cracking device, save energy and reduce consumption.
To achieve the above object, a first aspect of the present disclosure provides a method for processing VOCs, the method comprising:
and (3) pressurizing the VOCs gas, then sending the pressurized VOCs gas into a catalytic cracking riser reactor, and feeding the gas obtained by reaction into a separation and purification system of a catalytic cracking device along with catalytic cracking reaction oil gas.
Optionally, the pressure of the pressurized VOCs gas is 0.3mpa (g) or more.
Optionally, the pressurization mode is one or more of power medium pressurization, compressor pressurization and gas supercharger pressurization; the power medium is one or more of water vapor, dry gas, gas and fuel gas.
Optionally, the method further comprises: feeding said VOCs gas to a buffer tank prior to said pressurizing step; the pressure of the buffer tank is-0.1 to 0.3MPa (g).
Optionally, the catalytic cracking riser reactor comprises a pre-lift section, the pre-lift section is provided with a pre-lift nozzle, and the pressurized VOCs gas is injected into the pre-lift section through the pre-lift nozzle; in the pre-lifting section, the mass flow ratio of the pressurized VOCs gas to the water vapor is 1: (0.1-100).
To achieve the above object, a second aspect of the present disclosure provides an apparatus for treating VOCs, the apparatus comprising an inlet for VOCs and a gas pressurization device in communication with each other, the outlet of the gas pressurization device being adapted to communicate with a catalytic cracking riser reactor.
Optionally, a VOCs buffer tank is further arranged between the VOCs inlet and the supercharging device.
Optionally, the pressure boosting device is one or more of a booster ejector, a compressor and a gas booster.
Optionally, the apparatus further comprises a catalytic cracking riser reactor and a separation purification system of the catalytic cracking apparatus, wherein the outlet of the gas pressurization device is communicated with the inlet of the catalytic cracking riser reactor.
Optionally, the riser of the catalytic cracking riser reactor comprises a pre-lifting section, the bottom of the pre-lifting section is provided with a pre-lifting nozzle extending into the pre-lifting section, and the inlet of the pre-lifting nozzle is communicated with the outlet of the gas pressurization device.
The method for recycling VOCs gas simply and efficiently by using the existing catalytic cracking unit riser reactor and the product separation and purification system thereof in the refinery adopts a reaction recycling method, does not need to additionally arrange a VOCs gas treatment device, and avoids the defects of high investment, heat waste, serious secondary pollution and the like of the traditional combustion method; the method can effectively remove impurities such as sulfur, nitrogen and the like in the VOCs gas, and can reduce the pre-lifting steam consumption of the riser reactor of the catalytic cracking device, thereby reducing the cooling water consumption of a fractionating tower in the oil-gas fractionation process and the discharged ammonia-containing sewage quantity of the device, and reducing the energy consumption and the operation cost of the device.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure.
In the drawings:
fig. 1 is a schematic diagram of one embodiment of an apparatus for processing VOCs according to the present disclosure.
Description of the reference numerals
1. Buffer tank 2. gas supercharging equipment
3. Catalytic cracking riser reactor 4. catalytic cracking device separation purification system
5. Pre-lift nozzle 21 upstream line
22. Buffer tank outlet line 23 ejector motive medium line
24. Pressurized rear pipeline 25. reaction product gas pipeline
Detailed Description
The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
In the present disclosure, unless otherwise stated, the use of directional words such as "up" and "down" generally refers to the up and down of the device in normal use, and specifically refers to the orientation of the drawing in fig. 1. "inner and outer" are meant to refer to the profile of the device itself.
As shown in fig. 1, a first aspect of the present disclosure provides a method of processing VOCs, the method comprising: and (3) pressurizing the VOCs gas, then sending the pressurized VOCs gas into a catalytic cracking riser reactor 3, and sending the gas obtained by reaction into a catalytic cracking device separation and purification system 4 along with catalytic cracking reaction oil gas.
The method uses the existing riser reactor of the catalytic cracking unit and the product separation and purification system thereof in the refinery, adopts a reaction recovery method, simply and efficiently recovers and utilizes VOCs gas, and avoids the defects of high investment, heat waste, secondary pollution and the like of the traditional combustion method; in the method, gas obtained by reaction can enter a catalytic cracking device separation and purification system 4 along with catalytic cracking reaction oil gas, impurities such as sulfur, nitrogen and the like in VOCs gas are removed by utilizing the existing device, and sulfur and hydrocarbon substances in the VOCs gas are recovered; in addition, the method disclosed by the invention can reduce the pre-lifting steam consumption of the riser reactor of the catalytic cracking device and the oil-gas cooling water consumption at the top of the fractionating tower, reduce the amount of sewage containing ammonia discharged from the device, and reduce the energy consumption and the operation cost of the device.
