CN113058508A - Device and method for recycling polluted methanol - Google Patents
Device and method for recycling polluted methanol Download PDFInfo
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- CN113058508A CN113058508A CN202110312312.6A CN202110312312A CN113058508A CN 113058508 A CN113058508 A CN 113058508A CN 202110312312 A CN202110312312 A CN 202110312312A CN 113058508 A CN113058508 A CN 113058508A
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/007—Separating solid material from the gas/liquid stream by sedimentation
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/065—Feeding reactive fluids
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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Abstract
A device and a method for recycling polluted methanol belong to the technical field of methanol recycling, a catalytic cracking riser reactor is used as a reaction device, polluted methanol and heavy oil are simultaneously introduced into the reaction device, and the reaction is carried out at a preset temperature and under a preset pressure to generate an oil-gas mixture. The content of liquefied gas in the oil-gas mixture generated by the reaction is greatly increased, the resource recycling of the polluted methanol is realized, 90-95% of the polluted methanol can be converted into liquefied gas by the method, the polluted methanol is recycled, the waste is reduced, and the economic benefit is increased. The device provided by the invention can realize the method, has a simple structure and is convenient to operate.
Description
Technical Field
The invention belongs to the technical field of methanol recovery, and particularly relates to a device and a method for resource recovery of polluted methanol.
Background
In the MTBE preparation process, methanol and isobutene are used as raw materials to produce MTBE, a large amount of polluted methanol containing impurities is generated, the polluted methanol passes through a water washing tower firstly, impurities insoluble in water are removed, then the polluted methanol enters a methanol recovery tower, the polluted methanol discharged from the methanol recovery tower contains phenols, sulfur and other impurities, if the polluted methanol enters an MTBE device again, the catalyst can be poisoned, and if the polluted methanol is discharged, the great waste is caused, and the environment is polluted.
Disclosure of Invention
In view of the above, there is a need for a method for recycling waste methanol to solve the problems that the waste methanol contains impurities such as phenols and sulfur, and if the waste methanol enters the MTBE device again, the catalyst is poisoned, and if the waste methanol is discharged, the waste methanol is greatly wasted and the environment is polluted.
The invention also provides a device for recycling the polluted methanol by realizing the method.
In order to achieve the above objects, in one aspect, the present invention provides a method for resource recovery of contaminated methanol, which uses a catalytic cracking riser reactor as a reaction apparatus, and simultaneously feeds contaminated methanol and heavy oil into the reaction apparatus, and performs a reaction at a predetermined temperature and a predetermined pressure to generate an oil-gas mixture.
Preferably, the adding amount of the polluted methanol is 2.2-4.3% of the adding amount of the heavy oil.
Preferably, the preset temperature is 520-620 ℃, and the preset pressure is 0.09-0.12 MPa.
Preferably, the pre-lift gas of the reaction device is dry gas and steam mixed in a predetermined ratio.
Preferably, the dry gas accounts for 10-30% of the total amount of the pre-lift gas, and the balance is steam.
In another aspect, the present invention also provides an apparatus for resource recovery of contaminated methanol, which implements the above method, the apparatus comprising:
the riser reactor is used for heavy oil catalytic cracking reaction, riser reactor bottom is provided with promotes gas inlet pipe and heavy oil inlet pipe in advance, it is provided with the methyl alcohol inlet pipe to promote the gas inlet pipe in advance, the vertical section that promotes the gas inlet pipe in advance sets up venturi, venturi's circular cone contraction section entry is connected to the methyl alcohol inlet pipe.
Preferably, the pre-lift gas feed pipe is further provided with a dry gas feed pipe and a vapour feed pipe, the methanol feed pipe being located above the dry gas feed pipe and the vapour feed pipe.
Preferably, the dry gas inlet pipe slope sets up and forms the acute angle with the vapour inlet pipe, vapour inlet pipe and dry gas inlet pipe pass through proportional control ware control, the corner of promoting the gas inlet pipe in advance is the arc corner, the dry gas inlet pipe sets up on the arc corner outer wall of promoting the gas inlet pipe in advance.
