CN114410340B - Method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil - Google Patents
Method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil Download PDFInfo
- Publication number
- CN114410340B CN114410340B CN202111605684.4A CN202111605684A CN114410340B CN 114410340 B CN114410340 B CN 114410340B CN 202111605684 A CN202111605684 A CN 202111605684A CN 114410340 B CN114410340 B CN 114410340B
- Authority
- CN
- China
- Prior art keywords
- oil
- reaction
- catalyst
- catalytic cracking
- bed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/18—Arsenic, antimony or bismuth
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/32—Manganese, technetium or rhenium
- C07C2523/34—Manganese
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil. The method comprises the following steps: directly introducing raw oil into a first reaction section of a downlink reaction bed to contact with a catalytic cracking catalyst for moderating catalytic cracking reaction; introducing the oil solution obtained in the first downlink reaction section into a second expanded reaction section for moderate catalytic cracking reaction, and introducing the obtained oil solution into a third expanded reaction section of a downlink reaction bed for deep catalytic cracking reaction to obtain an oil gas product and a catalyst to be regenerated; the oil gas products are separated to obtain products such as low-carbon olefin, aromatic hydrocarbon and the like, and the products are recycled after the regenerated catalyst is eluted and burnt for regeneration. The method can maximally prepare the low-carbon olefin and the aromatic hydrocarbon, and hardly generates fuel oil. The method is suitable for treating raw materials such as crude oil, vacuum wax oil, normal pressure residual oil, vacuum residual oil and the like with various properties, and has the advantages of high selectivity of low-carbon olefin and low-carbon aromatic hydrocarbon, low yield of dry gas and coke, simple process flow and low production cost.
Description
Technical Field
The invention belongs to a catalytic conversion method of petroleum hydrocarbon, in particular to a catalytic conversion method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil.
Background
Since the 50 s of the 20 th century, catalytic cracking processes have been developed to a great extent, and the processes occupy a significant position in the oil refining process, and are also the subject of important development of oil refining enterprises in the future.
The catalytic cracking reactor is used as one of the core devices of the catalytic cracking process, and is transited from a fluidized bed reactor to a riser reactor and a downlink reactor, so that researchers at home and abroad continuously optimize and improve the reactor in the aspects of reducing reaction time, improving oil contact efficiency, inhibiting back mixing and the like.
Compared with a conventional up-flow riser reactor, the down-flow reactor has the advantages that the catalyst descends in the reactor by means of gravity, the problem of minimum lifting speed of the catalyst does not exist, the axis and radial distribution of main parameters are relatively uniform, the gas is fixedly connected to flow near the plug flow, the performance of the reactor is improved, the yield of a catalytic cracking target product is improved, side reactions are restrained, and the dry gas and coke yield is reduced. The fluidized bed diameter variation can make the gas-solid flow state change obviously, and several different particle concentration fields or flow fields are formed in the same reactor. Different particle concentration fields can provide optimal reaction environments for different types of reactions, so that the depth and direction of complex catalytic reactions can be accurately regulated and controlled.
As early as 1983, the U.S. Mobil company proposed a FCC process concept with a downgoing reactor, and then Texaco company also disclosed a downgoing catapult catalytic cracking reactor patent technology (LETZSCH W S, DHARIA D, ROSS J, et al, the future of fluid catalytic cracking [ A ],1997NPRA Annual Meeting,San Antonio,Texas,1997.). By the 90 s of the 20 th century, downstream reactors were creatively used in millisecond catalytic cracking (MSCC) technology (Hou Fusheng.21 st century, national catalytic cracking development strategy [ a ], chinese petrochemical group company, chinese petro-chemical committee arguments, beijing: chinese petrochemical publishing, 2001:34-35;KAUFF D A,BARTHOLLS D B,STEVES C A,et al.Successful application of the MSCC process[A ],1996NPRA Annual Meeting,San Antonio,Texas,1996.).
