53results about How to "Increased total liquid recovery" patented technology

The present invention is catalytically cracking co-catalyst for raising diesel oil yield and its preparation process. The co-catalyst is prepared with sprayed microballoon containing kaolin, pseudo boehmite and water galss, and through high temperature roasting over 900 deg.c, extraction with sodium hydroxide or other strong alkali to form pore channels, and final supporting phosphorus and RE oxide. The co-catalyst contains phosphorus in 1-3.5 wt%, RE oxide in 1-5 wt%, no zeolite component and sodium oxide less than 0.6 wt%. Adding certain amount of the co-catalyst into FCC catalyzing apparatus can raise diesel oil yield, improve product distribution and raise the utilization rate of available catalyst.

A cracking catalyst containing modified beta zeolite comprises 10 wt%-80 wt% of Y zeolite, 1-50 wt% of the modified beta zeolite, 5-70 wt% of clay and 5-60 wt% of a heat-resistant inorganic oxide; theanhydrous chemical expression formula of the modified beta zeolite is(0-0.2)Na2O.(0.5-15)MO2.(0.5-15)RE2O3.(0.5-15)Al2O3(60-98). SiO2 on the basis of oxide mass, wherein M is one or two substances selected from group IVB metals. The preparation method of the catalyst comprises mixing and beating of the Y zeolite, the modified beta zeolite, the clay, the heat resistant inorganic oxide, a binder and water and spraying drying. The catalyst has strong heavy oil cracking ability and high total liquid yield, and propylene in liquefied gas has high concentration.

A delay coking process able to flexible regulate the circualting ratio operation features that part of the circulating oil in reaction oil vapour of coking tower is separated out by the coking fractionation tower and then proportionally mixed with the raw material of coking tower. Its advantages are flexible regulation, high total liquid output, and high quality of coker wax oil.

The invention discloses a method and a device for gasoline upgrading, mainly solving the problems of high yield of dry gas and coke and low liquid recovery during the gasoline upgrading reaction in the double-riser catalytic cracking device, high energy consumption of the device and low desulphurization efficiency. The method is mainly characterized by the steps as follows: some of the regenerated catalysts returning to the heavy oil riser reactor; some of the regenerated catalysts mixing with the recycled catalysts from the rapid bed reactor in the catalysts mixer before contacting with the gasoline of poor quality and entering part I of the gasoline riser reactor, the rapid bed reactor, and the part II of the gasoline riser reactor; reactants flowing into a second settler for separation; upgrading reaction oil and gas entering the fractionation system for fractionating; spent catalysts entering the regenerators for coke burning regenerating. The invention can reduce dry gas and coke yield and improve the total liquid yield and meanwhile decrease the energy consumption of the whole device.

The invention relates to a preparation method and application of a catalytic cracking metal passivant. The preparation method comprises the following steps of: preparing raw materials in the following percentage by weight: 20%-45% of dispersing agents, 30%-50% of oxidants, 15%-30% of metal oxides, 10%-30% of solvents and 2%-5% of stabilizing agents; sequentially adding the oxidants and the metal oxides to the dispersing agents during preparation; increasing temperature to 50-90 DEG C within 2-4 hours, keeping the temperature for 1-5 hours and then cooling; adding the solvents and the stabilizing agents, and then filtering to remove impurities so as to obtain the metal passivant, wherein the dispersing agents are diethanol amine and / or triethanol amine; the oxidants are hydrogen peroxide of 30-50 percent and / or nitric acids of 66-68 percent; the metal oxides are one of diantimony trioxide, rare earth oxides and bismuth oxides or mixtures of more than two of the diantimony trioxide, the rare earth oxides and the bismuth oxides in any proportion; the solvents are one of water or alcohol solvents or mixtures of more than two of the water or the alcohol solvents in any proportion; and the stabilizing agents are methylcellulose compound solutions.

