CN1184281C - A kind of catalytic cracking method that adopts double-path feed agent casing type reactor - Google Patents

Abstract

A kind of catalytic cracking method that adopts dual-path inlet casing reactor comprises the following steps: (1) catalyst enters the inner pipe of the sleeve reactor and the annular ring between the inner pipe and the outer pipe through the double-path catalyst inlet pipe respectively. (2) The hydrocarbon oil raw material is injected into the inner tube of the reactor and the annular space between the inner tube and the outer tube, and contacts and reacts with the catalyst, and the reactant flows along the The wall of the device continues to flow upward; (3) The reactant flow in the inner pipe and the annular space between the inner pipe and the outer pipe merges at the inlet of the confluence pipe, and enters the gas-solid rapid separation equipment through the confluence pipe, so that the reaction oil gas and the After the reaction, the carbon-deposited catalyst phase is separated; (4) The reaction oil gas is sent to the subsequent separation system, and the reacted catalyst is stripped and regenerated, and then returned to the reactor for recycling.

Description

A kind of catalytic cracking method that adopts dual-path feed agent casing type reactor

technical field

The invention belongs to a method for catalytic cracking of petroleum hydrocarbons in the absence of hydrogen, more specifically, it is a method for catalytic cracking of hydrocarbon oil by adopting a double-path feed agent jacketed reactor.

Background technique

Although the catalytic cracking process has experienced decades of development and formed a relatively complete technical system, refiners are still conducting unremitting research and exploration, hoping that the process can not only meet the requirements of increasingly stringent environmental regulations Requirements, and can adapt to changes in market demand, creating good economic benefits for enterprises.

Both USP5043522 and USP5846403 are improvements to conventional catalytic cracking processes. They allow part of the catalytic gasoline to be injected into the riser reactor from the upstream of the raw oil feed nozzle, and contact and react with the high-temperature, high-activity regenerated catalyst to increase the production of light olefins such as propylene and butene, and at the same time increase the octane number of gasoline .

CN1279270A discloses a method for simultaneously increasing the production of liquefied gas and diesel. In this method, the catalytic gasoline is also injected into the riser reactor from the upstream of the raw material oil feed nozzle, so that it first contacts and reacts with the regenerated catalyst. This part of the re-refined catalytic gasoline is fully cracked under high temperature and high fuel ratio to generate a large amount of liquefied gas, and at the same time, a small amount of coke is deposited on the catalyst, which appropriately reduces the activity of the catalyst and is conducive to producing more diesel.

USP3894933 has introduced a kind of catalytic cracking method of double riser reactor that shares a settler. The method is to inject the light cycle oil into a riser reactor, contact and react with the regenerated catalyst, and make the conversion rate less than 30%; the reacted catalyst enters another riser, and contacts with fresh raw materials and heavy cycle oil ,reaction.

CN1069054A proposes a flexible and multi-effect hydrocarbon catalytic cracking method. The method involves two independent riser reactors and two settling separation systems connected with the riser. In the first riser reactor, the light hydrocarbons react with the regenerated catalyst at 600-700°C, the ratio of solvent to oil is 10-40, and the reaction time is 2-20 seconds, and the carbon content of the catalyst is controlled to be 0.1 ~0.4% by weight; the reacted catalyst enters another riser, contacts with heavy hydrocarbons, and reacts under conventional catalytic cracking reaction conditions.

In summary, the catalytic conversion methods for simultaneous processing of light oil and heavy oil disclosed in the background technology can basically be divided into the following two categories: (1) using a single riser reactor and setting the light oil inlet at Upstream of heavy oil inlet; (2) Double riser reactor is adopted, so that different risers can process different raw materials. The equipment of the first type of method has little modification, but the reaction conditions of light oil are basically relatively fixed. It is difficult to improve the product distribution and product properties through the optimization of operating parameters. The second method overcomes the shortcomings of the first method. The operating conditions of each riser can be adjusted independently, so that different raw oils can react under their respective suitable conditions. But for the second type of method, both the construction cost of the device and the transformation cost of the equipment will increase significantly. In addition, in the actual industrial production process, due to the complexity of the process, the operation difficulty of the device will be increased a lot.