Patent CN02125216.5 discloses a method for catalytic pyrolysis of hydrocarbons by using a downer reactor, which belongs to the petroleum product fractional pyrolysis technology. The reactor is used as a reactor, so that raw oil is subjected to catalytic pyrolysis reaction at high temperature and under the action of a catalyst to generate gas products mainly comprising light olefins such as ethylene, propylene, butylene and the like, and meanwhile, a stable liquid phase product rich in aromatic hydrocarbons is obtained. The patent adopts the descending bed reactor to realize gas-solid short-contact reaction, has a uniform gas-solid radial flow structure, and greatly reduces the gas-solid back mixing compared with the traditional riser reactor, so that the patent can obtain very high light olefin yield, and meanwhile, byproducts such as methane, coke and the like are fully inhibited.
Patent CN200410000267.7 discloses a method for producing clean gasoline and low-carbon olefin by catalytic pyrolysis of petroleum hydrocarbon. The fluidized bed reactor or the downer reactor is adopted, heavy raw oil petroleum hydrocarbon is used as a raw material, the raw material is contacted with a high-temperature catalyst for a short time under the action of atomized steam, the catalyst is high in catalyst-oil ratio, and the catalyst with high activity is matched for catalytic pyrolysis reaction, so that the low-carbon olefin and high-aromatic-content high-octane gasoline is obtained, and the product selectivity and the olefin yield are high.
The patent CN101045667A discloses a combined catalytic conversion method for producing low-carbon olefin in a high yield, which comprises the steps of contacting heavy oil raw materials with a regenerated catalyst and an optional carbon deposition catalyst in a down-pipe reactor, separating a cracking product from a spent catalyst, wherein the cracking product is separated to obtain the low-carbon olefin, at least one part of the rest products is introduced into the riser reactor to contact with the regenerated catalyst, separating oil gas from the catalyst, wherein the oil gas is separated to obtain the low-carbon olefin, and at least one part of the rest products is used as a product extraction device; the spent catalyst enters a regenerator after steam stripping, and the carbon deposition catalyst enters one or more devices of a pre-lifting section of a down-pipe reactor, a gas stripper connected with the down-pipe reactor and the regenerator in sequence after steam stripping, and the spent catalyst and the optional carbon deposition catalyst return to the down-pipe and the lifting pipe reactor after burning and regenerating. According to the method, propylene generated in the downlink reactor is separated from the catalyst in time, so that the secondary reaction of the propylene is effectively inhibited, and the yield of the low-carbon olefin is improved.
Patent CN110540860a discloses a process and system for catalytic cracking using double downcomers. The process comprises the following steps: 1) Sending heavy raw materials into the upper part of a first downlink pipe reactor to be contacted with a first catalytic cracking catalyst from the top of the first downlink pipe reactor, and carrying out catalytic cracking reaction from top to bottom; 2) The light raw material is sent into the upper part of a second downgoing pipe reactor to be contacted with a second catalytic cracking catalyst from the top of the second downgoing pipe reactor, and the catalytic cracking reaction is carried out from top to bottom; 3) And (2) feeding the first product and the first half regenerated catalyst obtained in the step (1) and the second product and the second half spent catalyst obtained in the step (2) into a fluidized bed reactor, enabling the first product and the first half regenerated catalyst to contact with a third catalytic cracking catalyst, and carrying out catalytic cracking reaction to obtain the third product and the spent catalyst. The process and the system can improve the yield of the low-carbon olefin and slow down the increase of the yield of the dry gas.
In summary, the above patent documents are limited to improvement of devices such as a riser, a downer reactor, a two-stage reducing downer reactor, and the like, and are limited in improvement of yield of low-carbon olefins and aromatic hydrocarbons when the device is used for preparing the low-carbon olefins and the low-carbon aromatic hydrocarbons by catalytic pyrolysis of raw oil, and particularly, the effect of improving the effect is not obvious when treating heavy and inferior raw oil.
Disclosure of Invention
The invention mainly aims at providing a method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil, aiming at the defects of the prior art.