Preferably, the catalytic cracking device further comprises a settler, the settler is used for gas-solid separation and is provided with an oil mixture inlet, an oil gas outlet and a catalyst outlet, and the oil mixture inlet of the settler is connected with the oil mixture outlet of the riser reactor.
Preferably, the catalytic cracking apparatus further comprises a regenerator for catalyst regeneration, which is arranged at the lower part of the settler, a catalyst inlet of the regenerator is connected with a catalyst outlet of the settler, and a catalyst outlet of the regenerator is connected with a catalyst inlet of the riser reactor.
By adopting the technical scheme, the invention has the beneficial effects that:
the method for recycling the polluted methanol provided by the invention comprises the steps of introducing the polluted methanol and heavy oil into a catalytic cracking riser reactor, wherein the polluted methanol is atomized and then enters the riser reactor, and the polluted methanol is reacted at a preset temperature and a preset pressure to generate an oil-gas mixture. The content of liquefied gas in the oil gas generated by the reaction is greatly improved, and the resource recycling of the polluted methanol is realized. By the method, 90-95% of the polluted methanol is converted into the liquefied gas, so that waste and environmental pollution are avoided, the polluted methanol is recycled, the yield of the liquefied gas in the catalytic cracking reaction is improved, the polluted methanol is prevented from being used for MTBE reaction to cause catalyst poisoning, the cost is greatly saved, and great economic benefits are generated.
The device for recycling the polluted methanol provided by the invention can realize the method for recycling the polluted methanol, and has the advantages of simple structure and convenience in operation.
Drawings
FIG. 1 is a schematic structural diagram of a device for resource recovery of contaminated methanol.
In the figure: riser reactor 100, settler 200, regenerator 300, pre-lift gas feed line 110, methanol feed line 111, dry gas feed line 112, vapor feed line 113.
Detailed Description
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
The embodiment of the invention provides a method for recycling polluted methanol, and a device for realizing the method is shown in figure 1, a catalytic cracking riser reactor is used as a reaction device, the polluted methanol and heavy oil are simultaneously introduced into the reaction device, and the reaction is carried out at a preset temperature and a preset pressure to generate an oil-gas mixture.
Dirty methyl alcohol gets into riser reactor 100, dirty methyl alcohol is atomized under the effect of pre-lift gas, obtains atomizing dirty methyl alcohol, and the contact area of atomizing increase reactant lets in heavy oil in riser reactor 100, and the catalyst also upwards flows under the effect of pre-lift gas simultaneously, and under predetermined temperature, predetermined pressure, atomizing dirty methyl alcohol takes place catalytic reaction when meetting the catalyst and generates low carbon olefin, and this process turns dirty methyl alcohol into liquefied gas, has realized dirty methyl alcohol's resource reuse, and resources are saved avoids extravagant.
Furthermore, the adding amount of the polluted methanol is 2.2% -4.3% of that of the heavy oil.
Further, the preset temperature is 520-620 ℃, and the preset pressure is 0.09-0.12 MPa.
Further, the pre-lift gas of the reaction device is dry gas and steam which are mixed in a preset ratio, and the dry gas can protect the catalyst from being cracked easily.
Furthermore, the dry gas accounts for 10-30% of the total amount of the pre-lifting gas, and the balance is steam.
Referring to fig. 1, the present invention also provides an apparatus for resource recovery of contaminated methanol, which implements the above method, the apparatus comprising: riser reactor 100 for dirty methanol catalytic reaction and heavy oil catalytic cracking reaction, riser reactor 100 bottom is provided with in advance and promotes gas inlet pipe 110 and heavy oil inlet pipe, and the vertical section that promotes gas inlet pipe 110 in advance sets up venturi, the circular cone shrink section entry of venturi is connected to methanol inlet pipe 111.
Further, pre-lift gas feed line 110 is provided with a methanol feed line 111, a dry gas feed line 112, and a vapor feed line 113, wherein dry gas feed line 112 and vapor feed line 113 are located below methanol feed line 111.