Contents of the invention

The object of the present invention is to: provide a kind of catalytic cracking method that adopts dual-path feed agent jacketed reactor, this method can create suitable reaction conditions for hydrocarbon oil raw materials of different properties, and make the product distribution and the product of catalytic cracking process properties are improved.

Method provided by the invention comprises the following steps:

(1) The catalyst enters the inner tube of the sleeve reactor and the annular reaction space between the inner tube and the outer tube through the double-channel catalyst inlet pipe, and flows upward under the action of the pre-lift medium;

(2) The hydrocarbon oil raw material is injected into the inner pipe of the reactor and the annular space between the inner pipe and the outer pipe, contacts and reacts with the catalyst, and the reactant flow continues to flow upward along the wall;

(3) The reactant flow in the inner pipe and the annular space between the inner pipe and the outer pipe merges at the entrance of the confluence pipe, and enters the gas-solid rapid separation equipment through the confluence pipe, so that the reaction oil gas and the catalyst of carbon deposition after the reaction phase separation;

(4) The reaction oil gas is sent to the subsequent separation system, and the reacted catalyst is stripped and regenerated, and then returned to the reactor for recycling.

Compared with the prior art, the beneficial effects of the present invention are mainly reflected in the following aspects:

The method provided by the invention has simple equipment and flexible operation. Not only heavy oil and light oil can be reacted in the same reactor, but also the reaction conditions can be flexibly adjusted according to the physical and chemical properties of raw materials and mass flow rate, thus creating favorable conditions for improving product distribution and product quality.

The method provided by the invention can realize the flexible adjustment of various production schemes, for example, gasoline scheme, diesel scheme, liquefied gas scheme and the like. Using this method, oil refining enterprises can adjust product structure in time according to changes in market demand, and obtain more significant economic benefits.

In addition, the method provided by the invention can also improve product quality and reduce environmental pollution caused by petroleum products. It is proved by experiments that this method can reduce the olefin content of gasoline and increase the octane number of gasoline; reduce the freezing point of diesel oil, improve the sensitivity of diesel oil to flow modifiers, and improve the stability of diesel oil; The content of impurities such as nitrogen has a certain effect.

Description of drawings

Fig. 1 is a structural schematic diagram of a double-channel feed casing type catalytic cracking reactor according to the present invention.

2 to 4 are principle flowcharts of the method provided by the present invention.

Detailed ways

The structure of the jacketed reactor of the present invention is shown in FIG. 1 . The reactor mainly includes the following components: catalyst inlet pipes 21 and 22, inner pipe 5, outer pipe 6, confluence pipe 8, pre-lift distribution rings 1 and 3, and feed nozzles 2 and 4; wherein, inner pipe 5 and outer pipe 6 are coaxial, and the ratio of the cross-sectional area of the core of the inner tube to the cross-sectional area of the inner and outer tube annulus is 1:0.1 to 10; the catalyst inlet pipe 21 is connected to the lower end of the inner tube 5, and the length of the inner tube accounts for the total length of the reactor The distance from the lower end of the outer tube 6 to the lower end of the inner tube 5 accounts for 2% to 20% of the total length of the reactor, and the catalyst inlet pipe 22 is connected to the lower end of the outer tube 6; one end of the confluence tube 8 is connected to the outer tube 6 The upper end is connected, while the other end is connected with the gas-solid separation device 9, the ratio of the cross-sectional area of the confluence pipe 8 to the inner pipe 5 is 1:0.2-0.8; the pre-lift distribution rings 1 and 3 are located in the inner pipe and the inner, The bottom of the annular space between the outer tubes; the feed nozzles 2 and 4 are located at the lower part of the inner and outer tubes, respectively. The reactor has applied for a utility model patent, the application number is 01264042.5.

In the method provided by the present invention, the catalysts respectively entering the inner tube of the sleeve reactor and the annular reaction space between the inner tube and the outer tube through the dual catalyst inlet tubes may be the same or different. Specifically, the catalyst that enters the inner tube of the jacketed reactor and the annular reaction space between the inner tube and the outer tube can be the high-temperature regenerant from the regenerator, or the regenerant and the spent agent and/or A mixture of semi-regenerated agents; or the regenerated catalyst can enter the inner tube of the jacketed reactor, while the semi-regenerated catalyst, spent catalyst or their mixture enters the annular reaction space between the inner tube and the outer tube, and vice versa. In a word, the catalyst entering the dual catalyst inlet pipe can be comprehensively considered and flexibly adjusted according to factors such as device conditions, raw material properties, and target product requirements. In addition, the catalyst entering the jacketed reactor can also be cooled by a catalyst cooler, or the catalyst mixing tank can be used to fully mix the regenerated agent with the spent agent and/or semi-regenerated agent, and then enter the jacketed reactor through the catalyst inlet pipe. reactor.

The catalyst used in the present invention can be any catalyst suitable for the catalytic cracking process, and its active components can be selected from Y-type or HY-type zeolite containing or not containing rare earth and/or phosphorus, or containing or not containing rare earth and/or phosphorus One, two or three of ultra-stable Y-type zeolite, ZSM-5 series zeolite or silica zeolite with five-membered ring structure, beta zeolite, ferrierite, or amorphous silica-alumina catalyst.

In the method provided by the present invention, the bottom of the jacketed reactor, the bottom of the inner tube, and the bottom of the annular reaction space between the inner tube and the outer tube are all provided with a pre-lifting medium. The pre-lift medium can be steam, dry gas or their mixture. The superficial linear velocity of gas in the inner tube is 0.3-6.0m/s, and the superficial linear velocity of gas in the annular space between the inner and outer tubes is 0.2-8.0m/s.

The hydrocarbon oil feedstock injected into the inner pipe and the annular space between the inner pipe and the outer pipe is selected from: primary processed gasoline fraction, secondary processed gasoline fraction, primary processed diesel fraction, secondary processed diesel fraction, straight run wax oil, coker wax Oil, deasphalted oil, hydrorefined oil, hydrocracking tail oil, vacuum wax oil, vacuum residue or atmospheric residue or a mixture of more than one. The raw material of hydrocarbon oil injected into the inner pipe is preferably: one of straight-run wax oil, coker wax oil, deasphalted oil, hydrorefined oil, hydrocracking tail oil, vacuum wax oil, vacuum residue or atmospheric residue a mixture of one or more species. The hydrocarbon oil raw material injected into the annular space between the inner pipe and the outer pipe is preferably: one or more mixtures of primary processed gasoline fraction, secondary processed gasoline fraction, primary processed diesel fraction, and secondary processed diesel fraction.

The reaction conditions of the hydrocarbon oil raw material in the inner tube are as follows: reaction temperature 460-580°C, preferably 480-550°C; reaction pressure 0.1-0.6MPa, preferably 0.2-0.4MPa; agent-to-oil ratio 3-15, preferably 4-10; The residence time of the inner tube is 1.0-10 seconds, preferably 1.5-5.0 seconds; the temperature before the catalyst contacts with the hydrocarbon oil is 620-720°C, preferably 650-700°C; the atomizing steam is 1-15% by weight (accounting for the raw material) , preferably 2 to 10% by weight.

The reaction conditions of the hydrocarbon oil raw material in the annular space between the inner pipe and the outer pipe are as follows: reaction temperature 300-680°C, preferably 400-600°C; reaction pressure 0.1-0.6MPa, preferably 0.2-0.4MPa; agent-to-oil ratio 2 ~30, preferably 4~20; the residence time of oil and gas is 0.5 ~ 20 seconds, preferably 1 ~ 15 seconds; atomized steam 1 ~ 15% by weight (accounting for raw materials), preferably 1 ~ 10% by weight. The reaction conditions of the hydrocarbon oil raw material in the annular space between the inner tube and the outer tube can be further optimized according to the properties of the hydrocarbon oil raw material and the requirements of the target product. When liquefied gas or light olefins are used as the main target product, relatively harsh reaction conditions can be adopted, for example, reaction temperature 530-680 ℃, agent-oil ratio 8-30, oil-gas residence time 5-20 seconds, etc.; And/or diesel as the main target product, relatively mild operating conditions should be adopted, for example, reaction temperature 300-540°C, agent-to-oil ratio 2-8, oil-gas residence time 1-5 seconds, etc.

The oil agent mixture in the inner pipe and the annular space between the inner pipe and the outer pipe is mixed at the inlet of the confluence pipe, and the reaction oil and gas continue to react in the confluence pipe. The reaction time is 0.1 to 3.0 seconds. It depends on the reaction conditions of the inner tube and the annular space, generally, the reaction temperature is 450-600°C, the agent-oil ratio is 4-12, the reaction pressure is 0.1-0.6MPa, and the weight ratio of water vapor to hydrocarbon oil is 0.01-0.10 : 1.

The method provided by the present invention will be further described below in conjunction with the accompanying drawings, but the present invention is not limited thereto.

As shown in Figure 2, the regenerated catalyst enters the inner pipe 5 and the annular reaction space between the inner pipe 5 and the outer pipe 6 of the double-way feed agent jacketed reactor through catalyst inlet pipes 21 and 22 respectively, and in the pre-lifting medium under the action of upward flow. The hydrocarbon oil feedstock is injected into the inner tube of the reactor and the annular space between the inner tube and the outer tube through nozzles 2 and 4 respectively, and contacts and reacts with the catalyst, and the mixture of reaction oil gas and catalyst flows upward along the wall of the reactor. The reactant flows in the inner pipe and the annular space between the inner pipe and the outer pipe merge at the inlet of the confluence pipe 8, and enter the settler 12 through the confluence pipe and the gas-solid rapid separation equipment. In the settler, the reaction oil gas is separated from the carbon-deposited catalyst after the reaction. The reacted oil gas enters the subsequent separation system 14, and is further separated into various products. The reacted catalyst falls into the stripper 13, and the reaction oil gas carried by the catalyst is stripped under the action of water vapor. The stripped catalyst is sent to the regenerator 15 for coke regeneration, and the regenerated catalyst is returned to the reactor for recycling.

As shown in Figure 3, the regenerated catalyst enters the bottom of the inner tube 5 of the jacketed reactor through the catalyst inlet tube 21, and flows upward under the action of the pre-lift medium. The semi-regenerated catalyst flows into the annular reaction space between the inner pipe 5 and the outer pipe 6 through the catalyst inlet pipe 22, and flows upward under the action of the pre-lift medium. The hydrocarbon oil feedstock is injected into the inner tube of the reactor and the annular space between the inner tube and the outer tube through nozzles 2 and 4 respectively, and contacts and reacts with the catalyst, and the mixture of reaction oil gas and catalyst flows upward along the wall of the reactor. The reactant flows in the inner pipe and the annular space between the inner pipe and the outer pipe merge at the inlet of the confluence pipe 8, and enter the settler 12 through the confluence pipe and the gas-solid rapid separation equipment. In the settler, the reaction oil gas is separated from the carbon-deposited catalyst after the reaction. The reaction oil gas enters the follow-up separation system 14, and is further separated into various products, and the reacted catalyst falls into the stripper 13, and the reaction oil gas carried by the catalyst is stripped under the action of water vapor; 23 and 24 are regenerated by charring, and the regenerated catalyst and part of the semi-regenerated catalyst are returned to the inner tube of the reactor and the annular reaction space between the inner tube and the outer tube for recycling.

As shown in Figure 4, the regenerated catalyst enters the bottom of the inner tube 5 of the jacketed reactor through the catalyst inlet tube 21, and flows upward under the action of the pre-lift medium. Part of the spent catalyst flows into the annular reaction space between the inner pipe 5 and the outer pipe 6 through the catalyst inlet pipe 22, and flows upward under the action of the pre-lift medium. The hydrocarbon oil feedstock is injected into the inner tube of the reactor and the annular space between the inner tube and the outer tube through nozzles 2 and 4 respectively, and contacts and reacts with the catalyst, and the mixture of reaction oil gas and catalyst flows upward along the wall of the reactor. The reactant flows in the inner pipe and the annular space between the inner pipe and the outer pipe merge at the inlet of the confluence pipe 8, and enter the settler 12 through the confluence pipe and the gas-solid rapid separation equipment. In the settler, the reaction oil gas is separated from the carbon-deposited catalyst after the reaction. The reaction oil gas enters the follow-up separation system 14, and is further separated into various products, and the reacted catalyst falls into the stripper 13, and the reaction oil gas carried by the catalyst is stripped under the action of water vapor; Part of it enters the regenerator 15 to burn and regenerate, and the regenerated catalyst returns to the bottom of the inner tube for recycling; the rest of the unregenerated catalyst is directly returned to the bottom of the annular reaction space between the inner tube and the outer tube for recycling.

In addition to the flow process shown in the above-mentioned Figures 2 to 4, in the method provided by the present invention, the regenerated catalyst, spent catalyst, semi-regenerated catalyst or a mixture of any two of them entering the reactor can be cooled by a catalyst cooler and then Enter the bottom of the jacketed reactor through the catalyst inlet pipe.

The following examples will further illustrate the method provided by the present invention, but the present invention is not limited thereto.

The catalyst used in the examples is industrially produced by the Catalyst Factory of Lanzhou Petroleum Refinery and Chemical Plant, and the trade name is LV-23. See Table 2 for its main properties. The hydrocarbon oil raw material used in the examples is Daqing VGO mixed with 30 wt% VR, and its properties are shown in Table 1. The test device used in the examples is a multifunctional small-scale riser catalytic cracking device.

Example 1

This embodiment illustrates: when adopting the method provided by the invention, and using diesel oil as the main target product, the obtained test results.

The main test steps are as follows: as shown in Figure 2, the raw oil shown in Table 1 is mixed with the re-refined oil of this device, heated by the preheating furnace, injected into the inner tube of the sleeve reactor, and mixed with the regenerated catalyst from the regenerator touch, react. Coking diesel raw materials (density 0.8520g/cm ³ , sulfur content 8225ppm, nitrogen content 5018ppm, cetane number 47) and naphtha fraction produced by this device are mixed and injected into the annular reaction space between the inner tube and the outer tube, It contacts and reacts with another stream of regenerant from the regenerator that has been cooled by the heat exchanger. The oil mixture in the inner pipe and the oil mixture in the annular reaction space respectively go up along the wall of the vessel. The above two streams are mixed with each other at the inlet of the confluence pipe, continue to react, and enter the settler through the confluence pipe. In the settler, the reaction oil gas is separated from the reacted catalyst, and the oil gas enters the subsequent fractionation system through the oil gas pipeline, and is further separated into various products. The resulting products are metered and analyzed separately. After being stripped by steam, the raw catalyst is sent to the regenerator to be burnt for regeneration, and the regenerated catalyst is returned to the reactor for recycling.

The main operating conditions are shown in Table 3, the product distribution is shown in Table 4, and the main product properties are shown in Table 5. As can be seen from Table 4 and Table 5, when diesel oil is used as the main target product, the present invention can make the yield of diesel oil reach 40.02% by weight and the total liquid yield reach 89.69% by weight under lower dry gas and coke yields . Since the inner tube adopts a higher reaction temperature and a shorter reaction time, it is beneficial to the cracking of heavy raw materials. The annular reaction space adopts a lower reaction temperature. When the flow in the annular reaction space contacts the flow in the inner tube, it acts as a quenching effect on the flow in the inner tube, terminating the secondary cracking of the middle distillate. Thus, the method provided by the present invention results in the desired product distribution as described above.

Example 2

This embodiment illustrates: when adopting the method provided by the present invention, and using liquefied petroleum gas and diesel oil as the main target products, the experimental results obtained.

The main test steps are as follows: As shown in Figure 2, the raw material oil shown in Table 1 is injected into the inner tube of the sleeve reactor after being heated by the preheating furnace as a fresh material, and is lifted from the catalyst inlet tube and lifted by the pre-lifting medium. The regenerated catalyst contacts and reacts. The gasoline fraction produced by the device is injected into the annular reaction space between the inner pipe and the outer pipe, and contacts and reacts with the regeneration agent inside. The oil mixture in the inner pipe and the oil mixture in the annular reaction space go up the wall respectively, mix with each other at the entrance of the confluence pipe, continue to react, and enter the settler. In the settler, the reaction oil gas is separated from the reacted catalyst, and the oil gas enters the subsequent fractionation system through the oil gas pipeline, and is further separated into various products. The resulting products are metered and analyzed separately. After being stripped by steam, the raw catalyst is sent to the regenerator to be burnt for regeneration, and the regenerated catalyst is returned to the reactor for recycling.

The main operating conditions are shown in Table 3, the product distribution is shown in Table 4, and the main product properties are shown in Table 5. As can be seen from Table 4 and Table 5, when liquefied gas and diesel oil are used as the main target products, the present invention can make the liquefied gas yield reach 17.45% by weight and the diesel yield under lower dry gas and coke yields. It reached 22.87% by weight, and the total light hydrocarbon liquid yield reached 77.95% by weight.

Comparative ratio

This example illustrates the test results obtained when a conventional two-stage riser reactor is used and liquefied gas and diesel are used as the main target products.

The main test steps are as follows: using the same feed oil and catalyst as in Example 2. The preheated raw oil is injected into the upper section of the riser reactor (ie, the second-stage riser), and contacts and reacts with the stream reaction oil gas and catalyst from the lower section of the riser reactor (ie, the first-stage riser). The gasoline fraction produced by this device is injected into a section of riser to contact and react with the regenerated catalyst from the regenerator. The oil agent mixture in the first-stage riser goes up to the second-stage riser, and the mixture of total oil gas and catalyst in the second-stage riser enters the settler. In the settler, the reaction oil gas is separated from the reacted catalyst, and the oil gas enters the subsequent fractionation system through the oil gas pipeline, and is further separated into various products. The resulting products are metered and analyzed separately. After being stripped by steam, the raw catalyst is sent to the regenerator to be burnt for regeneration, and the regenerated catalyst is returned to the reactor for recycling.

The main operating conditions are shown in Table 3, the product distribution is shown in Table 4, and the main product properties are shown in Table 5. As can be seen from Table 3, compared with the method of the present invention, the one-stage riser in the conventional two-stage riser reactor has very harsh light oil cracking conditions, the ratio of agent to oil is large, the temperature is high, and there is overcracking in the light oil; However, the heavy feed oil in the second-stage riser comes into contact with the carbon-deposited catalyst after the cracked light oil, the catalytic reaction is affected, and the heavy oil conversion capacity is obviously insufficient. As can be seen from Table 4, compared with Example 2, under similar reaction conditions, the gas and coke in the conventional reactor are more, indicating that the naphtha cracked back to refinement is excessive; The cracking ability of high-quality raw materials is relatively weak.

Table 1 Raw oil name Daqing VGO mixed with 30% VR Density (20°C), g/cm ³ Refractive Index (70°C), Kinematic Viscosity, mm ² /s, 80°C, 100°C Freezing Point, °C Aniline Point, °C Residual Carbon, Weight % 0.88811.478431.8818.09＞50112.92.7 Four components, weight % saturated aromatic hydrocarbon colloid asphaltenes 62.125.212.60.1 Elemental composition, wt% CHSNBr, gBr/100g 85.7413.010.130.202.8 Metal content, ppmFeNiCuVNa 2.33.0<0.10.12.6 Distillation range, °C initial boiling point 5% 10% 30% 50% 339388421473526 characteristic factor 12.7

Table 2 catalyst LV-23 Chemical composition, weight % Al ₂ O ₃ Na ₂ ORE ₂ O ₃ 51.20.322.0 Physical properties Specific surface area, m ² /g pore volume, ml/g bulk density, g/cm ³ wear index, %h ^-1 sieve composition, V% 0～20μm0～40μm0～80μm0～110μm0～149μm average particle size, μm 2280.390.701.73.219.268.581.896.366.8 medium aging condition 800℃/15h/100% steam aging agent 61

table 3 Test No. Example 1 Example 2 comparative example reactor Sleeve Reactor Sleeve Reactor Conventional Segmented Riser target product diesel fuel Liquefied petroleum gas + diesel Liquefied petroleum gas + diesel Operation method Heavy Oil Refining Operations Heavy oil one-way operation Heavy oil one-way operation Inner tube: raw material amount of raw material oil, g/h reaction temperature, ℃ agent-oil ratio reaction time, s atomized water, weight % heavy oil recovery ratio Fresh material + back to refining 8765087.51.077.80.30 Fresh material 11075005.11.615.90 Second stage riser: fresh material 1010////0 Annular reaction space: raw material oil light oil amount, g/h light oil ratio (accounting for fresh raw material), weight % reaction temperature, ℃ agent-oil ratio reaction time, s atomized water (accounting for light oil), weight % Coking diesel oil + catalytic naphtha 135+15032.54208.70.918.3 Catalytic naphtha 25122.757411.90.848.5 A riser: catalytic naphtha 23723.562026.00.796.5 Merging pipe: reaction temperature, ℃ agent-oil ratio reaction time, s water-oil ratio, weight % 4787.80.457.9 5036.30.576.3 Second stage riser 5016.12.326.4

Table 4 Test No. Example 1 Example 2 comparative example plan diesel fuel Liquefied petroleum gas + diesel Liquefied petroleum gas + diesel Material balance, weight % dry gas 2.26 2.52 2.97 liquefied gas 10.15 17.45 18.29 gasoline 39.52 37.63 34.55 diesel fuel 40.02 22.87 22.21 heavy oil 0 14.06 15.92 coke 8.05 5.47 6.06 total 100.00 100.00 100.00 Conversion rate, weight % 59.98 63.07 61.87 Light oil yield ^* , wt% 79.54 60.50 57.76 Total light hydrocarbon liquid yield ^* , wt% 89.69 77.95 75.05

*Light Oil Yield = Gasoline Yield + Diesel Yield

Total light hydrocarbon liquid yield = liquefied gas yield + gasoline yield + diesel yield

table 5 Gasoline properties density (20°C) g/cm ³ actual gum, mg/100ml diene value, gI ₂ /100g induction period, minS, ppmN, ppm octane number (measured) RONMON alkane content, v% olefin content, v % aromatics content, v% Example 10.720441.05101967890.979.437.841.720.5 Example 20.727740.95621126090.279.142.538.918.6 Comparative example 0.730231.15701065590.278.943.437.219.4 Diesel properties density, g/cm ³ freezing point, ℃ cetane number S, m% N, m% initial boiling point, ℃ 90% distillation, ℃ 0.8723-737.80.320.03201329 0.8836-1240.20.160.02202331 0.8812-841.00.170.03205333

Claims (7)

1, a kind of catalytic cracking method that adopts two-way inlet agent casing reactor, it is characterized in that the method may further comprise the steps: (1) The catalyst enters the inner tube of the sleeve reactor and the annular reaction space between the inner tube and the outer tube through the double-channel catalyst inlet pipe, and flows upward under the action of the pre-lift medium; (2) The hydrocarbon oil raw material is injected into the inner pipe of the reactor and the annular space between the inner pipe and the outer pipe, contacts and reacts with the catalyst, and the reactant flow continues to flow upward along the wall; (3) The reactant flow in the inner pipe and the annular space between the inner pipe and the outer pipe merges at the inlet of the confluence pipe, and enters the gas-solid rapid separation equipment through the confluence pipe, so that the oil gas and the carbon-deposited catalyst after the reaction are phased separation; (4) The oil and gas are sent to the subsequent separation system, and the reacted catalyst is stripped and regenerated, and returned to the reactor for recycling; Wherein, the hydrocarbon oil raw material injected into the inner pipe is selected from: straight-run wax oil, coker wax oil, deasphalted oil, hydrorefined oil, hydrocracking tail oil, vacuum wax oil, vacuum residue or conventional One or more than one mixture of pressed residue oil; and the hydrocarbon oil raw material injected into the annular space between the inner pipe and the outer pipe is selected from: primary processing gasoline fraction, secondary processing gasoline fraction, primary processing diesel fraction, secondary A mixture of one or more than one of secondary processed diesel oil fractions; the reaction conditions of the inner tube of the hydrocarbon oil raw material are as follows: reaction temperature 460-580°C, reaction pressure 0.1-0.6MPa, agent-to-oil ratio 3-15, The residence time of the oil and gas in the inner pipe is 1.0-10 seconds, the temperature before the contact between the catalyst and the hydrocarbon oil is 620-720°C, and the atomized steam is 1-15% by weight; the hydrocarbon oil raw material is between the inner pipe and the outer pipe The reaction conditions in the annular space are as follows: reaction temperature 300-680°C, reaction pressure 0.1-0.6MPa, agent-to-oil ratio 2-30, oil-gas residence time 0.5-20 seconds, atomized steam 1-15% by weight; The reactor mainly includes the following components: two-way catalyst inlet pipe (21, 22), inner pipe (5), outer pipe (6), confluence pipe (8), pre-lift distribution ring (1, 3) and inlet Material nozzles (2, 4); wherein, the inner pipe (5) is coaxial with the outer pipe (6), and the ratio of the cross-sectional area of the core of the inner pipe to the cross-sectional area of the annulus of the inner and outer pipes is 1:0.1-10; A catalyst inlet pipe (21) in the road catalyst inlet pipe is connected to the lower end of the inner pipe (5), and the length of the inner pipe accounts for 10% to 70% of the total length of the reactor; the lower end of the outer pipe (6) to the inner pipe (5) The distance of the lower end accounts for 2 to 20% of the total length of the reactor, and another catalyst inlet pipe (22) in the double-way catalyst inlet pipe is connected with the lower end of the outer pipe (6); one end of the confluence pipe (8) is connected with the outer pipe (6) The upper end is connected, and the other end is connected with the gas-solid separation equipment (9), the ratio of the cross-sectional area of the tube core of the confluence tube (8) and the inner tube (5) is 1: 0.2～0.8; the pre-lifting distribution ring ( 1) and (3) are respectively located at the bottom of the inner pipe and the annular space between the inner and outer pipes; the feed nozzles (2) and (4) are respectively located at the lower part of the inner pipe and the outer pipe; The superficial linear velocity of gas in the inner tube is 0.3-6.0 m/s, and the superficial linear velocity of gas in the annular space between the inner and outer tubes is 0.2-8.0 m/s. 2. According to the method of claim 1, it is characterized in that the catalysts in the inner pipe and the annular reaction space between the inner pipe and the outer pipe respectively entering the double-path catalyst inlet pipe of the sleeve reactor are selected from: regeneration agent, semi-regenerated agent, mixture of regenerated agent and semi-regenerated agent, mixture of spent agent and regenerated agent and/or semi-regenerated agent. 3. The method according to claim 2, characterized in that the catalyst entering the jacketed reactor through any one of the two-way catalyst inlet pipes is cooled by a catalyst cooler. 4. The method according to claim 1, characterized in that the active component of the catalyst is selected from Y-type or HY-type zeolite containing or not containing rare earth and/or phosphorus, ultrastable zeolite containing or not containing rare earth and/or phosphorus One, two or three of Y-type zeolite, ZSM-5 zeolite or silica zeolite with five-membered ring structure, beta zeolite and ferrierite. 5. The method according to claim 1, characterized in that the reaction conditions of the hydrocarbon oil raw material in the inner pipe are as follows: reaction temperature 480-550°C, reaction pressure 0.2-0.4MPa, agent-oil ratio 4-10, oil and gas The residence time of the tube is 1.5-5.0 seconds, the temperature before the catalyst contacts with the hydrocarbon oil is 650-700°C, and the atomizing steam is 2-10% by weight. 6. The method according to claim 1, characterized in that the reaction conditions of the hydrocarbon oil raw material in the annular space between the inner pipe and the outer pipe are as follows: reaction temperature 400-600°C, reaction pressure 0.2-0.4MPa, agent The oil ratio is 4-20, the residence time of oil and gas is 1-15 seconds, and the atomized steam is 1-10% by weight. 7. According to the method of claim 1, it is characterized in that the reaction conditions of the reactant flow in the confluence pipe in the step (3) are: reaction temperature 450～600°C, reaction pressure 0.1～0.6MPa, reaction time 0.1～3.0 seconds .

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