In order to achieve the above object, the present invention provides a method for maximizing the production of light olefins and aromatics from a feedstock, comprising: directly introducing raw oil into a first reaction section of a downlink reaction bed to contact with a catalytic cracking catalyst for moderating catalytic cracking reaction; introducing the oil solution obtained in the first downlink reaction section into a second expanding reaction section for moderate catalytic cracking reaction, and introducing the obtained oil solution into a third expanding reaction section of a downlink reaction bed for deep catalytic cracking reaction to obtain an oil gas product and a catalyst to be regenerated. The oil gas product is subjected to a separation unit to obtain a high-value chemical raw material; after the regenerated catalyst is eluted by water vapor, the residual oil gas product is sent into a burning regenerator, and the regenerated catalyst is recycled.
In the above method for maximizing the production of light olefins and aromatic hydrocarbons, it may further preferably include the following specific steps:
1) After the raw oil is preheated to 80-380 ℃, the raw oil is sprayed into the top of a downer reactor from a feed atomizing nozzle to contact with a catalytic cracking catalyst, and enters a first reaction section of the downer reactor to carry out mild catalytic cracking reaction;
2) Introducing the obtained oil solution in the first expanding reaction section of the descending reaction bed into the second expanding reaction section of the descending reaction bed for moderate catalytic cracking reaction, and introducing the obtained oil solution into the third expanding reaction section of the descending reaction bed for deep catalytic cracking reaction to obtain an oil gas product and a catalyst to be regenerated;
the process conditions of the descending reaction bed are as follows: the reaction pressure is 0.01-0.5MPa, the reaction temperature is 450-680 ℃, the weight ratio of water vapor to raw oil is 0.1-10:1, and the catalyst-oil ratio is 4-25:1; the preferable process conditions are as follows: the reaction pressure is 0.05-0.2MPa, the reaction temperature is 480-600 ℃, the weight ratio of water vapor to raw oil is 0.5-5:1, and the catalyst-oil ratio is 6-15:1;
the reaction depth of raw materials in each reaction section is determined by the structure of the reducing reactor and the contact time, and the contact time of the three reaction sections of the descending bed is respectively as follows: the preferable contact time is 0.08-2 s, 0.02-2 s and 0.02-1 s respectively: 0.5 to 2s, 0.2 to 2s and 0.1 to 1s;
3) The oil gas product after the deep catalytic cracking reaction of the third expanded downlink reaction section and the catalyst to be regenerated enter a separation unit device connected with the third downlink reaction section, and the oil gas is separated from the catalyst to be regenerated;
the gasoline product in the step 3) is a gasoline fraction product rich in low-carbon olefin and high octane number; wherein at least a part of the light gasoline component at 40-80 ℃ and the heavy oil component at 320-420 ℃ in the oil gas product is returned to the first expanding reaction section for circulation.
In the above method for preparing low-carbon olefin and aromatic hydrocarbon maximally, preferably, the catalyst regeneration mode is one of single-stage regeneration, two-stage regeneration, turbulent bed, rapid bed or transport bed regeneration.
Preferably, the catalyst is a catalyst comprising, on a dry weight basis, 30-85wt% of a support, 10-50 wt% of a binder, and 0.1-20wt% of an active component on an oxide basis; it is further preferred to include 55 to 65wt% of a carrier, 30 to 45wt% of a binder, and 0.5 to 10% of an active component in terms of oxide.
The carrier comprises at least one of white carbon black, mesoporous high silicon molecular sieve, silicon dioxide, aluminum oxide, ferric oxide, zirconium oxide, titanium oxide, silicon aluminum composite oxide and silicon titanium composite oxide, preferably at least one of silicon dioxide, titanium oxide and zirconium oxide;
the binder is at least one of aluminum sol, aluminum gel, silica sol, silica gel, titanium sol, attapulgite, kaolin and montmorillonite, preferably at least one of silica sol, aluminum sol, attapulgite and kaolin;
the active component is at least one of alkali metal, alkaline earth metal, rare earth element, nickel, cobalt, manganese, gallium, bismuth, phosphorus and boron, preferably at least one of alkali metal, alkaline earth metal and lanthanum.
The raw oil comprises paraffin-based raw oil, intermediate-based raw oil and at least one of naphthenic raw oil, vacuum wax oil, atmospheric residue and vacuum residue with various properties; the feed oil also includes at least one of the above-mentioned feed oils blended into deasphalted oil, hydrocracked tail oil, shale oil, atmospheric residuum, vacuum residuum, and vacuum wax oil.
