CN114045179A - Multiphase flow residual oil hydro-upgrading and catalytic cracking combined process and system - Google Patents
Multiphase flow residual oil hydro-upgrading and catalytic cracking combined process and system Download PDFInfo
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- CN114045179A CN114045179A CN202111443208.7A CN202111443208A CN114045179A CN 114045179 A CN114045179 A CN 114045179A CN 202111443208 A CN202111443208 A CN 202111443208A CN 114045179 A CN114045179 A CN 114045179A
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- 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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
Abstract
A multiphase flow residual oil hydrogenation modification and catalytic cracking combined process adopts a suspension bed hydrogenation process to carry out hydrogenation modification on residual oil, metal elements and carbon residue in raw materials are removed to the maximum extent through shallow hydrogenation modification under the conditions of hydrogen and reaction, and reaction products are subjected to gas-liquid primary separation to obtain heavy distillate oil, light distillate oil and medium distillate oil; the medium distillate oil is a first-stage catalytic cracking raw material, the heavy distillate oil and a catalytic cracking reaction product enter a catalytic cracking fractionating tower together to complete the removal of catalyst or solid impurities and the separation of products, the products comprise a gas product, a gasoline fraction, a diesel oil fraction, recycle oil and oil slurry, wherein the recycle oil is returned as a second-stage catalytic cracking raw material, a small part of the oil slurry is discharged as fuel oil for use, and the rest of the oil slurry is returned as a suspension bed feed for secondary hydrogenation reaction. The invention also provides a corresponding system, realizes energy mutual supply and resource mutual use, and maximally improves the residual oil conversion rate and the clean oil yield.
Description
Technical Field
The invention belongs to the technical field of crude oil processing, and particularly relates to a multiphase flow residual oil hydro-upgrading and catalytic cracking combined process and system.
Background
With the increasing heaviness and deterioration of crude oil market supply, the high-efficiency conversion of heavy and inferior oil and the cleaning of products always become important power for promoting the technical level of petrochemical industry to be improved and the industry to be developed. Catalytic cracking and hydrocracking are important processing means for heavy and inferior oil conversion, and have an irreplaceable position in the field of heavy oil conversion. The catalytic cracking technology has the technical advantages of low investment, flexible operation, high reaction rate and the like, but has the problems of high raw material requirement, obvious coking, poor product property, low liquid yield, unavailable oil slurry and the like, and the product can meet the product index requirement only by carrying out secondary hydrogenation treatment. Therefore, the heavy and inferior oil is processed by adopting a residual oil hydrogenation technology and a catalytic cracking combined process technology at present, naphtha and diesel oil fractions are separated from reaction products of residual oil after hydrotreating, hydrogenated tail oil is used as a heavy oil catalytic cracking raw material, and recycle oil generated after catalytic cracking reaction is recycled to be refined or recycled to a residual oil hydrogenation device, but the heavy and inferior oil has the defects of low gasoline yield, large heat energy loss, high equipment investment and the like.
The hydrocracking technology of the suspended bed residual oil adopts a porous solid catalyst, has higher removal rate of carbon residue and heavy metal, and can remove certain impurity elements such as sulfur, nitrogen and the like, so the hydrocracking technology can be widely used for processing heavy and poor residual oil with high viscosity, high carbon residue, high metal and high impurity content, and has higher heavy oil conversion rate, liquid yield and lower coking rate. Can be combined with various processes such as catalytic cracking, wax oil hydrogenation, delayed coking and the like to produce clean fuel oil such as gasoline, diesel oil, ship fuel and the like and high value-added chemical products such as triphenyl triene and the like.
CN 102453543B discloses a residual oil hydrotreating and catalytic cracking combined process method, which adopts a fluidized bed hydrotreating process, wherein light components of reaction products enter the bottom of a riser reactor as a first-stage catalytic cracking feed, heavy components and catalytic cracking reaction products enter a catalytic cracking fractionating tower together, and dry gas, liquefied gas, gasoline fractions, diesel fractions, recycle oil and oil slurry are separated, wherein the recycle oil serves as a second-stage feed of the riser reactor, and the oil slurry serves as a delayed coking feed component.