In the method according to the present disclosure, there is no particular requirement for the VOCs gas to be treated, which may be of conventional origin, such as, for example, desulfurizer off-gas, caustic sludge tank off-gas, coker LPG sweetening off-gas, sump tank area off-gas, tank area diesel tank respiratory gas, andone or more of the breathing gases of the gasoline tank. The content of sulfur element in the VOCs gas can be 0-106mg/m3For example, it may be 5000 to 30000mg/m3(ii) a The content of N element can be 0-106mg/m3For example, it may be 10 to 1000mg/m3。
The method has no requirement on the pressure of the treated VOCs feed gas, and the method can be applied to negative pressure, normal pressure or positive pressure operation. In one embodiment of the present disclosure, to ensure that the gas entering the reactor 3 is maintained in a stable operating state, the pressure of the pressurized VOCs gas may be 0.3mpa (g) or more, and preferably may be 0.35 to 0.5mpa (g).
According to the present disclosure, the optional pressurization mode may be one or more of power medium pressurization, compressor pressurization and gas booster pressurization, and preferably may be one or more of power medium pressurization and compressor pressurization. When the method for boosting the power medium is selected, one or more of steam, dry gas, gas and fuel gas existing in the production of a refinery can be used as the boosting medium, preferably one or more of steam and dry gas, and the pressure of the boosting medium is used for boosting the VOCs raw material gas, so that the energy consumption and the operation cost of the device are saved, and the VOCs raw material gas under different pressures can have the same pressure at the outlet of the boosting equipment by adjusting the flow of the boosting medium.
In order to ensure that the flow rate of the VOCs gas entering the pressure boosting device 2 is stable, in one embodiment of the present disclosure, the VOCs gas may be fed into the buffer tank 1 for buffering before the pressure boosting step, so that the gas entering the pressure boosting device 2 has a stable flow rate, thereby ensuring the system stability. According to the present disclosure, the pressure of the buffer tank 1 employed may be in the range of-0.1 to 0.3MPa (g), preferably may be in the range of-0.1 to 0.1MPa (g).
The catalytic cracking riser reactor 3 employed in accordance with the present disclosure may be of a type conventional in the art and may, for example, include a pre-lift section which may be provided with pre-lift nozzles 5 into which pressurized VOCs gas may be injected via the pre-lift nozzles 5. The pressurized VOCs gas and steam for stripping can respectively enter the catalytic cracking riser reactor 3, and can also be mixed with the steam and then enter the pre-lifting section of the catalytic cracking riser reactor 3 through the pre-lifting nozzle 5. In a preferred embodiment, the pressurized VOCs gas and steam are mixed and then enter the pre-lift section of the catalytic cracking riser reactor 3 through the pre-lift nozzle 5, so that the amount of pre-lift steam is reduced, and the operation cost of the device is reduced. In the pre-lift section, the ratio of the mass flow rate of the pressurized VOCs gas to the mass flow rate of the water vapor may be 1: (0.1-100), and preferably may be 1: (1-10). The pre-lifting section disclosed by the invention simultaneously adopts VOCs gas and steam to lift the regenerated catalyst, and on the basis of recycling the VOCs gas, the VOCs gas is used for replacing part of the steam, so that the amount of the steam is saved, the amount of cooling water in the oil-gas condensation process at the top of the fractionating tower and the amount of ammonia-containing sewage discharged by the device are reduced, and the energy consumption and the operation cost of the device are reduced.
The second aspect of the present disclosure provides an apparatus for treating VOCs, which comprises an inlet of VOCs and a gas pressurizing device 2, which are sequentially communicated, wherein an outlet of the gas pressurizing device 2 is used for communicating with a catalytic cracking riser reactor 3.
The device disclosed by the invention utilizes the existing riser reactor of the catalytic cracking unit and the product separation and purification system thereof in a refinery, adopts a reaction recovery method to react VOCs gas in the catalytic cracking unit reactor and recover and utilize sulfur and hydrocarbon substances therein, avoids the defects of high investment, heat waste, secondary pollution and the like of the traditional combustion method, realizes high-efficiency simple and convenient recovery and utilization of VOCs, and simultaneously reduces energy consumption and device investment.
According to the present disclosure, the pressure range of the VOCs feed gas is great, in order to guarantee the device even running, make the VOCs gas that gets into reactor 3 have stable flow and pressure, in an embodiment, can be provided with VOCs buffer tank 1 between VOCs entry and the supercharging equipment, so that the feed gas gets into supercharging equipment 2 through buffer tank outlet pipeline 22 after buffering through VOCs buffer tank 1, behind the pressurization to certain pressure in supercharging equipment 2, pipeline 24 gets into reactor 3 after the pressurization.