Compared with the prior art, the method has the beneficial effects that: the invention can convert non-aromatic components in the raw oil into low-carbon olefin to the greatest extent, converts aromatic components into low-carbon aromatic hydrocarbons and needle coke, reduces the yield of oil products with low added value and the dependence on hydrogen, and realizes the efficient utilization of petroleum resources, namely' Yikene and Yirene, and Yirene.
Detailed Description
The implementation of the technical solution of the present invention and the advantages thereof will be described in detail by the following specific examples, but should not be construed as limiting the scope of the implementation of the present invention.
Comparative example 1: process method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil of uplink riser reactor
And respectively taking intermediate base raw oil and vacuum residuum of a certain refinery as raw materials, and carrying out maximized raw oil preparation on the raw materials on an ascending riser reactor to prepare low-carbon olefin and aromatic hydrocarbon. The actual product distribution of the refinery is shown in Table 1.
The process conditions are as follows: the reaction pressure is 0.2MPa, the temperature is 520 ℃, the weight ratio of steam to raw oil is 0.3:1, the catalyst-oil ratio is 12:1, and the contact time is 2s.
The catalyst is an industrial FCC catalyst.
Comparative example 2: process method for maximally preparing low-carbon olefin and aromatic hydrocarbon from raw oil of downer reactor
The intermediate base raw oil and the vacuum residue oil of a certain refinery are respectively used as raw materials, and the raw oil is maximized on a downlink reactor to prepare the low-carbon olefin and the aromatic hydrocarbon. The raw material properties were the same as in comparative example 1.
The process conditions are as follows: the reaction pressure is 0.2MPa, the temperature is 520 ℃, the weight ratio of steam to raw oil is 0.3:1, the catalyst-oil ratio is 12:1, and the contact time is 2s;
the catalyst was as in comparative example 1.
Comparative example 3: process method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil of two-stage reducing downer reactor
The intermediate base raw oil and the vacuum residue oil of a certain refinery are respectively used as raw materials, and the raw oil is maximized on a downlink reactor to prepare the low-carbon olefin and the aromatic hydrocarbon. The raw material properties were the same as in comparative example 1.
The process conditions are as follows: the reaction pressure is 0.2MPa, the temperature is 520 ℃, the weight ratio of steam to raw oil is 0.3:1, the catalyst-oil ratio is 12:1, and the contact time is 2s.
The catalyst was as in comparative example 1.
The raw materials used in the examples and comparative examples are the same, and the properties are shown in Table 1. Unless otherwise indicated, the following is the same. Comparative examples representative product compositions are shown in table 2.
Example 1
And respectively taking intermediate base raw oil and vacuum residuum of a certain refinery as raw materials, and carrying out experiments of maximizing the raw oil to prepare low-carbon olefin and aromatic hydrocarbon on a three-section reducing downstream bed reactor device. The specific implementation steps are as follows:
by adopting the process method of the invention, the raw oil is directly introduced into the first expanding reaction section of the descending reaction bed to contact with the catalytic cracking catalyst for moderating the catalytic cracking reaction after being preheated to 200 ℃; introducing the oil solution obtained in the first expanding reaction section of the descending bed into the second expanding reaction section for medium catalytic cracking reaction, and introducing the obtained oil solution into the third expanding reaction section of the descending bed for deep catalytic cracking reaction to obtain an oil gas product and a catalyst to be regenerated. The oil gas product is subjected to a separation unit to obtain a high-value chemical raw material; after the regenerated catalyst is eluted by water vapor, the residual oil gas product is sent into a burning regenerator, and the regenerated catalyst is recycled. The method of the patent technology can prepare the low-carbon olefin and the aromatic hydrocarbon from the raw oil to the maximum extent, and has high selectivity of the low-carbon olefin and the low-carbon aromatic hydrocarbon and low yield of dry gas and coke.