Further, dry gas inlet pipe 112 slope setting and with the vapour inlet pipe acute angle of formation, vapour inlet pipe 113 and dry gas inlet pipe 112 pass through proportional control ware control, the corner of pre-lifting gas inlet pipe is arc corner, dry gas inlet pipe 112 sets up on the arc corner outer wall of pre-lifting gas inlet pipe 110.
Further, the catalytic cracking apparatus further comprises a settler 200, wherein the settler 200 is used for gas-solid separation and is provided with an oil mixture inlet, an oil gas outlet and a catalyst outlet, and the oil mixture inlet of the settler 200 is connected with the oil mixture outlet of the riser reactor 100.
Further, the catalytic cracking apparatus further comprises a regenerator 300, wherein the regenerator 300 is used for catalyst regeneration and is arranged at the lower part of the settler 200, a catalyst inlet of the regenerator 300 is connected with a catalyst outlet of the settler 200, and a catalyst outlet of the regenerator 300 is connected with a catalyst inlet of the riser reactor 100.
The technical effects of the present invention are further described in detail by the following specific examples:
example 1
Introducing 1.5t/h of steam into a pre-lifting gas feeding pipe 110 as pre-lifting gas, washing a dirty methanol mixture from an MTBE device with water, feeding the dirty methanol mixture into a methanol recovery tower, feeding the dirty methanol in the methanol recovery tower into a methanol feeding pipe 111, wherein the introduction amount of the dirty methanol is 0.5t/h, feeding the dirty methanol into the pre-lifting gas feeding pipe 110, atomizing the dirty methanol, enabling the dirty methanol to flow upwards in a riser reactor 100, introducing 22.8t/h of heavy oil through a heavy oil inlet pipe at the lower part of the riser reactor 100, simultaneously feeding a catalyst into the riser reactor 100 from an outlet of a regenerator 200, enabling the dirty methanol and the heavy oil to flow upwards under the driving of the pre-lifting gas, reacting in the riser reactor 100, wherein the reaction temperature is 520-620 ℃, and the reaction pressure is 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
To verify the effectiveness of the present invention, the average of the product distribution obtained by conducting a number of tests using the apparatus and process described in FIG. 1 was compared with the average of the product distribution obtained by a comparative example, which was unpublished methanol, under the same conditions as in example 1, as shown in Table 1.
TABLE 1 product distribution
As can be seen from Table 1, compared with the experimental result without adding the polluted methanol, the yield of the liquefied gas in the product obtained by the method provided by the invention is increased by 1.9%, the yield of the liquefied gas is increased by 0.456t in 24 hours on average, and the economic benefit is increased by 1459 yuan.
Example 2
Introducing 1.5t/h of steam into a pre-lifting gas feed pipe 110 to serve as pre-lifting gas, washing a dirty methanol mixture from an MTBE device, introducing the dirty methanol mixture into a methanol recovery tower, introducing the dirty methanol into a methanol feed pipe 111, wherein the introduction amount of the dirty methanol is 1t/h, introducing the dirty methanol into the pre-lifting gas feed pipe 110, atomizing the dirty methanol, enabling the dirty methanol to flow upwards in a riser reactor 100, introducing 22.8t/h of heavy oil through a heavy oil inlet pipe at the lower part of the riser reactor 100, simultaneously introducing a catalyst into the riser reactor 100 from an outlet of a regenerator 200, enabling the dirty methanol and the heavy oil to flow upwards under the driving of the pre-lifting gas, reacting in the riser reactor 100, wherein the reaction temperature is 520-620 ℃, and the reaction pressure is 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
To verify the effectiveness of the present invention, the average of the product distribution obtained by conducting a number of tests using the apparatus and process described in FIG. 1 was compared with the average of the product distribution obtained by a comparative example, which was unpublished methanol, under the same conditions as in example 2, as shown in Table 2.
TABLE 2 product distribution
As can be seen from Table 2, compared with the experimental result of the method without adding the polluted methanol, the yield of the liquefied gas in the product obtained by the method provided by the invention is increased by 4.2%, the yield of the liquefied gas is increased by 1.008t in 24 hours on average, and the economic benefit is increased by 3225 yuan.
Example 3
Introducing 1.5t/h of pre-lift gas into a pre-lift gas feed pipe 110, wherein the dry gas is 0.22 t/h, the steam is 1.28 t/h, a dirty methanol mixture from an MTBE device enters a methanol recovery tower through water washing, dirty methanol in the methanol recovery tower enters a methanol feed pipe 111, the introduction amount of the dirty methanol is 1t/h, the dirty methanol enters the pre-lift gas feed pipe 110, is atomized and flows upwards in a riser reactor 100, 22.8t/h of heavy oil is introduced through a heavy oil inlet pipe at the lower part of the riser reactor 100, meanwhile, a catalyst enters the riser reactor 100 from an outlet of a regenerator 200, is driven by the pre-lift gas to flow upwards to contact the dirty methanol and the heavy oil, and reacts in the riser reactor 100, the reaction temperature is 520-620 ℃, and the reaction pressure is 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
To verify the effectiveness of the present invention, the average product distribution obtained from multiple tests using the apparatus and process described in FIG. 1 was compared to the average product distribution obtained from a comparative example using steam as the pre-lift gas, all other conditions being the same as in example 3, as shown in Table 3.
TABLE 3 product distribution
As can be seen from Table 3, compared with the experimental results of using steam as the pre-lift gas, the yield of gasoline in the product obtained by the method of the invention is improved by 0.54%, the yield of diesel oil is improved by 0.36%, the yield of liquefied gas is improved by 0.1%, 270Kg of catalyst can be saved on average every day, the cost is reduced by 2700 Yuan, and the sewage discharge amount is reduced.
Example 4
Introducing 1.5t/h of pre-lift gas into a pre-lift gas feed pipe 110, wherein dry gas is 0.27t/h, steam is 1.23t/h, a dirty methanol mixture from an MTBE device enters a methanol recovery tower through water washing, dirty methanol in the methanol recovery tower enters a methanol feed pipe 111, the introduction amount of the dirty methanol is 1t/h, the dirty methanol enters the pre-lift gas feed pipe 110, is atomized and flows upwards in a riser reactor 100, 22.8t/h of heavy oil is introduced through a heavy oil inlet pipe at the lower part of the riser reactor 100, meanwhile, a catalyst enters the riser reactor 100 from an outlet of a regenerator 200, is driven by the pre-lift gas to flow upwards to contact the dirty methanol and the heavy oil, and reacts in the riser reactor 100 at the reaction temperature of 520-620 ℃ and the reaction pressure of 0.1 MPa.
The generated oil mixture enters the settler 200 to realize gas-solid separation, the catalyst flows out from the catalyst outlet of the settler 200 and enters the regenerator 300 to be regenerated, and the regenerated catalyst flows out from the outlet of the regenerator 300 and enters the riser reactor 100 again to realize the reutilization of the catalyst. The oil gas flows out from the oil gas outlet of the settler 200, and gasoline, diesel oil, liquefied gas, dry gas and the like are obtained after post-treatment.
To verify the effectiveness of the present invention, the average product distribution obtained from multiple tests using the apparatus and process described in FIG. 1 was compared to the average product distribution obtained from a comparative example using steam as the pre-lift gas, all other conditions being the same as in example 4, as shown in Table 4.
TABLE 4 product distribution
As can be seen from Table 4, compared with the experimental results of using steam as the pre-lift gas, the yield of gasoline in the product obtained by the method of the invention is improved by 0.6%, the yield of diesel oil is improved by 0.4%, the yield of liquefied gas is improved by 0.1%, 289Kg of catalyst can be saved on average every day, 2890 yuan of cost is reduced, and the sewage discharge amount is reduced.
The device can also be filled with pure methanol to achieve the effect.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.
Claims (10)
1. A method for recycling polluted methanol is characterized in that: the catalytic cracking riser reactor is used as a reaction device, dirty methanol and heavy oil are simultaneously introduced into the reaction device, and the reaction is carried out at a preset temperature and a preset pressure to generate an oil-gas mixture.
2. The method for resource recovery of polluted methanol as claimed in claim 1, wherein the method comprises the following steps: the adding amount of the polluted methanol is 2.2% -4.3% of that of the heavy oil.
3. The method for resource recovery of polluted methanol as claimed in claim 2, wherein: the preset temperature is 520-620 ℃, and the preset pressure is 0.09-0.12 MPa.
4. The method for resource recovery of polluted methanol as claimed in claim 1, wherein the method comprises the following steps: the pre-lift gas of the reaction device is dry gas and steam which are mixed in a preset ratio.
5. The method for resource recovery of polluted methanol as claimed in claim 1, wherein the method comprises the following steps: the dry gas accounts for 10-30% of the total amount of the pre-lifting gas, and the balance is steam.
6. An apparatus for resource recovery of contaminated methanol for carrying out the method according to any one of claims 1 to 5, characterized in that the apparatus comprises: the riser reactor is used for heavy oil catalytic cracking reaction, riser reactor bottom is provided with promotes gas inlet pipe and heavy oil inlet pipe in advance, it is provided with the methyl alcohol inlet pipe to promote the gas inlet pipe in advance, the vertical section that promotes the gas inlet pipe in advance sets up venturi, the circular cone shrink section entry of venturi is connected to the methyl alcohol inlet pipe.
7. The apparatus for resource recovery of contaminated methanol according to claim 6, wherein: the pre-lift gas feed pipe is further provided with a dry gas feed pipe and a vapor feed pipe, which are located below the methanol feed pipe.
8. The apparatus for resource recovery of contaminated methanol according to claim 6, wherein: the dry gas inlet pipe inclines to set up and forms the acute angle with the vapour inlet pipe, vapour inlet pipe and dry gas inlet pipe pass through proportional control ware control, the corner that promotes the gas inlet pipe in advance is arc corner, the dry gas inlet pipe sets up on the arc corner outer wall that promotes the gas inlet pipe in advance.
9. The apparatus for resource recovery of contaminated methanol according to claim 6, wherein: the catalytic cracking device also comprises a settler, wherein the settler is used for gas-solid separation and is provided with an oil mixture inlet, an oil gas outlet and a catalyst outlet, and the oil mixture inlet of the settler is connected with the oil mixture outlet of the riser reactor.
10. The apparatus for resource recovery of contaminated methanol according to claim 6, wherein: the catalytic cracking device also comprises a regenerator, wherein the regenerator is used for regenerating a catalyst and is arranged at the lower part of the settler, a catalyst inlet of the regenerator is connected with a catalyst outlet of the settler, and a catalyst outlet of the regenerator is connected with a catalyst inlet of the riser reactor.
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| CN109957421A (en) * | 2017-12-25 | 2019-07-02 | 中国石油天然气股份有限公司 | Combination method of catalytic cracking and light hydrocarbon deep processing |
| CN110950731A (en) * | 2018-09-27 | 2020-04-03 | 中国石油化工股份有限公司 | Catalytic cracking method |
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2021
- 2021-03-24 CN CN202110312312.6A patent/CN113058508A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3974062A (en) * | 1974-10-17 | 1976-08-10 | Mobil Oil Corporation | Conversion of full range crude oils with low molecular weight carbon-hydrogen fragment contributors over zeolite catalysts |
| CN101081995A (en) * | 2006-05-31 | 2007-12-05 | 中国石油化工股份有限公司 | Method for reducing sulfur content of catalytically cracked gasoline |
| CN101210190A (en) * | 2006-12-27 | 2008-07-02 | 中国石油化工股份有限公司 | A method for producing light olefins and gasoline by co-feeding heavy petroleum hydrocarbons and methanol |
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| CN109679680A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of catalysis conversion method of light fraction oil |
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