US 6447671 discloses a combined process for the hydroconversion of heavy oils, in the process, heavy residual oil is subjected to a hydrocracking reaction in a fluidized bed, light fractions of reaction products enter a fixed bed hydrotreating section or directly enter a distillation device for narrow fraction cutting, heavy fractions are filtered out of catalyst solid residues through a filtering system and then enter the heavy oil fixed bed hydrogenation device, or all material flows flowing out from the fluidized bed hydrocracking reaction directly enter a heavy oil fixed bed hydrogenation device after passing through a filtering system, reaction products enter a distillation device, light fractions and heavy fractions are cut out, the heavy fraction enters a catalytic cracking device or is recycled to heavy oil hydrotreating or hydrocracking technology, the reasonable matching of processing means is carried out according to the feeding requirement of the device and the material flow property after reaction, the characteristics of the combined process technology are not fully exerted, and simultaneously the catalytic cracking slurry oil is not reasonably utilized.
US 6277270 discloses a process for treating heavy petroleum hydrocarbon feedstocks using a combination of fixed bed, ebullated bed hydrogenation and catalytic cracking processes, which separates a residual feedstock by vacuum distillation to obtain vacuum wax oil and vacuum residual oil, wherein all or part of the vacuum wax oil enters a fixed bed hydrogenation treatment device for reaction, the hydrogenated wax oil is distilled under normal pressure to obtain distillate oil and hydrogenated tail oil, wherein the vacuum residue oil directly or mixed with partial vacuum wax oil enters a fluidized bed device for hydrocracking reaction, the generated oil is distilled under normal pressure to obtain normal pressure distillate oil and normal pressure residue oil, wherein the atmospheric distillate oil is subjected to fixed bed hydrogenation reaction, the atmospheric residue oil is subjected to a fluidized bed hydrogenation device or is discharged as fuel oil, the combined process adopts the fluidized bed hydrocracking technology for the vacuum residue, and has the problems that the vacuum residue cannot be directly used as a raw material, the heavy oil conversion rate is low, the catalytic slurry oil is difficult to utilize and the like.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a multiphase flow residual oil hydro-upgrading and catalytic cracking combined process and system, so as to solve the problems that heavy and poor residual oil cannot be used as a catalytic cracking raw material or as a catalytic raw material, the coke production rate is high, catalytic cracking slurry oil is difficult to utilize and the like, greatly improve the flexibility of a catalytic cracking device, ensure the period stable operation of the device, simultaneously realize the synergistic interaction of two process technologies, greatly shorten the process flow and reduce the energy consumption of the device.
In order to achieve the purpose, the invention adopts the technical scheme that:
a multiphase flow residual oil hydro-upgrading and catalytic cracking combined process is characterized by comprising the following steps:
step 1, performing hydrogenation modification on residual oil by adopting a suspension bed hydrogenation process, wherein the catalyst is a multi-stage pore solid catalyst, metal elements and carbon residue in the raw materials are removed to the maximum extent through shallow hydrogenation modification under the conditions of hydrogen and reaction, the reaction product is subjected to two-stage separation to realize gas-liquid primary separation, wherein heavy distillate oil and light gas-liquid products are obtained through first-stage separation, the light gas-liquid products are the raw materials for second-stage separation, and light distillate oil, medium distillate oil and gas products are obtained through second-stage separation;
and 2, taking the medium distillate oil as a catalytic cracking primary raw material, feeding the heavy distillate oil and a catalytic cracking reaction product into a catalytic cracking fractionating tower, removing a catalyst or solid impurities and separating products in the catalytic cracking fractionating tower, wherein the products comprise a gas product, a gasoline fraction, a diesel oil fraction, recycle oil and oil slurry, the recycle oil is returned as a catalytic cracking secondary raw material, a small part of the oil slurry is discharged as fuel oil for use, and the rest of the oil slurry is returned as a suspension bed feed for secondary hydrogenation reaction.
The invention also provides a multiphase flow residual oil hydro-upgrading and catalytic cracking combined system, which comprises:
a feed tank for storing a residual oil feed;
the inlet of the suspension bed hydrogenation reactor is connected with the outlet of the raw material tank, and the suspension bed hydrogenation process is executed;
the inlet of the first-stage separator is connected with the outlet of the suspension bed hydrogenation reactor, and the reaction product of the suspension bed hydrogenation reactor is used as a raw material to carry out first-stage separation to obtain heavy distillate oil and light gas-liquid products;
the inlet of the second-stage separator is connected with the outlet of the first-stage separator, and the light gas-liquid product is used as a raw material to carry out second-stage separation to obtain light distillate oil, medium distillate oil and a gas product;
the inlet of the catalytic cracking riser reactor is connected with the outlet of the second-stage separation, and the catalytic cracking reaction is carried out by taking the middle distillate oil as the raw material;
a fractionating tower, the inlet of which is connected with the outlet of the catalytic cracking riser reactor, and the catalytic cracking reaction product and the heavy distillate oil are used as raw materials to remove catalyst or solid impurities and separate products, so as to obtain a gas product, a gasoline fraction, a diesel fraction, recycle oil and slurry oil; wherein the recycle oil returns to the catalytic cracking riser reactor to be used as a catalytic cracking second-stage raw material, the oil slurry is divided into circulating oil slurry and external throwing oil slurry, the circulating oil slurry returns to the raw material tank to be used as a suspension bed feed to carry out a secondary hydrogenation reaction, and the external throwing oil slurry is used as fuel oil.
The catalytic cracking riser reactor adopts a single riser or double risers, the medium distillate oil and the return oil are mixed or independently segmented as reaction raw materials, and the regenerator adopts one-segment or two-segment regeneration and is specifically determined according to the properties of the raw materials and the catalytic cracking feeding mode; the first-stage separator and the second-stage separator are high-pressure separators, flash towers or liquid-rotating separators; the suspension bed hydrogenation reactor at least comprises one reactor, when a plurality of reactors are arranged, the reactors are assembled in series or in parallel,
the system also comprises a circulating hydrogen compressor, wherein the inlet of the circulating hydrogen compressor is connected with the hydrogen outlet of the second-stage separator, and the outlet of the circulating hydrogen compressor is connected with the inlet of the suspension bed hydrogenation reactor.
Compared with the prior art, the invention has the beneficial effects that:
1. the combined process technology can effectively reduce the content of residual oil metal and carbon residue through the hydrogenation modification of the suspension bed, has better oil property generated by hydrogenation, is beneficial to improving the distribution and the product property of catalytic cracking products, and effectively solves the series problems of poor catalytic cracking raw material property, obvious coking, difficult oil slurry utilization and the like.
2. The combined process technology fully utilizes the high content of 2-4 ring polycyclic aromatic hydrocarbon in the catalytic slurry oil, can be used as a hydrogen donor with good suspension bed hydrogenation modification, effectively improves the residual oil hydrogenation conversion efficiency, simultaneously promotes the residual oil macromolecule cracking by a small amount of catalyst in the catalytic cracking slurry oil, and realizes the double promotion of the residual oil conversion and the liquid yield.
3. The combined process technology can fully exert the synergistic interaction of the combined process technology and the performance relay between two different types of reactions, realize the mutual use of raw materials, the heat complementation and the process coupling, simplify the process flow, and reduce the investment cost and the energy consumption of devices.
4. The invention can greatly improve the properties of the catalytic cracking raw materials by combining with the catalytic cracking process technology according to different properties of the hydrogenation modified product light distillate oil, medium distillate oil and heavy distillate oil, effectively ensures the service performance of the catalyst, finally reduces the coke yield, improves the liquid product yield, and provides favorable guarantee for the stable operation of the device.
In a word, the method optimally combines the hydrogenation modification of the residual oil in the suspension bed and the catalytic cracking process, fully exerts the synergistic interaction effect of the two technologies, not only effectively solves the problems that the heavy and poor residual oil has high sulfur nitrogen metal and carbon residue content and cannot be directly used as a catalytic cracking raw material, expands the raw material range, improves the product distribution and the product property, but also effectively solves the problems that the hydrogenation modified residual oil raw material in the suspension bed has low aromatic hydrocarbon content, poor colloid stability and residual oil hydrogenation effect and the like, realizes energy mutual supply and resource mutual use, and maximally improves the residual oil conversion rate and the clean oil product yield.
Drawings
FIG. 1 is a simplified diagram of a combined process flow of hydrogenation modification and catalytic cracking in a suspension bed.
1-a raw material tank; 2-a suspension bed hydrogenation reactor; 3-a reaction product; 4-a first stage separator; 5-heavy distillate oil; 6-light gas-liquid products; 7-a second stage separator; 8-light distillate oil; 9-medium distillate oil; 10-recycle hydrogen compressor; 11-a catalytic cracking riser reactor; 12-a catalytic cracking reaction product; 13-a fractionation column; 14-gaseous products; 15-gasoline fraction; 16-diesel fraction; 17-recycle oil; 18-circulating oil slurry; 19-external throwing slurry oil.
Detailed Description
The method and system provided by the present invention will be further described with reference to the accompanying drawings, but the present invention is not limited thereto.
As shown in fig. 1, the present invention provides a multiphase flow residue hydro-upgrading and catalytic cracking combined system, comprising:
a feed tank 1 for storing a residual oil feed; the heavy oil of which the residual oil is difficult to meet the requirement of catalytic cracking raw materials comprises one or a mixture of more of high sulfur nitrogen, high metal, high carbon residue, high viscosity and other heavy inferior oils such as atmospheric residual oil, vacuum residual oil, deoiled asphalt, coal tar, oil sand asphalt, delayed coking tail oil and steam cracking tar, and particularly high metal and high carbon residue residual oil.
And an inlet of the suspension bed hydrogenation reactor 2 is connected with an outlet of the raw material tank 1, and the suspension bed hydrogenation process is executed.
And an inlet of the first-stage separator 4 is connected with an outlet of the suspension bed hydrogenation reactor 2, and the reaction product 3 of the suspension bed hydrogenation reactor 2 is used as a raw material to carry out first-stage separation to obtain heavy distillate oil 5 and a light gas-liquid product 6.
And the inlet of the second-stage separator 7 is connected with the outlet of the first-stage separator 4, and the light gas-liquid product 6 is used as a raw material to carry out second-stage separation to obtain light distillate oil 8, medium distillate oil 9 and a gas product.
The catalytic cracking riser reactor 11 has an inlet connected to the outlet of the second stage separation, and the medium distillate oil 9 is used as the raw material for catalytic cracking reaction.
The inlet of the fractionating tower 13 is connected with the outlet of the catalytic cracking riser reactor 11, and the catalytic cracking reaction product 12 and the heavy distillate oil 5 are used as raw materials to remove catalyst or solid impurities and separate products, so as to obtain a gas product 14, a gasoline fraction 15, a diesel fraction 16, recycle oil 17 and slurry oil. Wherein the recycle oil 17 returns to the catalytic cracking riser reactor 11 to be used as a catalytic cracking second-stage raw material, the oil slurry is divided into a recycle oil slurry 18 and an external throwing oil slurry 19, the recycle oil slurry 18 returns to the raw material tank 1 to be used as a suspension bed feed for carrying out a secondary hydrogenation reaction, and the external throwing oil slurry 19 is used as fuel oil.
In the present invention, the catalytic cracking riser reactor 11 can adopt a single riser or a double riser, and the medium distillate oil 9 and the recycle oil 17 are mixed or separately segmented as reaction raw materials.
The first stage separator 4 and the second stage separator 7 are high pressure separators, flash towers, or hydrocyclone separators. The suspension bed hydrogenation reactor 2 at least comprises one reactor, and when the number of the reactors is multiple, the reactors are assembled in series or in parallel.
The invention also comprises a recycle hydrogen compressor 10, wherein the inlet of the recycle hydrogen compressor 10 is connected with the gas product outlet of the second-stage separator 7, the outlet is connected with the inlet of the suspension bed hydrogenation reactor 2, and the recycle hydrogen gas rich in hydrogen after the gas product is treated returns to the recycle hydrogen compressor 10.
Correspondingly, the multiphase flow residual oil hydro-upgrading and catalytic cracking combined process comprises the following two steps:
step 1, uniformly mixing a residual oil raw material and a solid catalyst in a raw material tank 1, boosting the pressure by a booster pump, mixing the mixture with hydrogen, entering a suspension bed hydrogenation modification reactor 2, and performing hydrogenation modification on the residual oil in the suspension bed hydrogenation reactor 2 by adopting a suspension bed hydrogenation process, wherein the catalyst is a multi-stage pore solid catalyst, one or more of iron oxyhydroxide, nickel oxide, cobalt oxide, tungsten oxide, molybdenum oxide and the like are used as active components, and a carrier is made of high-carbon-containing materials such as active carbon, coal powder, coke and the like and a carrierOne or more molecular sieves, and the addition amount of the catalyst is 0.3-2.0% of the weight of the raw material. Calculated by the weight of the catalyst, the content of the iron oxyhydroxide can be 15 to 49 percent, the content of the nickel oxide, the cobalt oxide, the molybdenum oxide or the tungsten oxide can be 1 to 20 percent, and the bulk density of the catalyst can be 0.68 to 0.69g/cm3The average particle diameter can be 65-75 μm, and the specific surface area can be 300-600m2/g。
Under the conditions of hydrogen temperature and reaction condition (working condition: reaction temperature 380--1The hydrogen-oil ratio is 800-2000 NL/kg; more preferred conditions are: the reaction temperature is 380--1And the hydrogen-oil ratio is 800-.
According to the method, a coking precursor and metal impurities are effectively adsorbed by utilizing the high specific area and pore volume of a catalyst through shallow hydrogenation modification, meanwhile, the content of the impurity elements such as sulfur, nitrogen and oxygen is reduced, the metal elements and carbon residue in the raw materials are removed to the maximum extent, the reaction product 3 is subjected to two-stage separation by a first-stage separator 4 and a second-stage separator 7 to realize gas-liquid primary separation, wherein the first-stage separation is used for obtaining heavy distillate oil 5 (higher than 480 ℃) and a light gas-liquid product 6, the light gas-liquid product 6 is used as a raw material for the second-stage separation, and the second-stage separation is used for obtaining light distillate oil 8 (lower than 365 ℃), medium distillate oil 9 (365-. Wherein the light distillate oil 8 is less and is a mixed component of gasoline (<205 ℃) or gasoline and diesel oil fractions (<365 ℃), and can be taken as a gasoline and diesel oil blending component or a hydrofining raw material to be discharged out of a device; the medium distillate oil 9 is wax oil fraction, and the hydrogen can be returned to the recycle hydrogen compressor 10 to be compressed and then used as suspension bed feed to carry out secondary hydrogenation reaction.
And 2, utilizing equipment such as a catalytic cracking riser reactor 11 and the like to perform catalytic cracking by taking the medium distillate oil 9 as a catalytic cracking first-stage raw material (the working condition is that the reaction temperature is 480-550 ℃, the bottom temperature is 500-560 ℃, the upper section temperature is 480-530 ℃, the regeneration temperature is 670-780 ℃ (preferably 650-750 ℃), the catalyst-oil ratio is 4-15 (preferably 4-8), the reaction time is 0.5-3.0s (preferably 0.6-2.0s), and the pressure is 0.1-0.3MPa), wherein the catalyst adopts a conventional molecular sieve or an alumino silicate catalyst, preferably an industrial catalyst taking ZSM-5, Y-type, USY-type and other molecular sieves as auxiliaries and alumino silicate as a carrier.
The heavy distillate oil 5 and the catalytic cracking reaction product 12 enter a catalytic cracking fractionating tower 13 together, the removal of catalyst or solid impurities and the separation of products are finished in a catalytic cracking fractionating tower 13, the products comprise gas products 14 (dry gas and liquefied gas), gasoline fraction 15, diesel oil fraction 16, recycle oil 17 and oil slurry, wherein the gas product 14, the gasoline fraction 15 and the diesel oil fraction 16 enter a tank area, the recycle oil 17 contains a large amount of medium distillate oil, the recycle oil is returned to be used as a second-stage raw material of catalytic cracking for hydrocracking reaction, the oil slurry is discharged from the bottom of a fractionating tower, a small part of the oil slurry is discharged as an external throwing oil slurry 19 to be used as fuel oil, most of the other oil slurry is the circulating oil slurry 18, and the circulating oil slurry is returned to be used as the suspension bed feed for carrying out secondary hydrogenation reaction, so that the conversion efficiency and the liquid yield of the residual oil are greatly improved, the yield of dry gas and coke is reduced, and the series problems that the oil slurry of a catalytic cracking device is difficult to utilize, the conversion rate of the residual oil hydrogenated in the suspension bed is low and the like are effectively solved.
The medium distillate oil 9 as the first-stage catalytic cracking raw material can enter the bottom of a riser together with the recycle oil 17, or can independently serve as riser feeding to enter the upper section of the riser.
The properties of the feedstock used in the examples of the present invention are shown in table 1, and the catalyst was independently developed using a porous carbon material supported Fe-Ni catalyst of the catalyst used for the suspension bed hydro-upgrading, wherein the catalyst contained 13.85% of Fe, 0.8% of Ni, and a specific surface area of 523m2The average particle diameter in the catalyst is 73 mu m, and the weight percent is the mass fraction.
Comparative example
The method takes the feeding components of the circulating material of the catalytic slurry oil without residual oil hydro-upgrading as a comparative example, so that the technical advantages of the invention are highlighted for convenience of comparison, and the catalytic cracking process conditions, the catalyst and the feeding mode are kept unchanged.
TABLE 1 Properties of the stock oils
TABLE 2 suspension bed residuum upgrading and catalytic cracking process conditions
Examples
In this embodiment, the flow chart of the combined method and process system of suspension bed hydro-upgrading and catalytic cracking provided by the present invention is shown in fig. 1, wherein after the hydro-upgrading liquid phase product is separated in two stages by a thermal high-fraction separator and a thermal low-fraction separator, the light distillate oil below 200 ℃ can be used as gasoline blending component or hydrorefining raw material, and can be specifically determined according to the properties of the raw material; 200-420 ℃ middle distillate oil can be used as a catalytic cracking raw material; and (3) the heavy distillate oil with the temperature of more than 420 ℃ and the catalytic cracking product enter a catalytic cracking fractionating tower together, the recycle oil returns to the catalytic cracking riser tube for continuous reaction, and the catalytic oil slurry is circulated to be used as the hydrogenation modified solvent oil of the residual oil of the suspension bed to participate in secondary conversion. Table 2 shows the process conditions and product distribution.
The comparison result shows that the residual oil after hydrogenation modification in the suspension bed has greatly reduced content of carbon residue, metals, sulfur, nitrogen, oxygen and impurities, and compared with the residual oil directly used as the catalytic cracking raw material, the liquid yield is 89.9%, the liquid yield is improved by 6.7%, the coke yield is reduced by 3.11%, and the dry gas yield is reduced by 1.4%.
Therefore, the method can well solve the series problems that the yield of coke is high when the high-carbon residue and high-metal content residual oil is used as the raw material of the catalytic cracking device, the long-period stable operation of the device is difficult to ensure, and the like.
Claims (10)
1. A multiphase flow residual oil hydro-upgrading and catalytic cracking combined process is characterized by comprising the following steps:
step 1, performing hydrogenation modification on residual oil by adopting a suspension bed hydrogenation process, wherein the catalyst is a multi-stage pore solid catalyst, metal elements and carbon residue in the raw materials are removed to the maximum extent through shallow hydrogenation modification under the conditions of hydrogen and reaction, the reaction product is subjected to two-stage separation to realize gas-liquid primary separation, wherein heavy distillate oil and light gas-liquid products are obtained through first-stage separation, the light gas-liquid products are the raw materials for second-stage separation, and light distillate oil, medium distillate oil and gas products are obtained through second-stage separation;
and 2, catalytically cracking the medium distillate oil serving as a catalytic cracking primary raw material, feeding the heavy distillate oil and a catalytic cracking reaction product into a catalytic cracking fractionating tower, removing a catalyst or solid impurities and separating products in the catalytic cracking fractionating tower, wherein the products comprise a gas product, a gasoline fraction, a diesel oil fraction, recycle oil and oil slurry, the recycle oil is returned as a catalytic cracking secondary raw material, a small part of the oil slurry is discharged as fuel oil, and the rest of the oil slurry is returned as a suspension bed feed to perform a secondary hydrogenation reaction.
2. The combined process of hydroupgrading and catalytic cracking of multiphase flow residue according to claim 1, wherein the residue is one or more of atmospheric residue, vacuum residue, deoiled asphalt, coal tar, oil sand asphalt, delayed coking tail oil and steam cracking tar, the catalyst takes one or more of iron oxyhydroxide, nickel oxide, cobalt oxide, tungsten oxide and molybdenum oxide as an active component, the carrier takes one or more of active carbon, coal powder and coke, and the addition amount of the catalyst is 0.3-2.0% of the weight of the raw material feed.
3. The combined process of hydroupgrading and catalytic cracking of multiphase flow residue according to claim 2, wherein the iron oxyhydroxide is 15-49% by weight of the catalyst, the nickel oxide, cobalt oxide, molybdenum oxide or tungsten oxide is 1-20% by weight of the catalyst, and the bulk density of the catalyst is 0.68-0.69g/cm3The average particle diameter is 65-75 μm, the specific surface area is 300-2/g。
4. The combined process of hydroupgrading and catalytic cracking of multiphase flow residue according to claim 1, wherein the suspension bed hydrogenation process is operated under the following conditions: the reaction temperature is 380--1The hydrogen-oil ratio is 800-2000 NL/kg.
5. The combined process of hydroupgrading and catalytic cracking of multiphase flow residue according to claim 1, wherein in the step 1, the light distillate oil is gasoline and diesel oil fraction which can be used as gasoline and diesel oil blending component or hydrofining raw material, and the gas product obtained from the second stage of separation is returned as suspension bed feed for secondary hydrogenation reaction.
6. The combined multiphase flow residuum hydro-upgrading and catalytic cracking process of claim 1, characterized in that in step 2, the catalyst is a conventional molecular sieve or alumino silicate catalyst.
7. The combined process of hydro-upgrading and catalytic cracking of multiphase flow residue according to claim 1 or 6, wherein in the step 2, the catalytic cracking conditions are as follows: the reaction temperature is 480-550 ℃, the regeneration temperature is 670-780 ℃, the catalyst-oil ratio is 4-15, the reaction time is 0.5-3.0s, and the pressure is 0.1-0.3 MPa.
8. A multiphase flow residue hydro-upgrading and catalytic cracking combined system is characterized by comprising:
a feed tank for storing a residual oil feed;
the inlet of the suspension bed hydrogenation reactor is connected with the outlet of the raw material tank, and the suspension bed hydrogenation process is executed;
the inlet of the first-stage separator is connected with the outlet of the suspension bed hydrogenation reactor, and the reaction product of the suspension bed hydrogenation reactor is used as a raw material to carry out first-stage separation to obtain heavy distillate oil and light gas-liquid products;
the inlet of the second-stage separator is connected with the outlet of the first-stage separator, and the light gas-liquid product is used as a raw material to carry out second-stage separation to obtain light distillate oil, medium distillate oil and a gas product;
the inlet of the catalytic cracking riser reactor is connected with the outlet of the second-stage separation, and the catalytic cracking reaction is carried out by taking the middle distillate oil as the raw material;
a fractionating tower, the inlet of which is connected with the outlet of the catalytic cracking riser reactor, and the catalytic cracking reaction product and the heavy distillate oil are used as raw materials to remove catalyst or solid impurities and separate products, so as to obtain a gas product, a gasoline fraction, a diesel fraction, recycle oil and slurry oil; wherein the recycle oil returns to the catalytic cracking riser reactor to be used as a catalytic cracking second-stage raw material, the oil slurry is divided into circulating oil slurry and external throwing oil slurry, the circulating oil slurry returns to the raw material tank to be used as a suspension bed feed to carry out a secondary hydrogenation reaction, and the external throwing oil slurry is used as fuel oil.
9. The combined system for hydroupgrading of multiphase flow residue and catalytic cracking according to claim 8, wherein the catalytic cracking riser reactor adopts a single riser or a double riser, the medium distillate oil and the return oil are mixed or separately segmented as reaction raw materials, and the regenerator adopts one-stage or two-stage regeneration; the first-stage separator and the second-stage separator are high-pressure separators, flash towers or liquid-rotating separators; the suspension bed hydrogenation reactor at least comprises one reactor, and when the number of the reactors is multiple, the reactors are assembled in series or in parallel.
10. The combined system for hydroupgrading and catalytic cracking of multiphase flow residue according to claim 8, further comprising a recycle hydrogen compressor, wherein an inlet of the recycle hydrogen compressor is connected to the gas product outlet of the second stage separator, and an outlet of the recycle hydrogen compressor is connected to the inlet of the suspension bed hydrogenation reactor.
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| CN115475622A (en) * | 2022-08-24 | 2022-12-16 | 宁波中金石化有限公司 | Preparation method and application of slurry bed hydrogenation catalyst based on waste porcelain powder carrier |
| CN115491232A (en) * | 2022-10-13 | 2022-12-20 | 陕西延长石油（集团）有限责任公司 | Method for producing ultralow-sulfur marine fuel oil by low-pressure hydrogenation of heavy and poor-quality residual oil |
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| CN111420671A (en) * | 2020-04-07 | 2020-07-17 | 延安大学 | Coal tar suspension bed hydrocracking catalyst and preparation method thereof |
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| CN101724463A (en) * | 2008-10-29 | 2010-06-09 | 中国石油化工股份有限公司 | Combined process method for performing hydro-cracking and catalytic cracking on suspension bed residual oil |
| CN102453543A (en) * | 2010-10-15 | 2012-05-16 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and catalytic cracking for residuum |
| CN102876377A (en) * | 2011-07-11 | 2013-01-16 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking combined method of heavy hydrocarbon raw material |
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| CN111420671A (en) * | 2020-04-07 | 2020-07-17 | 延安大学 | Coal tar suspension bed hydrocracking catalyst and preparation method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115475622A (en) * | 2022-08-24 | 2022-12-16 | 宁波中金石化有限公司 | Preparation method and application of slurry bed hydrogenation catalyst based on waste porcelain powder carrier |
| CN115475622B (en) * | 2022-08-24 | 2023-08-25 | 宁波中金石化有限公司 | Preparation method and application of slurry bed hydrogenation catalyst based on waste porcelain powder carrier |
| CN115491232A (en) * | 2022-10-13 | 2022-12-20 | 陕西延长石油（集团）有限责任公司 | Method for producing ultralow-sulfur marine fuel oil by low-pressure hydrogenation of heavy and poor-quality residual oil |
| CN115491232B (en) * | 2022-10-13 | 2024-01-23 | 陕西延长石油（集团）有限责任公司 | Method for producing ultralow-sulfur marine fuel oil by low-pressure hydrogenation of heavy inferior residual oil |
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| CN114045179B (en) | 2023-04-11 |
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