The process conditions are as follows: the reaction pressure is 0.2MPa, the temperature is 520 ℃, the weight ratio of steam to raw oil is 3:1, the catalyst-oil ratio is 10:1, and the contact time of three reaction sections of the reducing descending bed from top to bottom is as follows: 2s, 1s and 0.5s.
The catalyst preparation process is as follows: mixing attapulgite with water, pulping, adding silica sol, adding hydrochloric acid for acidification, stirring for 2 hours, adding macroporous silica powder, pulping, stirring for 0.5 hour, adding alkali metal barium acetate and manganese nitrate, continuously stirring for half an hour, and spraying to prepare the microsphere catalyst. The catalyst was 60wt% support, and 32wt% binder on a dry basis, and 8wt% active component on an oxide basis. The catalyst was subjected to hydrothermal aging at 800℃under 100% steam for 6 hours before use. The catalyst was designated DPC-1.
Example 2
The reaction materials and the process were the same as in example 1.
The process conditions are as follows: the reaction pressure is 0.2MPa, the temperature is 520 ℃, the weight ratio of steam to raw oil is 3:1, the catalyst-oil ratio is 10:1, and the contact time of three reaction sections of the reducing descending bed from top to bottom is as follows: 2s, 1.5s and 1s.
The preparation process of the catalyst comprises the following steps: mixing attapulgite with water, pulping, adding silica sol, adding hydrochloric acid for acidification, stirring for 2h, adding a molecular sieve, pulping, stirring for 0.5h, adding alkali metal magnesium acetate and bismuth nitrate, continuously stirring for 0.5h, and spraying to prepare the microsphere catalyst. The catalyst was 60wt% support, and 32wt% binder on a dry basis, and 8wt% active component on an oxide basis. The catalyst was subjected to hydrothermal aging at 800℃under 100% steam for 6 hours before use. The catalyst was designated DPC-2.
Example 3
The reaction materials and the process were the same as in example 1.
The catalyst was the same as in example 2.
The process conditions are as follows: the reaction pressure is 0.2MPa, the temperature is 520 ℃, the weight ratio of steam to raw oil is 3:1, the catalyst-oil ratio is 10:1, and the contact time of three reaction sections of the reducing descending bed from top to bottom is as follows: 2s, 2s and 1s.
The preparation process of the catalyst comprises the following steps: mixing kaolin and water, pulping, sequentially adding silica sol and aluminum sol, adding hydrochloric acid for acidification, stirring for 2h, adding a molecular sieve, pulping, stirring for 0.5h, adding alkali metal magnesium acetate and manganese nitrate, continuously stirring for half an hour, and spraying to prepare the microsphere catalyst. The catalyst was 65wt% support, and 27wt% binder on a dry basis, and 8wt% active component on an oxide basis. The catalyst was subjected to hydrothermal aging at 800℃under 100% steam for 6 hours before use. The catalyst was designated DPC-2.
Representative product compositions for the examples are shown in Table 2.
Table 1 basic properties of the raw materials used in comparative examples and examples
Table 2 comparative and example representative product schemes (intermediate crude oil)
Note that: reaction temperature
Table 3 comparative and example representative product schemes (vacuum residuum)
Compared with the comparative example, the method for preparing the low-carbon olefin and the aromatic hydrocarbon by using the raw oil provided by the invention has the advantages that the raw oil sequentially passes through the variable-diameter downer reactor, the conversion rate of heavy components in the raw oil is improved by controlling the reaction depth of each reaction section, and the secondary reaction of the low-carbon olefin and the aromatic hydrocarbon is inhibited, so that the dry gas and the coke yield are reduced, and the raw material yield of chemicals is increased maximally. The foregoing embodiments are merely illustrative of the technical concept and features of the present invention, and are not intended to limit the scope of the invention in any way. All equivalent changes or modifications made according to the spirit of the main technical proposal of the invention should be covered in the protection scope of the invention.