The invention discloses a cracking catalyst containing metallic oxide modified beta zeolite. The cracking catalyst comprises the following ingredients by taking the weight of the cracking catalyst as a standard in percentage by weight: 10-80% of Y type zeolite, 1-50% of the metallic oxide modified beta zeolite, 5-70% of clay and 5-60% of heat-resisting inorganic oxide; based on mass of oxide, the anhydrous chemical expression of the metallic oxide modified beta zeolite is as follows: (0-0.2)Na2O.(0.5-15)ZrO2.(0-10) MxOy. (0.5-15) Al2O3.(60-97)SiO2, wherein M is one selected from Ti, Cr, Fe and Ga; x refers to atomic number of M, and y refers to a number meeting the requirement of M oxidation state. The preparation method of the catalyst comprises the steps of mixing and pulping the Y type zeolite, the metallic oxide modified beta zeolite, the clay, the heat-resisting inorganic oxide binder and water, and carrying out spray drying. The catalyst is high in heavy oil cracking capacity, and high in yield of total liquid yield and liquefied gas; the propylene concentration in the liquefied gas is obviously improved.

A petroleum hydrocarbon catalytic cracking catalyst comprises a carrier, a Y-type molecular sieve, a mesoporous molecular sieve with a M41S structure and a molecular sieve with a pore opening diameterof 0.59-0.73 nanometer. The Y-type molecular sieve comprises an ultra-stable Y-type molecular sieve containing phosphorus and rare earth, the total pore volume of the Y-type molecular sieve is 0.33-0.39 ml / g, the pore volume of secondary pores of 2-100 nm accounts for 10-25% of the total pore volume, the unit cell constant is 2.440-2.455 nm, the proportion of non-framework aluminum content to thetotal aluminum content is not higher than 20%, the lattice collapse temperature is not lower than 1050 DEG C, and the ratio of B acid content to L acid content measured by pyridine adsorption infrared method at 200 DEG C is not lower than 2.50. The catalyst has high heavy oil conversion activity, good coke selectivity, high gasoline yield, liquefied gas yield, light oil yield and total liquid yield.

The invention relates to an imidazoline derivative with the structure general formula (I), wherein R represents an organic acid alkyl chain with the general formula of -CnHm, n is an integer larger than or equal to 12, and m is equal to 2n-1; R' represents an amido with the general formula of -(CH2CH2NH)n-1H, and n is an integer larger than or equal to 2. The invention also relates to a preparation method of the imidazoline derivative with the structure general formula (I), compounds with the general formulas (II) and (III) which are respectively prepared by adopting the imidazoline derivative as a raw material and modified carboxylic acid or ethylene oxide and a petroleum refining auxiliary agent. The invention has favorable atomization effect and corrosion resistance, and the crude oil can be fully emulsified in petroleum refinement to improve the atomization effect of a nozzle, inhibit colloid generation and reduce the generation of deposited carbon on catalyst, thereby being beneficial to reducing the dry gas and improving total liquid yield, reducing the performance requirement on equipment and prolonging the service life of the equipment.

A petroleum hydrocarbon catalytic cracking catalyst comprises a carrier, a Y-type molecular sieve, a mesoporous molecular sieve with a M41S structure and a molecular sieve with a pore opening diameterof 0.59-0.73 nanometer. The Y-type molecular sieve comprises an ultra-stable Y-type molecular sieve containing rare earth, the total pore volume is 0.33-0.39 ml / g, the pore volume of secondary poreswith pore diameters of 2-100 nm accounts for 10-25% of the total pore volume, the unit cell constant is 2.440-2.455 nm, the proportion of non-framework aluminum content to the total aluminum content is not higher than 20%, the lattice collapse temperature is not lower than 1050 DEG C, and the ratio of B acid content to L acid content measured by pyridine adsorption infrared method at 200 DEG C isnot lower than 2.50. The catalyst has high heavy oil conversion activity, good coke selectivity, high gasoline yield, liquefied gas yield, light oil yield and total liquid yield.

The invention provides a catalytic cracking catalyst. The catalytic cracking catalyst contains clay, alumina containing an additive and a modified Y type molecular sieve. The modified Y type molecularsieve comprises 5 to 12 wt% of rare earth and no more than 0.5 wt% of sodium oxide, and has a total pore volume of 0.36 to 0.48 mL / g; the pore volume of secondary pores accounts for 20 to 38% of thetotal pore volume; a lattice constant is 2.440 nm to 2.455 nm; the content of non-framework aluminum is no more than 10% of total aluminum content; lattice collapse temperature is higher than 1060 DEGC; and a ratio of the amount of acid B to the amount of acid L is no less than 3.50. A preparation method for the catalytic cracking catalyst comprises the following steps: preparing a rare earth-containing Y type molecular sieve with a conventional cell size; carrying out roasting in a water vapor atmosphere with a temperature of 350 to 520 DEG C and a volume percentage of 30 to 95% for 4.5 to 7h; carrying out a contact reaction with silicon tetrachloride; and carrying out acid treatment. The catalytic cracking catalyst has higher heavy oil conversion activity, low coke selectivity, and higher gasoline yield, liquefied gas yield, light oil yield and total liquid yield.