According to the present disclosure, the type of the gas pressurizing device 2 is not limited, and in one embodiment of the present disclosure, the gas pressurizing device 2 may be used as one or more of a pressurizing injector, a compressor and a gas booster, and preferably may be used as one or more of a pressurizing injector and a compressor.
According to the present disclosure, in order to fully utilize the existing device and efficiently and simply realize the recycling of the VOCs, the device further comprises a catalytic cracking riser reactor 3 and a separation purification system 4 of the catalytic cracking device, and the outlet of the gas pressurization device 2 can be communicated with the inlet of the catalytic cracking riser reactor 3 through a pressurized pipeline 24.
According to the present disclosure, the catalytic cracking riser reactor 3 may be of a conventional type, and in one embodiment according to the present disclosure, the riser of the catalytic cracking riser reactor 3 may include a pre-lifting section, the bottom of the pre-lifting section is provided with a pre-lifting nozzle 5 extending to the inside of the pre-lifting section, and an inlet of the pre-lifting nozzle 5 is communicated with an outlet of the gas pressurizing device 2, so as to inject the pressurized VOCs raw material gas into the reactor 3 for reaction to achieve recycling.
The present disclosure is further illustrated by the following examples, but is not to be construed as being limited thereby.
Examples
As shown in fig. 1, the apparatus for treating VOCs of the present embodiment comprises a buffer tank 1, a booster ejector 2, a catalytic cracking riser reactor 3, and a separation purification system 4 of a catalytic cracking apparatus, which are connected in sequence. VOCs raw material gas enters a buffer tank 1 through an upstream pipeline 21 for buffering and then enters a pressurizing ejector 2, existing steam in a refinery is used for pressurizing and then enters a pre-lifting nozzle 5 through an outlet pipeline of the pressurizing ejector 2, after the pressurized VOCs gas reacts in a catalytic cracking riser reactor 3, the gas obtained by the reaction enters a separation and purification system 4 of a catalytic cracking device along with catalytic cracking reaction oil gas.
The upstream VOCs raw gas comes from the tail gas of a desulfurizing device, the tail gas of an alkaline residue tank, the tail gas of the coking device LPG sweetening device and the tail gas of a sump oil tank areaThe content of sulfide in VOCs is 16-95000mg/m30.3-12mg/m of ammonia3The total flow rate of VOCs after mixing was 471.2kg/h (containing sulphur and nitrogen). The pressure of the upstream VOCs raw material gas is normal pressure, the pressure in the buffer tank 1 is-0.02 MPa (g), VOCs gas at the outlet of the VOCs buffer tank 1 is pressurized to 0.45MPa (g) through a pressurizing ejector 2 and then is sent to the bottom of a catalytic cracking riser reactor 3 through a pre-lifting nozzle 5, and the mass flow ratio of the VOCs gas and steam in the lifting nozzle 5 is 1: 8. the ejector 2 adopts 1.0MPa (g) and steam at 250 ℃ as a power medium, and after the steam reacts in the catalytic cracking riser reactor 3, the steam and a reaction product of the catalytic cracking device enter the product separation and purification system 4 through a reaction product gas pipeline 25 to recover hydrocarbon substances.
By adopting the method for treating the VOCs, the recovery rate of hydrocarbon substances in the VOCs is more than 99 percent during normal continuous operation; compared with a catalytic cracking device without introducing VOCs gas, the pre-lifting steam dosage of the catalytic cracking riser reactor 3 is reduced by about 450kg/h, the discharge amount of ammonia-containing sewage is reduced by about 450kg/h, the oil gas cooling water dosage at the top of the fractionating tower is reduced by about 3000kg/h, and the energy consumption index of the device is favorably reduced.
Comparative example
The fourth generation Regenerative Thermal Oxidation (RTO) device adopts a rotary valve for shunting, a plurality of heat accumulators are compactly combined into a combustion chamber, and a heat exchanger or a hot air adjusting device is arranged in the combustion chamber, so that the heat supply requirement is met while waste gas is treated.
The VOCs is treated by adopting the RTO device, and the VOCs gas is heated to over 760 ℃, so that the VOCs are oxidized and decomposed into carbon dioxide and water. The high-temperature gas generated by oxidation flows through a specially-made ceramic heat accumulator to heat the ceramic body to store heat, and is used for preheating subsequently-entering organic waste gas so as to save fuel consumption of waste gas heating. The ceramic heat accumulator is divided into more than two (including two) zones or chambers, and each heat accumulator chamber sequentially undergoes heat accumulation-heat release-cleaning and other procedures, and the operation is repeated and continuous. After the heat accumulation chamber is discharged, a proper amount of clean air is required to be introduced immediately to clean the heat accumulation chamber, and the next heat accumulation procedure can be performed only after the cleaning is completed.
The RTO device adopts a ceramic heat accumulator, so that the device is heavy; it is desirable to operate as continuously as possible; the organic matters containing sulfur, nitrogen and halogen cannot be thoroughly purified; the exhaust gas temperature is high, and a waste heat boiler needs to be arranged subsequently to recover heat, so that part of heat is lost; the removal rate of VOCs is only 95%; when the VOCs contain S, N, the smoke needs to be purified to be discharged after reaching the standard; the process is complex, needs a large amount of additional equipment and occupied area, and has high one-time investment cost.
Compared with the method, the removal rate of VOCs in RTO treatment is low, the investment is high, the heat loss is large, the energy consumption and the operation cost are high, and the secondary pollution is serious.
The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.
It should be noted that, in the foregoing embodiments, various features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various combinations that are possible in the present disclosure are not described again.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.
Claims (10)
1. A method for processing VOCs, the method comprising:
and (3) pressurizing the VOCs gas, then sending the pressurized VOCs gas into a catalytic cracking riser reactor, and feeding the gas obtained by reaction into a separation and purification system of a catalytic cracking device along with catalytic cracking reaction oil gas.
2. The method of claim 1, wherein the pressurized VOCs gas has a pressure of 0.3mpa (g) or greater.
3. The method of claim 1, wherein the pressurization mode is one or more of power medium pressurization, compressor pressurization and gas booster pressurization; the power medium is one or more of water vapor, dry gas, gas and fuel gas.
4. The method of claim 1, wherein the method further comprises: feeding said VOCs gas to a buffer tank prior to said pressurizing step; the pressure of the buffer tank is-0.1 to 0.3MPa (g).
5. The process of claim 1 wherein the catalytic cracking riser reactor comprises a pre-lift section having a pre-lift nozzle through which the pressurized VOCs gas is injected into the pre-lift section; in the pre-lifting section, the mass flow ratio of the pressurized VOCs gas to the water vapor is 1: (0.1-100).
6. An apparatus for treating VOCs, comprising an inlet for VOCs and a gas pressurizing device in communication with each other, wherein an outlet of the gas pressurizing device is in communication with a catalytic cracking riser reactor.
7. The apparatus of claim 6, wherein a buffer tank of VOCs is further provided between the inlet of VOCs and the pressurizing device.
8. The apparatus of claim 6, wherein the pressure boosting device is one or more of a booster ejector, a compressor, and a gas booster.
9. The apparatus of claim 6, further comprising a catalytic cracking riser reactor and a separate purification system for the catalytic cracking apparatus, wherein the outlet of the gas pressurization device is in communication with the inlet of the catalytic cracking riser reactor.
10. The apparatus of claim 9, wherein the riser of the catalytic cracking riser reactor comprises a pre-lift section, the bottom of the pre-lift section is provided with a pre-lift nozzle extending to the inside of the pre-lift section, and the inlet of the pre-lift nozzle is communicated with the outlet of the gas pressurizing device.
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| CN201911411021.1A CN113117520A (en) | 2019-12-31 | 2019-12-31 | Device and method for processing VOCs |
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| CN208320470U (en) * | 2018-04-13 | 2019-01-04 | 中国石化工程建设有限公司 | A kind of processing unit of activated coke flue gas purification system regeneration tail gas |
| CN110339657A (en) * | 2018-04-03 | 2019-10-18 | 中国石化工程建设有限公司 | A kind of regeneration fume from catalytic cracking dry purification process and device |
| CN110368775A (en) * | 2018-04-13 | 2019-10-25 | 中国石化工程建设有限公司 | A kind of processing method and processing device of activated coke flue gas purification system regeneration tail gas |
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|---|---|---|---|---|
| JPH06343983A (en) * | 1993-06-02 | 1994-12-20 | Kurita Water Ind Ltd | Treatment for volatile organic halogenated compound |
| US5512082A (en) * | 1993-11-12 | 1996-04-30 | Uop | Process for the removal of volatile organic compounds from a fluid stream |
| JPH0910553A (en) * | 1995-06-27 | 1997-01-14 | Sumitomo Metal Mining Co Ltd | Treatment of discharged gas containing volatile organic halide |
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| CN110339657A (en) * | 2018-04-03 | 2019-10-18 | 中国石化工程建设有限公司 | A kind of regeneration fume from catalytic cracking dry purification process and device |
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| CN110368775A (en) * | 2018-04-13 | 2019-10-25 | 中国石化工程建设有限公司 | A kind of processing method and processing device of activated coke flue gas purification system regeneration tail gas |
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