Claims (9)
1. A method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil is characterized in that: preheating raw oil, and then spraying the preheated raw oil into a first expanding reaction section of a downlink reaction bed to contact a catalytic cracking catalyst for moderating catalytic cracking reaction; introducing the oil solution obtained in the first expanding reaction section of the descending reaction bed into the second expanding reaction section for moderate catalytic cracking reaction, and introducing the product oil solution into the third expanding reaction section of the descending reaction bed for deep catalytic cracking reaction to obtain an oil gas product and a catalyst to be regenerated; the oil gas product is subjected to a separation unit to obtain a high-value chemical raw material; after the regenerated catalyst is eluted by water vapor, the residual oil gas product is sent into a coke burning regenerator for catalyst regeneration, and the regenerated catalyst is recycled; the catalytic cracking catalyst comprises a carrier, a binder and an active component, wherein the carrier comprises at least one of white carbon black, mesoporous high-silicon molecular sieve, silicon dioxide, aluminum oxide, ferric oxide, zirconium oxide, titanium oxide, silicon-aluminum composite oxide and silicon-titanium composite oxide, the binder is at least one of aluminum sol, aluminum gel, silica gel, titanium sol, attapulgite, kaolin and montmorillonite, and the active component is at least one of alkali metal, alkaline earth metal, rare earth element, nickel, cobalt, manganese, gallium, bismuth, phosphorus and boron.
2. The method according to claim 1, characterized by the steps of:
1) Preheating raw oil to 80-380 ℃, spraying the raw oil into the top of a downstream reaction bed to contact with a catalytic cracking catalyst, and entering a first expanding reaction section of the downstream reaction bed to carry out mild catalytic cracking reaction;
2) Introducing the oiling agent obtained in the first expanding reaction section of the descending reaction bed into the second expanding reaction section for moderate catalytic cracking reaction;
3) Introducing the oil agent obtained by the moderate catalytic cracking reaction into a third expanding reaction section of a downstream reaction bed to carry out deep catalytic cracking reaction, so as to obtain a mixture of an oil gas product and a catalyst to be regenerated;
4) The mixture of the oil gas product and the catalyst to be regenerated enters a separation unit device connected with a third expanding reaction section, and the oil gas product and the catalyst to be regenerated are separated;
the reaction depth of raw materials in the first reaction section, the second diameter-expanding reaction section and the third diameter-expanding reaction section of the descending reaction bed is controlled by the contact time of oil solution, and the contact time of the three reaction sections is respectively as follows: 0.08 to 1s, 0.02 to 2s and 0.02 to 1s;
the process conditions of the descending reaction bed are as follows: the reaction pressure is 0.01-0.5MPa, the reaction temperature is 450-680 ℃, the weight ratio of steam to raw oil is 0.1-10:1, and the catalyst-oil ratio is 4-25:1;
the oil gas product is a gasoline fraction product rich in low-carbon olefin and high octane number; wherein at least a part of the light gasoline component at 40-80 ℃ and the heavy oil component at 320-420 ℃ in the oil gas product is returned to the first expanding reaction section for circulation.
3. The method according to claim 1, wherein the three reaction sections of the downer are contacted for 0.5-1 s, 0.5-2 s, 0.1-1 s, respectively.
4. The method of claim 1, wherein the downstream reaction bed process conditions are: the reaction pressure is 0.05-0.2MPa, the reaction temperature is 480-600 ℃, the weight ratio of steam to raw oil is 0.5-5:1, and the catalyst-oil ratio is 6-15:1.
5. The method of claim 1, wherein the catalyst regeneration is one of a single stage regeneration, a two stage regeneration, a turbulent bed, a rapid bed, or a transport bed regeneration.
6. The process of claim 1 wherein the catalytic cracking catalyst comprises, on a dry weight basis, 30-85wt% support, 10-50 wt% binder, and 0.1-20wt% active component on an oxide basis.
7. The process of claim 1 wherein the catalytic cracking catalyst comprises, on a dry weight basis, 50-65wt% support, 30-40 wt% binder, and 2-10% active component on an oxide basis.
8. The method of claim 1, wherein the feedstock is at least one of crude oil, vacuum wax oil, atmospheric residuum, and vacuum residuum of various nature.