The invention discloses a heavy oil catalytic cracking catalyst, a preparation method of the heavy oil catalytic cracking catalyst and a heavy oil catalytic cracking method. The heavy oil catalytic cracking catalyst contains a molecular sieve and a carrier, wherein the carrier contains clay, aluminum oxide and silicon dioxide, and the weight ratio of the molecular sieve to the carrier is (0.136-0.37):1; the catalyst is prepared from the following components in percentage by weight: 40-55wt% of clay, 20-30wt% of aluminum oxide, 12-27wt% of molecular sieve and 5-10wt% of silicon dioxide. According to the heavy oil catalytic cracking catalyst, the weight ratio of molecular sieve to the carrier is appropriate, the catalyst has strong heavy oil cracking ability and high conversion rate, the total liquid yield is improved, the light toil yield is improved, the production rate of dry gas and liquefied gas is reduced and the coke has good selectivity.

The invention relates to a high-stability modified Y-type molecular sieve and a preparation method thereof, wherein the modified Y-type molecular sieve contains 5-12 wt% of RE2O3 and 0.1-0.7 wt% of Na2O, and has the total pore volume of 0.33-0.39 mL / g, the pore volume of the secondary pores with the pore size of 2-100 nm accounts for 10-25% of the total pore volume, the unit cell constant is 2.440-2.455 nm, the non-framework aluminum content is not more than 20% of the total aluminum content, the lattice collapse temperature is not below 1050 DEG C, and the pyridine adsorption infrared methoddetermination results show that a ratio of the amount of B acid to the amount of L acid is not less than 2.50. The preparation method comprises: ion exchange, modification treatment at a certain temperature under water vapor conditions, and reaction with silicon tetrachloride. According to the present invention, the modified Y-type molecular sieve has advantages of high heavy oil conversion activity, low coke selectivity, high diesel yield, high liquefied gas yield, high light-oil yield and high total liquid recovery.

The invention relates to a super-stable Y-type molecular sieve containing phosphorus and rare earth, wherein the Y-type molecular sieve contains 4-11 wt% of rare earth, 0.05-10 wt% of phosphorus and 0.1-0.7 wt% of sodium oxide, and has the pore volume of 0.33-0.39 mL / g, the pore volume of the pores with the pore size of 2-100 nm accounts for 15-30% of the total pore volume, the unit cell constantis 2.440-2.455 nm, the non-framework aluminum accounts for less than 20% of the total aluminum, the lattice collapse temperature is more than 1050 DEG C, and a ratio of the amount of B acid to the amount of L acid is not less than 2.50. The preparation method comprises: preparing a rare earth-containing Y-type molecular sieve having a conventional unit cell size, calcining for 4.5-7 h at a temperature of 350-480 DEG C under 30-90% by volume of steam atmosphere, carrying out phosphorus modification treatment, and carrying out a contact reaction with silicon tetrachloride gas. According to the present invention, the Y-type molecular sieve has advantages of good hydrothermal stability, high heavy oil conversion activity, low coke selectivity, high heavy oil conversion diesel yield, high liquefied gas yield and high total liquid recovery.

A cracking catalyst containing modified beta zeolite comprises 10 wt%-80 wt% of Y zeolite, 1-50 wt% of the modified beta zeolite, 5-70 wt% of clay and 5-60 wt% of a heat-resistant inorganic oxide; theanhydrous chemical expression formula of the modified beta zeolite is(0-0.2)Na2O.(0.5-15)MO2.(0.5-15)RE2O3.(0.5-15)Al2O3(60-98). SiO2 on the basis of oxide mass, wherein M is one or two substances selected from group IVB metals. The preparation method of the catalyst comprises mixing and beating of the Y zeolite, the modified beta zeolite, the clay, the heat resistant inorganic oxide, a binder and water and spraying drying. The catalyst has strong heavy oil cracking ability and high total liquid yield, and propylene in liquefied gas has high concentration.

A cracking catalyst containing modified beta zeolite comprises, by weight, 10-80% of Y type zeolite, 1-50% of modified beta zeolite, 5-70% of clay and 5-60% of heat-resistant inorganic oxide. The anhydrous chemical expression of the modified beta zeolite is, by mass of oxide, (0-0.2)Na2O.(0.5-15)ZrO2.(0-10)MxOy.(1-10)P2O5.(0.5-15)Al2O3.(60-98)SiO2, wherein M is one or more of Ti, Cr, Fe and Ga, x refers to the atomicity of M, y refers to a number required by the oxidation state of M. A preparation method of the catalyst includes the step that Y type zeolite, modified beta zeolite, clay, heat-resistant inorganic oxide, adhesive and water are mixed, pulped, sprayed and dried. The catalyst is high in hydrocarbon cracking capacity, high in liquefied gas yield and high in propylene concentration in liquefied gas.

The invention provides a catalytic cracking catalyst and a preparation method thereof, the catalyst is prepared from 15-60 wt% of molecular sieve, 15-60 wt% of clay, 10-30 wt% of pseudoboehmite, 5-20wt% of adhesive, 0.1-5 wt% of phosphorus-containing compound (calculated by P), 0.1-3 wt% of magnesium-containing compound (calculated by Mg), and may also contain 0-5 wt% of rare earth oxide. The preparation method comprises the following steps: (1) catalyst forming: mixing and pulping molecular sieve, clay, pseudoboehmite, phosphorus-containing compound and adhesive; then adding magnesium-containing compound to mix and pulp, heating and stirring, spraying and forming, and roasting to obtain the formed catalyst; (2) catalyst modification: mixing and pulping the formed catalyst, ammonium salt,phosphorus-containing compound and water, adjusting pH, heating and reacting, and filtering and drying to obtain the catalytic cracking catalyst of the invention. The catalytic cracking catalyst provided by the invention has the characteristics of low coke yield and high total liquid collection (liquefied gas, gasoline and diesel).

The invention discloses a low-coking type catalytic cracking catalyst and a preparation method thereof. The catalyst contains a mesoporous-macroporous silicon-aluminum material, in terms of the weightof oxide, the anhydrous chemical expression of the mesoporous-macroporous silicon-aluminum material is (0-0.3)Na2O:(2-18)Al2O3:(82-98)SiO2, the pore volume of the mesoporous-macroporous silicon-aluminum material is 0.8-2 mlg<-1>, the specific surface area is 150-350 m<2>g<-1>, the most probable aperture is 30-100 nm, and the B / L acid ratio is 0.8-2.0; and the catalyst also contains a phosphorus and rare earth modified Y-type molecular sieve, the molecular sieve contains, in percentage by weight, 0.8-4.0 wt% of RE2O3 and 0.5-5.0 wt% of P, the crystal cell is 2.435-2.442 nm, and the crystallinity is 45-55%. The catalyst has the characteristics of being high in total liquid yield and low in coke yield.

A delay coking process able to flexible regulate the circualting ratio operation features that part of the circulating oil in reaction oil vapour of coking tower is separated out by the coking fractionation tower and then proportionally mixed with the raw material of coking tower. Its advantages are flexible regulation, high total liquid output, and high quality of coker wax oil.

An ultra-stable Y-type molecular sieve containing phosphorus and rare earth and a preparation method thereof. The Y-type molecular sieve contains 4 to 11 wt% rare earth, 0.05 to 10 wt% phosphorus, 0.1 to 0.7 wt% sodium oxide, and has a pore volume of 0.33 to 0.39 mL / g, the volume of 2-100nm pores accounts for 15-30% of the total pore volume, the unit cell constant is 2.440-2.455nm, non-framework aluminum accounts for less than 20% of the total aluminum, the lattice collapse temperature is greater than 1050°C, and the B acid content The ratio to the amount of L acid is not less than 2.50. The preparation method includes: preparing a Y-type molecular sieve with a conventional unit cell size containing rare earth, roasting it for 4.5-7 hours in an atmosphere of 350-480°C and 30-90 volume % water vapor, phosphorus modification treatment and mixing with silicon tetrachloride gas. Contact reaction steps. The Y-type molecular sieve has good hydrothermal stability, high heavy oil cracking activity, good coke selectivity, and high yields of heavy oil converted into gasoline, liquefied gas and total liquid.

The invention discloses a catalytic cracking method and device. The method is characterized by comprising the following steps: introducing raw oil into bottom of a riser reactor to contact and react with a catalyst from a catalyst heat exchanger; separating oil gas after the reaction from a coked catalyst; introducing separated reaction oil gas into a fractionating tower; carrying out steam stripping on the separated coked catalyst and sending the coked catalyst into a regenerator for regeneration; sending part of the regenerated catalyst into the riser reactor from different height positions of the riser; and carry out heat transfer on the other part of the regenerated catalyst by a heat exchanger and entering the other part of the regenerated catalyst into bottom of the riser reactor. The method of the invention can lower total yield of dry gas and coke by 0.5-1.5 percentage, increase total liquid yield of liquefied gas, gasoline and diesel by more than 1 percentage, and reduce gasoline olefin volume content by 5-15 percentage.

The invention discloses a catalytic cracking method and a catalytic cracking device. According to the invention, raw oil enters the lower part of a riser reactor, and is subjected to a contact reaction with a catalyst from a catalyst pre-lift mixer; oil gas obtained after reaction is separated from spent catalyst; reaction oil gas obtained by separation is delivered into a fractionating tower, and the separated spent catalyst is regenerated; part of high-temperature regenerated catalyst after regeneration enters an external heat remover; part of cooled regenerated catalyst is delivered back to the regenerator, another part of the cooled regenerated catalyst enters the catalyst pre-lift mixer, and a third part of the cooled regenerated catalyst enters the riser reactor from different height positions of the riser. The method provided by the invention can be used for reducing dry gas and coke total yield. A total liquid yield is increased by more than 1.5 percentage points; gasoline olefin volume content is reduced by 5-15 percentage points; and SOx content in flue gas is reduced by more than 30%.

Belonging to the technical field of catalytic cracking for petroleum refining, the invention relates to a method for reducing emission of carbon dioxide in catalytic cracking flue gas. The method comprises the steps of: conducting emulsification to a catalytic cracking raw material under the conditions of normal pressure, an emulsification of 45-90DEG C, a water adding amount of 1%-10%, a multifunctional composite emulsifier adding amount of 0.01%-2%, and a stirring speed of 15000-20000r / min, and subjecting the emulsified raw oil to direct catalytic reaction as a catalytic material. After emulsification of a heavy oil catalytic cracking raw material, the atomization degree and dispersibility of catalytic charged material are improved, and particle sizes of charged droplets are greatly reduced, thus reaching the purposes of enhancing light oil yield and total liquid yield, lowering coke yield so as to reduce the content of carbon dioxide in flue gas.

The invention relates to a method for emulsification continuous feeding of a heavy oil weight catalytic cracking raw material, comprising the following steps of: mixing and emulsifying the catalytic cracking raw material, a compound emulsifier and water; and directly introducing emulsified emulsifying oil into a catalytic device for catalytic reaction, wherein the emulsifying is carried out at normal pressure and the temperature of 50-95 DEG C, the water adding quantity accounts for 1-15% of the mass of the emulsifying oil, the adding quantity of the compound emulsifier accounts for 0.01-2% of the mass of the emulsifying oil, and the stirring speed is more than 15,000r / min. In the invention, the emulsified emulsifying oil as the catalytic raw material is directly introduced into the catalytic device for catalytic reaction without utilizing a buffer oil tank in the middle process, the dwell time after emulsification is short and the emulsion breaking problem is unavailable. After the heavy oil catalytic cracking raw material is emulsified, the dispersity and the atomization degree of the catalytic cracking feeding are improved, the atomization efficiency is enhanced, the particle diameter of feeding oil drop is greatly reduced, an oiling agent is ensured to be effectively contacted, the cracking depth is increased, and the purposes of enhancing the yield of light weight oil and the total liquid yield and reducing the yield of coke can be achieved.

The invention provides a catalytic cracking catalyst. The catalytic cracking catalyst contains clay, an alumina binder and a modified Y type molecular sieve. The modified Y type molecular sieve comprises 5 to 12 wt% of rare earth and no more than 0.5 wt% of sodium oxide, and has a total pore volume of 0.36 to 0.48 mL / g; the pore volume of secondary pores accounts for 20 to 38% of the total pore volume; a lattice constant is 2.440 nm to 2.455 nm; the content of non-framework aluminum is no more than 10% of total aluminum content; lattice collapse temperature is higher than 1060 DEG C; and a ratio of the amount of acid B to the amount of acid L is no less than 3.50. A preparation method for the catalytic cracking catalyst comprises the following steps: preparing a rare earth-containing Y type molecular sieve with a conventional cell size; carrying out roasting in a water vapor atmosphere with a temperature of 350 to 520 DEG C and a volume percentage of 30 to 95% for 4.5 to 7 h; carryingout a contact reaction with silicon tetrachloride; and carrying out acid treatment. The catalyst has higher heavy oil conversion activity, low coke selectivity, and higher gasoline yield, liquefied gas yield, light oil yield and total liquid yield.

The invention discloses a catalytic cracking method and device. The method comprises the following steps: introducing raw oil into a lower part of a riser reactor to contact and react with a catalyst from a catalyst heat exchanger; separating oil gas after the reaction from a coked catalyst; introducing separated reaction oil gas into a fractionating tower; carrying out steam stripping on the separated coked catalyst and sending the coked catalyst into a regenerator for regeneration; carrying out heat transfer and cooling on the regenerated catalyst and part of system prevailing wind within the catalyst heat exchanger; sending part of the regenerated catalyst into the riser reactor from different heights of the riser; and sending the other part of the regenerated catalyst into the lower part of the riser reactor. The method can reduce total yield of dry gas and coke by 0.8-2 percentage, increase total liquid yield of liquefied gas, gasoline and diesel by 1.2 percentage, and reduce volume content of gasoline olefin by 5-15 percentage.

A rare earth-containing modified Y-type molecular sieve rich in secondary pores and a preparation method thereof. The Y-type molecular sieve has a rare earth content of 5 to 12% by weight, a sodium content of no more than 0.5% by weight, and a total pore volume of 0.36 to 0.48 mL. / g, the secondary pore volume accounts for 20~38% of the total pore volume, the unit cell constant is 2.440~2.455nm, the non-framework aluminum content accounts for less than 10% of the total aluminum content, the lattice collapse temperature is higher than 1060°C, B acid The ratio of the amount to the amount of L acid is not less than 3.50. The preparation method includes: preparing a Y-type molecular sieve with a conventional unit cell size containing rare earths, roasting it for 4.5 to 7 hours in an atmosphere of 350 to 520°C and 30 to 95 volume % water vapor, contacting with silicon tetrachloride gas and treating with acid. A step of. The modified Y-type molecular sieve has higher heavy oil conversion activity and lower coke selectivity, and has higher gasoline yield, liquefied gas yield, light oil yield and total liquid recovery.

A catalytic cracking catalyst containing clay, alumina containing additives and modified Y-type molecular sieve. The modified Y-type molecular sieve contains 5 to 12% by weight of rare earths, no more than 0.5% by weight of sodium oxide, and a total pore volume of 0.36 to 0.36% by weight. 0.48mL / g, the secondary pore volume accounts for 20~38% of the total pore volume, the unit cell constant is 2.440~2.455nm, non-framework aluminum accounts for less than 10% of the total aluminum, the lattice collapse temperature is higher than 1060℃, B acid The ratio of the amount to the amount of L acid is not less than 3.50. The preparation method includes: preparing a Y-type molecular sieve with a conventional unit cell size containing rare earths, roasting it for 4.5 to 7 hours in an atmosphere of 350 to 520°C and 30 to 95 volume % water vapor, contacting with silicon tetrachloride gas and treating with acid. . The catalytic cracking catalyst has higher heavy oil conversion activity and lower coke selectivity, and has higher gasoline yield, liquefied gas yield, light oil yield and total liquid yield.

The invention discloses a low-coking catalytic cracking catalyst and a preparation method thereof. The catalyst contains medium and macroporous silicon-aluminum materials, and its anhydrous chemical expression is: (0-0.3)Na based on the weight of oxides. 2 O:(2‑18)Al 2 o 3 :(82‑98)SiO 2 ; its pore volume is 0.8‑2mlg ‑1 , the specific surface area is 150‑350m 2 g ‑1 , the most probable pore size is 30-100nm, the B / L acid ratio is 0.8-2.0; the catalyst also contains phosphorus and rare earth modified Y-type molecular sieves, and the molecular sieves contain RE in weight percent 2 o 3 is 0.8-4.0wt%, P is 0.5-5.0wt%, the unit cell is 2.435-2.442nm, and the crystallinity is 45-55%. The catalyst of the invention has the characteristics of high total liquid yield and low coke yield.