9. The method of claim 8, wherein the feedstock further incorporates at least one of deasphalted oil, hydrocracked tail oil, shale oil, atmospheric residuum, vacuum residuum, and vacuum wax oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111605684.4A CN114410340B (en) | 2021-12-26 | 2021-12-26 | Method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111605684.4A CN114410340B (en) | 2021-12-26 | 2021-12-26 | Method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114410340A CN114410340A (en) | 2022-04-29 |
| CN114410340B true CN114410340B (en) | 2023-08-04 |
Family
ID=81269502
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111605684.4A Active CN114410340B (en) | 2021-12-26 | 2021-12-26 | Method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114410340B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609174A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor hydrocarbons catalytic conversion method and its device |
| CN109679686A (en) * | 2017-10-18 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of hydrocarbon cracking method of high output of ethylene and light aromatic hydrocarbons |
| CN110819385A (en) * | 2018-08-10 | 2020-02-21 | 中国石油化工股份有限公司 | Catalytic cracking method |
| CN113663607A (en) * | 2021-09-14 | 2021-11-19 | 中国石油大学(北京) | Downer reactor and method of operating same |
-
2021
- 2021-12-26 CN CN202111605684.4A patent/CN114410340B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109679686A (en) * | 2017-10-18 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of hydrocarbon cracking method of high output of ethylene and light aromatic hydrocarbons |
| CN110819385A (en) * | 2018-08-10 | 2020-02-21 | 中国石油化工股份有限公司 | Catalytic cracking method |
| CN109609174A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor hydrocarbons catalytic conversion method and its device |
| CN113663607A (en) * | 2021-09-14 | 2021-11-19 | 中国石油大学(北京) | Downer reactor and method of operating same |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114410340A (en) | 2022-04-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101724452B (en) | Fluid catalytic cracking process, and gasoline and liquefied petroleum gas obtained by process | |
| CN103031147A (en) | Catalytic conversion method for processing high-nitrogen raw material | |
| US20190316041A1 (en) | Process for producing low-carbon olefins by gaseous phase catalytic cracking of heavy oil with multi-stages in milliseconds | |
| CN103031148B (en) | The catalysis conversion method of processing high-nitrogen stock | |
| CN1069016A (en) | The method of preparing ethene by direct conversion of heavy hydrocarbon | |
| CN101205475B (en) | Hydrocarbons catalytic conversion method for preparing low olefin-content gasoline | |
| US10508247B2 (en) | Process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation | |
| CN114410340B (en) | Method for preparing low-carbon olefin and aromatic hydrocarbon by maximizing raw oil | |
| CN1340602A (en) | Two-stage catalytic cracking process for hydrocarbon oil | |
| CN101899324B (en) | Catalytic conversion method for producing light diesel oil with high hexadecane value and low olefin gasoline | |
| CN113621401B (en) | Method for preparing ethylene, propylene and aromatic hydrocarbon to maximum extent | |
| CN112457874B (en) | Method for controlling multistage catalytic cracking according to multi-zone partition coupling bed layers of raw material types | |
| CN1333048C (en) | Petroleum hydrocarbon catalytic conversion method | |
| CN116004279A (en) | Hydrogen production and CO enrichment from hydrocarbon raw materials 2 Is a method of (2) | |
| US9580664B2 (en) | Catalytic conversion method for improving product distribution | |
| CN114410345B (en) | Method for directly preparing low-carbon olefin and aromatic hydrocarbon from raw oil | |
| CN113004936A (en) | Method, device and reaction system for producing low-carbon olefin from petroleum hydrocarbon | |
| CN112322325A (en) | Multi-bed-layer partition cooperative control multi-stage catalytic cracking method according to raw material types | |
| CN114410344B (en) | Catalytic conversion method for inferior oil | |
| CN114686252B (en) | Method for preparing chemicals from crude oil | |
| CN114410346B (en) | Method for preparing low-carbon olefin and aromatic hydrocarbon from crude oil | |
| CN1286948C (en) | Catalytic cracking process for preparing high-grade gasoline | |
| CN104109557B (en) | The catalysis conversion method of a kind of inferior distillate oil or heavy oil product | |
| CN116083121A (en) | Method for producing light olefins and light aromatics from heavy hydrocarbons | |
| CN109554192A (en) | A kind of method of oil shale oil catalyzed conversion |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |