A catalytic conversion process and system for producing low carbon olefins and light aromatics from crude oil

Abstract

The present application provides a catalytic conversion method for producing low-carbon olefins and light aromatics from crude oil, comprising: S1, flashing the crude oil to obtain light distillate oil and heavy distillate oil; contacting the light distillate oil with a first catalyst in a downflow bed reactor to obtain a first semi-regenerated agent; S2, introducing a second catalyst and the first semi-regenerated agent into a riser reactor from the bottom and the middle, respectively; and introducing the heavy distillate oil from the bottom into the riser reactor to sequentially contact the second catalyst and the first semi-regenerated agent, and performing a second catalytic conversion reaction to obtain a second oil agent mixture; S3, introducing the second oil agent mixture into a catalyst separation device for separation; S4, performing gas-solid separation on a third oil agent mixture. The present application also provides a catalytic conversion system. Through the above technical solutions, the present application improves the yield of low-carbon olefins and light aromatics produced from crude oil.

Description

Technical Field

[0001] The present invention relates to the field of petrochemical industry, and in particular to a catalytic conversion method and system for producing low-carbon olefins and light aromatics from crude oil. Background Art

[0002] Crude oil is a complex mixture of various hydrocarbons. At present, oil refineries mainly convert crude oil into fuels such as gasoline, kerosene and diesel, while producing ethylene, propylene and BTX (benzene, toluene and xylene are referred to as BTX). The annual growth rate of vehicle fuel demand has gradually declined in recent years, and fuels such as gasoline, kerosene and diesel are facing a trend of overcapacity. Petrochemical products such as ethylene, propylene and BTX have a wide range of uses, and demand has gradually increased in recent years. Therefore, there has been an oil refining method that reduces the fuel yields of gasoline, kerosene and diesel and improves the petrochemical product yields of ethylene, propylene and BTX.

[0003] For example, CN106029610A discloses an integrated process and facility for converting crude oil into petrochemical products. The integrated process includes crude oil distillation, hydrocracking, aromatization, and olefin synthesis, and the facility includes a crude oil distillation unit, a hydrocracking unit, an aromatization unit, and an olefin synthesis unit.

[0004] However, there is a need to further increase the yield of ethylene, propylene and light aromatics from crude oil. Summary of the Invention

[0005] The purpose of the present invention is to further improve the yield of ethylene, propylene and light aromatics prepared from crude oil.

[0006] In order to achieve the above-mentioned object, the present invention provides a catalytic conversion method for producing light olefins and light aromatics from crude oil, which comprises the following steps: S1, flashing crude oil to obtain light distillate oil and heavy distillate oil; contacting the light distillate oil with a first catalyst in a downer reactor to perform a first catalytic conversion reaction, and performing a first gas-solid separation on the obtained first oil-agent mixture to obtain a first reaction oil gas and a first semi-regenerated agent; S2, introducing a second catalyst and the first semi-regenerated agent into a riser reactor from the bottom and the middle respectively; and introducing the heavy distillate oil from the bottom into the riser reactor to contact the second catalyst and the first semi-regenerated agent. Half of the regenerated agents are contacted in sequence to carry out a second catalytic conversion reaction to obtain a second oil-agent mixture; S3, the second oil-agent mixture is introduced into a catalyst separation device for separation to obtain a second catalyst to be regenerated and a third oil-agent mixture; S4, the third oil-agent mixture is subjected to gas-solid separation to obtain a third reaction oil gas and a first catalyst to be regenerated; S5, the first catalyst to be regenerated is subjected to a first stripping and a first regeneration, and then returned to step S1 as the first catalyst to participate in the first catalytic conversion reaction, and the second catalyst to be regenerated is subjected to a second stripping and a second regeneration, and then returned to step S2 as the second catalyst to participate in the second catalytic conversion reaction.

[0007] The application also provides a catalytic conversion system for producing low-carbon olefins and light aromatics from crude oil, which comprises a crude oil flash tank, a downward reactor, a riser reactor, a settler and a regenerator; a top discharge port of the crude oil flash tank is communicated with an oil gas inlet at an upper end of the downward reactor, and a bottom discharge port of the crude oil flash tank is communicated with a lower oil gas inlet of the riser reactor; a lower end of the downward reactor is provided with a first gas-solid separator, and a solid outlet of the first gas-solid separator is communicated with a first half-regeneration agent inlet at a middle part of the riser reactor; the settler is provided with a settler partition plate and a catalyst separator, the settler partition plate separates the settler into a first settling zone at an upper part and a second settling zone at a lower part; the catalyst separator has a first material outlet arranged in the first settling zone and a second material outlet arranged in the second settling zone; the first settling zone is further connected with a first stripper, and the second settling zone is further connected with a second stripper; the regenerator is provided with a regenerator partition plate, which separates the regenerator into a first regeneration zone and a second regeneration zone; the first stripper and the first regeneration zone are connected through a first spent catalyst conveying connection; the second stripper and the second regeneration zone are connected through a second spent catalyst conveying connection; the first regeneration zone and the downward reactor are connected through a first regenerated catalyst conveying connection; the second regeneration zone and the riser reactor are connected through a second regenerated catalyst conveying connection; the lower part of the second settling zone is provided with the second stripper, and the first spent catalyst conveying connection is provided with the first stripper.

[0008] Through the above technical scheme, the crude oil is subjected to flash separation, the light fraction oil obtained is reacted with the first catalyst of the light oil catalyst, and the heavy fraction oil is reacted with the second catalyst rich in the heavy oil catalyst and the first half-regeneration agent in sequence, so that not only the conversion of the light fraction oil and the heavy fraction oil is realized in a partitioned manner, but also the relay of the primary cracking reaction and the secondary cracking reaction of the heavy fraction oil is facilitated, and the yield of low-carbon olefins and light aromatics is improved.

[0009] Other features and advantages of the present application will be described in detail in the following specific embodiments. BRIEF DESCRIPTION OF DRAWINGS

[0010] The accompanying drawings are included to provide a further understanding of the application, and constitute a part of the specification, and are used together with the following specific embodiments to explain the application, but do not constitute a limitation on the application. In the drawings:

[0011] Figure 1 It is a structural schematic diagram of the catalytic conversion system of one embodiment of the present application.

[0012] Description of Reference Numerals

[0013] Figure 1 In the figure, the reference numerals are described as follows:

[0014] 1-Crude oil flash tank 2-Catalyst distributor 3-Downward reactor

[0015] 4-First gas-solid separator 5-Riser reactor 6-Catalyst separator

[0016] 7-First settling zone 8-First stripper 9-Second settling zone

[0017] 10-Second stripper 11-First regeneration zone 12-Second regeneration zone

[0018] 101-Crude oil 102-Light distillate oil 103-Heavy distillate oil

[0019] 104-recycled light fraction 105-first reaction oil and gas 106-first half regeneration agent

[0020] 107-Pre-lift gas 108-Second oil mixture delivery pipe

[0021] 109, 115 - stripping gas 110, 116 - stripping baffle 111 - settler baffle

[0022] 112-Second spent agent delivery pipe 113, 118-Oil and gas pipeline

[0023] 114, 117-First spent agent delivery pipe

[0024] 119-cyclone separator 120-gas collecting chamber 121-reaction oil and gas

[0025] 122-main air 123-regenerator partition 124-first catalyst delivery pipe

[0026] 125-second catalyst delivery pipe 126, 127-cyclone separator 128-gas collecting chamber

[0027] 129-Regeneration flue gas DETAILED DESCRIPTION

[0028] The following is a detailed description of the specific embodiments of the present invention. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present invention and are not intended to limit the present invention.

[0029] refer to Figure 1The present invention provides a catalytic conversion method for producing light olefins and light aromatics from crude oil, the catalytic conversion method comprising the following steps: S1, flashing crude oil to obtain light distillate oil and heavy distillate oil; contacting the light distillate oil with a first catalyst in a downer reactor to perform a first catalytic conversion reaction, and performing a first gas-solid separation on the obtained first oil-agent mixture to obtain a first reaction oil gas and a first semi-regenerated agent; S2, introducing a second catalyst and the first semi-regenerated agent into a riser reactor from the bottom and the middle respectively; and introducing the heavy distillate oil from the bottom into the riser reactor to mix with the second catalyst and the first semi-regenerated agent. The catalyst and the second catalyst are contacted in sequence to carry out a second catalytic conversion reaction to obtain a second oil-agent mixture; S3, the second oil-agent mixture is introduced into a catalyst separation device for separation to obtain a second spent catalyst and a third oil-agent mixture; S4, the third oil-agent mixture is further subjected to gas-solid separation to obtain a third reaction oil gas and a first spent catalyst; S5, the first spent catalyst is subjected to a first stripping and a first regeneration, and then returned to step S1 as the first catalyst to participate in the first catalytic conversion reaction, and the second spent catalyst is subjected to a second stripping and a second regeneration, and then returned to step S2 as the second catalyst to participate in the second catalytic conversion reaction.

[0030] In the present invention, the first half-regenerated catalyst produced in the downward reactor carries part of the oil and gas, the medium and heavy fraction oil in the lower part of the riser reactor contacts the second catalyst to carry out the first stage of the second catalytic conversion reaction, and then contacts the first half-regenerated catalyst in the upper part of the riser reactor to carry out the second stage of the second catalytic conversion reaction, that is, the catalytic conversion reaction can be carried out in relay.

[0031] Wherein, optionally, in order to facilitate the separation of the first spent catalyst and the second spent catalyst, the particle size and density of the second catalyst are both larger than the particle size and density of the first catalyst.

[0032] Optionally, the first catalyst contains 60-100% by mass of light oil catalyst and 0-40% by mass of heavy oil catalyst; the second catalyst contains 0-40% by mass of light oil catalyst and 60-100% by mass of heavy oil catalyst.

[0033] Preferably, the first catalyst contains 80-100 mass% of light oil catalyst and 0-20 mass% of heavy oil catalyst; the second catalyst contains 0-20 mass% of light oil catalyst and 80-100 mass% of heavy oil catalyst.

[0034] Optionally, the heavy oil catalyst comprises unmodified Y-type molecular sieve or modified Y-type molecular sieve, clay and a binder.

[0035] Wherein, optionally, based on the total weight of the heavy oil catalyst, the content of unmodified Y-type molecular sieve or modified Y-type molecular sieve is 10-80%, preferably 30-60%, the content of clay is 10-80%, preferably 15-60%, and the content of binder is 10-30%, preferably 10-20%.

[0036] Optionally, the particle size of the heavy oil catalyst is in the range of 60 to 250 μm, preferably 80 to 200 μm, and the particle density is 1200 to 1600 kg / m 3 , preferably 1300~1500kg / m 3 .

[0037] The clay is selected from various clays that can be used as catalyst components, such as kaolin, montmorillonite, bentonite, etc. The binder is selected from one or a mixture of two or three of silica sol, alumina sol and pseudo-boehmite, wherein the preferred binder is a bialuminum binder of alumina sol and pseudo-boehmite.

[0038] Optionally, the light oil catalyst comprises unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve, clay and a binder.

[0039] Wherein, optionally, based on the total weight of the catalyst, the content of unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve is 10 to 60%, preferably 20 to 50%, the content of clay is 10 to 80%, preferably 20 to 70%, and the content of binder is 10 to 30%, preferably 10 to 20%.

[0040] Optionally, the particle size of the light oil catalyst is in the range of 10 to 100 μm, preferably 30 to 80 μm, and the particle density is 800 to 1200 kg / m 3 , preferably 900~1100kg / m 3 .

[0041] The clay is selected from various clays that can be used as catalyst components, such as kaolin, montmorillonite, bentonite, etc. The binder is selected from one or a mixture of two or three of silica sol, alumina sol and pseudo-boehmite, wherein the preferred binder is a bialuminum binder of alumina sol and pseudo-boehmite.

[0042] Wherein, optionally, the first regeneration and the second regeneration are performed in the first regeneration zone and the second regeneration zone of the regenerator respectively; the first regeneration zone and the second regeneration zone are arranged in parallel, and both the first regeneration zone and the second regeneration zone adopt full regeneration.

[0043] Optionally, the regeneration conditions of the first regeneration zone and the second regeneration zone independently include: a regeneration temperature of 670-730°C, preferably 690-710°C, a catalyst distribution density of 30-350 kg / m 3 , preferably 80~250kg / m 3 The main wind residence time is 0.5 to 15 seconds, preferably 2 to 10 seconds.

[0044] Wherein, optionally, the reaction temperature of the downward reactor is 620-700° C., preferably 640-680° C., the agent-oil ratio is 10-50, preferably 20-30, and the reaction time is 0.1-5 seconds, preferably 0.5-3 seconds.

[0045] Wherein, optionally, the reaction temperature of the riser reactor is 520-620° C., preferably 540-600° C.; the catalyst-oil ratio is 2-25, preferably 3-20; and the reaction time is 1-15 seconds, preferably 2-10 seconds.

[0046] Optionally, the distance between the inlet of the first half regenerated agent on the riser reactor and the bottom of the riser reactor is 30 to 70%, preferably 40 to 60%, of the total height of the riser reactor.

[0047] Wherein, optionally, the temperature cut point between the light distillate oil and the heavy distillate oil is any temperature between 250 and 400°C, preferably any temperature between 280 and 350°C.

[0048] Among them, preferably, the method also includes: separating and re-refining light fractions from the first reaction oil gas and / or the third reaction oil gas, and introducing the re-refining light fractions from the top of the downward reactor for re-refining; the initial distillation point of the re-refining light fractions is any temperature between 10 and 40°C, and the final distillation point is any temperature between 50 and 80°C.

[0049] Optionally, the method further comprises introducing a pre-lift gas into the bottom of the riser reactor, wherein the pre-lift gas may be selected from one or more of water vapor, nitrogen, and dry gas, preferably water vapor.

[0050] The present invention also provides a catalytic conversion system for producing light olefins and light aromatics from crude oil, the catalytic conversion system comprising a crude oil flash tank, a down-type reactor, a riser reactor, a settler and a regenerator; the top discharge port of the crude oil flash tank is communicated with the oil and gas inlet at the upper end of the down-type reactor, and the bottom discharge port of the crude oil flash tank is communicated with the oil and gas inlet at the lower end of the riser reactor; a first gas-solid separator is provided at the lower end of the down-type reactor, and the solid outlet of the first gas-solid separator is communicated with the first semi-regeneration agent inlet in the middle of the riser reactor; a settler partition and a catalyst separator are provided in the settler, and the settler partition separates the settler into a first settling zone at the upper part and a second settling zone at the lower part; the material inlet of the catalyst separator is communicated with the upper end of the riser reactor, and the catalyst separator also has an opening A first material outlet in the first sedimentation zone and a second material outlet in the second sedimentation zone; a first stripper is also connected to the outside of the first sedimentation zone, and a second stripper is also connected to the lower part of the second sedimentation zone; a regenerator partition is provided in the regenerator, and the regenerator partition separates the regenerator into a first regeneration zone and a second regeneration zone; a first catalyst to be regenerated is connected to the first stripper and the first regeneration zone; a second catalyst to be regenerated is connected to the second stripper and the second regeneration zone; a first regenerated catalyst is connected to the downward reactor; a second regenerated catalyst is connected to the riser reactor; a second stripper is provided at the lower part of the second sedimentation zone, and a first stripper is provided in the first catalyst to be regenerated connection.

[0051] Wherein, the down-type reactor is selected from one or more of a constant diameter down-type reactor and a variable diameter down-type reactor, and the riser reactor is selected from one or more of a constant diameter riser reactor and a variable diameter riser reactor.

[0052] Optionally, the catalyst separation device separates the first catalyst from the second catalyst based on a difference between a particle size and a density of the first catalyst and a particle size and a density of the second catalyst.

[0053] In one embodiment, a first regenerated catalyst delivery connection is provided between the first regeneration zone and the downcomer reactor, and a first catalyst inlet is further provided at the upper portion of the downcomer reactor. The first catalyst inlet can be used to introduce fresh first catalyst or regenerated first catalyst. In one embodiment, a second regenerated catalyst delivery connection is provided between the second regeneration zone and the riser reactor, and a second catalyst inlet is further provided at the lower portion of the riser reactor. The second catalyst inlet can be used to introduce fresh second catalyst or regenerated second catalyst.

[0054] Among them, optionally, the catalyst separator is a combination of one or more of a cyclone type quick separator, a three-leaf quick separator, a catapult type quick separator, a U-tube type separator and a wall-cutting type quick separator, preferably a cyclone type quick separator; the number of the catalyst separators arranged in each of the settlers is one or more; and the multiple catalyst separators are connected in series and / or in parallel.

[0055] As a particularly preferred embodiment of the present invention, refer to Figure 1The down-type reactor 3 is topped with a catalyst distributor 2 for dispersing the first catalyst from the first regeneration zone 11 to achieve a well-fluidized state. A first gas-solid separator 4 is located at the bottom of the down-type reactor 3. Since the first reaction oil mixture is separated into the first reaction oil gas 105 and the first semi-regenerated agent, the catalyst outlet of the first gas-solid separator 4 is connected to the middle of the riser reactor 5. The down-type reactor 3 is selected from one or more of a constant-diameter down-type reactor and a variable-diameter down-type reactor. In the present invention, the bottom of the riser 5 is connected to the second regeneration zone 12 via a second catalyst delivery pipe 125. The middle of the riser reactor 5 is connected to the first gas-solid separator 4 at the bottom of the down-type reactor 3 via a first semi-regenerated agent delivery pipe 106. The height of the connection from the bottom of the riser reactor is 30-70%, preferably 40-60%, of the total height of the riser reactor. The top of the riser reactor 5 is connected to the catalyst separator 6 within the settler via a second reaction oil mixture delivery pipe 108. The catalyst separator 6 is located within the settler. The settler is divided into an upper first settling zone 7 and a lower second settling zone 9 by a settler partition 111. The first spent catalyst outlet of the catalyst separator 6 is located in the first settling zone 7, and the second spent catalyst outlet is located in the second settling zone 9. The first settling zone 7 is connected to the first stripper 8, so that the first spent catalyst is stripped in the first stripper 8 and introduced into the first regeneration zone 11 through the first spent catalyst delivery pipe 117 for regeneration. The second settling zone 9 is connected to the second stripper 10, so that the second spent catalyst is stripped in the second stripper 10 and introduced into the second regeneration zone 12 through the second spent catalyst delivery pipe 112 for regeneration. The catalyst separator 6 is selected from a combination of one or more of a cyclone-type rapid separator, a three-leaf rapid separator, a catapult-type rapid separator, a U-tube separator, and a wall-cutting rapid separator, preferably a cyclone-type rapid separator. A cyclone separator 119 is also provided inside the settler to separate the catalyst entrained in the reaction oil gas, and the obtained reaction oil gas 121 is led out of the device. The delivery speed of the catalyst can be adjusted by the valve on the catalyst delivery pipe. In the present invention, a first regeneration zone 11 and a second regeneration zone 12 are provided in the regenerator. The first regeneration zone 11 and the second regeneration zone 12 are arranged in parallel, and a partition 123 is provided between the two to separate the two catalysts. The first regeneration zone 11 and the second regeneration zone 12 both adopt complete regeneration. Cyclone separators 126 and 127 are provided on the upper part of the first regeneration zone 11 and the second regeneration zone 12 to separate the catalyst entrained in the regeneration flue gas, and the obtained regeneration flue gas 129 is led out of the device.The first regeneration zone 11 is connected to the catalyst distributor 2 at the top of the down-type reactor 3 through a first catalyst delivery pipe 124, and the regeneration zone 12 is connected to the bottom of the riser reactor 5 through a second catalyst delivery pipe 125. The catalyst delivery speed can be adjusted by the valve on the catalyst delivery pipe.

[0056] As a particularly preferred embodiment of the present invention, refer to Figure 1Crude oil 101 is preheated to 250-400° C. and then introduced into a crude oil flash tank 1. Crude oil 101 is separated into light distillate 102 and heavy distillate 103 at a temperature of 250-400° C., preferably 280-350° C., and a pressure of 0.1-0.3 MPa, preferably 0.12-0.2 MPa. The temperature cut point between the light distillate 102 and the heavy distillate 103 is any temperature between 250-400° C., preferably any temperature between 280-350° C. The obtained light distillate oil 102 is sprayed into the downstream reactor 3 through a nozzle, and is contacted and reacted with the first catalyst introduced into the catalyst distributor 2 through the first catalyst delivery pipe 124 under the conditions of a reaction temperature of 620-700°C, preferably 640-680°C, a catalyst-oil ratio of 10-50, preferably 20-30, and a reaction time of 0.1-5 seconds, preferably 0.5-3 seconds. The generated first oil-agent mixture is separated through the first gas-solid separator 4, and the obtained first reaction oil gas 105 is drawn out of the device, and the obtained first half regeneration agent is introduced into the middle part of the riser reactor 5 through the first half regeneration agent delivery pipe 106. The heavy distillate oil 103 is sprayed into the bottom of the riser reactor 5 through a nozzle and reacts with the second catalyst introduced into the bottom of the riser reactor 5 through the second regeneration agent delivery pipe 125 under the conditions of a reaction temperature of 520-620° C., preferably 540-600° C.; a catalyst-oil ratio of 2-25, preferably 3-20; and a reaction time of 1-15 seconds, preferably 2-10 seconds. It then contacts and reacts with the first half-regeneration agent introduced into the middle of the riser reactor 5. The resulting second reaction oil-agent mixture is introduced into the catalyst separator 6 and separated into a first spent catalyst and a second spent catalyst. The first spent catalyst is introduced into the first stripper 8 through the first settling zone 7 for stripping. The stripped first spent catalyst is introduced into the first regeneration zone 11 through the first spent catalyst delivery pipe 117 for regeneration. The regenerated first catalyst is introduced into the catalyst distributor 2 at the top of the down-type reactor 3 through the first catalyst delivery pipe 124. The second spent catalyst is introduced into the second stripper 10 through the second settling zone 9 for stripping. The stripped second spent catalyst is introduced into the second regeneration zone 12 through the second spent catalyst delivery pipe 112 for regeneration. The regenerated second catalyst is introduced into the bottom of the riser reactor 5 through the second catalyst delivery pipe 125. The main air 122 is introduced into the first regeneration zone 11 and the second regeneration zone 12 respectively, and is completely regenerated with the first spent catalyst and the second spent catalyst respectively. The generated regenerated flue gas 129 is led out of the device. The regeneration temperature of the first regeneration zone and the second regeneration zone is 670-730°C, preferably 690-710°C, and the catalyst density is 30-350 kg / m 3 , preferably 80~250kg / m 3The main air residence time is 0.5 to 15 seconds, preferably 2 to 10 seconds. Reaction oil and gas 105 and 121 enter the subsequent product separation system. In the product separation system, the catalytic cracking products are separated into fuel gas, ethylene, ethane, propylene, propane, C4 hydrocarbons, light gasoline, heavy gasoline, diesel, and slurry oil. The light gasoline is introduced into the top of the descending reactor 3 to react with the first catalyst.

[0057] The present invention is further described in detail below through examples.

[0058] Three catalysts were used in the examples and comparative examples, namely GOR-II catalyst, RAG-6 catalyst and DMMC-2 catalyst, all of which are commercial catalysts produced by the Qilu Branch of Sinopec Catalyst Company. The specific properties of the three catalysts are shown in Table 1. Among them, GOR-II is a catalyst containing 40% by weight of Y molecular sieve, RAG-6 is a catalyst containing 35% by weight of ZSM-5 molecular sieve, and DMMC-2 is a catalyst containing 25% by weight of Y molecular sieve and 15% by weight of ZSM-5 molecular sieve. Before the test, the catalyst was aged for 17 hours at 800°C and 100% water vapor. The raw oil used in the examples and comparative examples was Yangzhou crude oil, and its specific properties are shown in Table 2. In the examples and comparative examples, Yangzhou crude oil was first obtained into light distillate oil and heavy distillate oil respectively. The properties of light distillate oil and heavy distillate oil are shown in Table 3. Light gasoline fraction was also used as refining material in the examples and comparative examples. Its composition and properties are shown in Table 4.

[0059] Table 1 Composition and properties of catalysts

[0060] catalyst GOR-II RAG-6 DMMC-2 Chemical composition, % (w) <![CDATA[Al2O3]]> 57.5 51.2 48.1 SiO2 36.1 43.1 46 BET Full Analysis <![CDATA[BET总面积 / (m 2 ·g -1 )]]> 181.000 197.000 102.491 <![CDATA[微孔面积 / (m 2 ·g -1 )]]> 104.000 98.000 49.601 <![CDATA[总孔体积 / (cm 3 ·g -1 )]]> 0.2240 0.1500 0.1057 <![CDATA[微孔体积 / (cm 3 ·g -1 )]]> 0.0340 0.0450 0.0259 Particle density / (kg / m 3 )]]> 1352 965 987 Particle size distribution, %(w) 0-20μm 0.1 0.5 0.1 0-40μm 5.1 32.6 17 0-80μm 20.3 87.3 70.9 0-105μm 50.6 98.5 87.8 >105μm 49.4 1.5 12.2

[0061] Table 2 Composition and properties of Yangzhou crude oil

[0062] project Yangzhou crude oil <![CDATA[密度(20℃) / (kg / m 3 )]]> 848.8 Residual carbon mass fraction / % 3.46 Element mass composition / % C 85.94 H 13.56 S 0.20 N 0.14 Mass group composition / % Saturated hydrocarbons 65.1 Aromatics 26.3 colloid 8.4 Asphaltene 0.2 Metal mass composition / (mg / kg) Fe 1.4 Ni 9.9 V 0.1 Na 3.0 Ca 0.8 Distillation range / ℃ Initial distillation point 40 10v％ 164.2 30v％ 330.3 50v％ 435.5 70v％ 574.1 85v％ 716.7

[0063] Table 3 Composition and properties of light distillate and heavy distillate

[0064]

[0065]

[0066] Table 4 Chemical composition and properties of light gasoline fractions

[0067] project Light gasoline <![CDATA[密度(20℃) / (kg / m 3 )]]> 635.1 Element mass composition / % carbon 84.76 hydrogen 15.24 Sulfur / (μg / g) 46.29 Nitrogen / (μg / g) 32 Distillation range / ℃ Initial distillation point 12 10v％ 18 30v％ 30 50v％ 35 70v％ 57 90v％ 59 Final distillation point 60 Mass group composition / % Alkanes 37.19 Olefins 62.49 Cycloalkanes 0.32 Aromatics 0

[0068] Example 1

[0069] The test Figure 1The reaction was carried out in the apparatus shown. This apparatus comprises a descending reactor and a riser reactor. The descending reactor has a diameter of 15 mm and a length of 2500 mm, while the riser reactor has an inner diameter of 16 mm and a length of 3200 mm. Preheated light distillate oil is introduced into the descending reactor, where it contacts and reacts with a first catalyst enriched in RAG-6 catalyst. The resulting first reaction oil mixture is separated by a separation device, and the resulting first reaction oil gas is withdrawn from the device. The first half of the regenerated catalyst is introduced into the riser reactor 1500 mm from the bottom. Preheated heavy distillate oil is introduced into the bottom of the riser reactor, where it contacts and reacts with a second catalyst enriched in GOR-II catalyst. It then contacts and reacts with the first half of the regenerated catalyst, and the resulting second reaction oil mixture is introduced into a catalyst separator for separation, yielding a first spent catalyst enriched in RAG-6 catalyst and a second spent catalyst enriched in GOR-II catalyst. Both catalysts are introduced into a stripper for stripping via a settling zone. The stripped spent catalyst is then introduced into different regeneration zones for regeneration. The regenerated catalyst is then recycled back into the reactor. Reaction conditions and results are shown in Table 5.

[0070] Example 2

[0071] The method of Example 1 was followed, except that the light gasoline fraction and light distillate oil were introduced as feedstocks into the top of the down-flow reactor. The mass ratio of light gasoline fraction to light distillate oil was 0.2:1. Reaction conditions and results are shown in Table 5.

[0072] Comparative Example 1

[0073] Unlike Example 1, the apparatus used in this comparative example consisted of only one riser reactor. The riser reactor had an inner diameter of 16 mm and a length of 3200 mm. Preheated Yangzhou crude oil was introduced into the riser reactor and contacted with the DMMC-2 catalyst. The resulting oil-agent mixture was separated by a separation device, and the resulting reaction oil and gas were withdrawn from the device. The spent catalyst was introduced into a stripper via a settling zone for stripping. The stripped spent catalyst was then introduced into a regeneration zone for regeneration. The regenerated catalyst was then introduced into the riser reactor for recycling. Reaction conditions and results are shown in Table 5.

[0074] Comparative Example 2

[0075] The method of Example 1 was followed, except that the catalysts used in the descending reactor and the riser reactor were a mixed catalyst of RAG-6 and GOR-II at a mass ratio of 1:1. The reaction conditions and results are shown in Table 5.

[0076] Table 5 Reaction conditions and results of Examples 1-2 and Comparative Examples 1-2

[0077]

[0078]

[0079] As shown in Table 5, the method and device provided by the present application can improve the yield of low-carbon olefins such as ethylene and propylene.

[0080] The preferred embodiments of the present application are described in detail above, but the present application is not limited to the specific details of the above-described embodiments, and various simple modifications can be made to the technical solutions of the present application within the technical concept of the present application, and these simple modifications all belong to the protection scope of the present application.

[0081] In addition, it should be noted that each specific technical feature described in the above specific embodiments can be combined in any appropriate manner without contradiction. In order to avoid unnecessary repetition, the present application will not further describe various possible combinations.

[0082] In addition, various different embodiments of the present application can also be combined in any manner, as long as it does not deviate from the idea of the present application, and it should also be considered as disclosed by the present application.

Claims

1. A catalytic conversion method for producing light olefins and light aromatics from crude oil, characterized in that: The catalytic conversion method comprises the following steps: S1. Flashing crude oil to obtain light distillate oil and heavy distillate oil; contacting the light distillate oil with a first catalyst in a down-flow reactor to perform a first catalytic conversion reaction; and performing a first gas-solid separation on the obtained first oil agent mixture to obtain a first reaction oil gas and a first semi-regenerated agent; the cut point temperature of the light distillate oil and the heavy distillate oil is any temperature between 250° C. and 400° C.; S2. Introducing the second catalyst and the first semi-regenerated agent into the riser reactor from the bottom and the middle, respectively; and introducing the heavy distillate oil from the bottom into the riser reactor to contact with the second catalyst and the first semi-regenerated agent in sequence, performing a second catalytic conversion reaction, and obtaining a second oil-agent mixture; S3, introducing the second oil agent mixture into a catalyst separation device for separation to obtain a second spent catalyst and a third oil agent mixture; S4, performing gas-solid separation on the third oil mixture to obtain a third reaction oil gas and a first spent catalyst; S5, performing a first stripping and a first regeneration on the first spent catalyst, and then returning to step S1 as the first catalyst to participate in the first catalytic conversion reaction, and performing a second stripping and a second regeneration on the second spent catalyst, and then returning to step S2 as the second catalyst to participate in the second catalytic conversion reaction; The particle size and density of the second catalyst are both greater than the particle size and density of the first catalyst; The first catalyst contains 60-100% by mass of a light oil catalyst and 0-40% by mass of a heavy oil catalyst; the second catalyst contains 0-40% by mass of a light oil catalyst and 60-100% by mass of a heavy oil catalyst; The heavy oil catalyst comprises an unmodified Y-type molecular sieve or a modified Y-type molecular sieve, clay, and a binder; based on the total weight of the heavy oil catalyst, the content of the unmodified Y-type molecular sieve or the modified Y-type molecular sieve is 10-80%, the content of the clay is 10-80%, and the content of the binder is 10-30%; The light oil catalyst comprises unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve, clay and a binder; based on the total weight of the light oil catalyst, the content of the unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve is 10-60%, the content of the clay is 10-80%, and the content of the binder is 10-30%.

2. The catalytic conversion method according to claim 1, wherein: The first catalyst contains 80-100% by mass of light oil catalyst and 0-20% by mass of heavy oil catalyst; the second catalyst contains 0-20% by mass of light oil catalyst and 80-100% by mass of heavy oil catalyst.

3. The catalytic conversion method according to claim 2, wherein: Based on the total weight of the heavy oil catalyst, the content of unmodified Y-type molecular sieve or modified Y-type molecular sieve is 30-60%, the content of clay is 15-60%, and the content of binder is 10-20%; The particle size of the heavy oil catalyst is in the range of 60 to 250 μm, and the particle density is in the range of 1200 to 1600 kg / m 3 .

4. The catalytic conversion method according to claim 3, wherein: The particle size of the heavy oil catalyst is in the range of 80 to 200 μm, and the particle density is in the range of 1300 to 1500 kg / m 3 .

5. The catalytic conversion method according to claim 1, wherein: Based on the total weight of the light oil catalyst, the content of unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve is 20-50%, the content of clay is 20-70%, and the content of binder is 10-20%; The particle size of the light oil catalyst is in the range of 10 to 100 μm, and the particle density is in the range of 800 to 1200 kg / m 3 .

6. The catalytic conversion method according to claim 5, wherein: The particle size of the light oil catalyst is in the range of 30 to 80 μm, and the particle density is in the range of 900 to 1100 kg / m 3 .

7. The catalytic conversion method according to claim 1, wherein: The first regeneration and the second regeneration are performed in the first regeneration zone and the second regeneration zone of the regenerator respectively; the first regeneration zone and the second regeneration zone are arranged in parallel, and both the first regeneration zone and the second regeneration zone adopt complete regeneration.

8. The catalytic conversion method according to claim 7, wherein: The regeneration conditions of the first regeneration zone and the second regeneration zone independently include: a regeneration temperature of 670-730°C, a catalyst distribution density of 30-350 kg / m 3 , the main wind stay time is 0.5~15s.

9. The catalytic conversion method according to claim 8, wherein: The regeneration conditions of the first regeneration zone and the second regeneration zone independently include: a regeneration temperature of 690-710°C, a catalyst distribution density of 80-250 kg / m 3 , the main wind stay time is 2 to 10s.

10. The catalytic conversion method according to claim 1, wherein: The reaction temperature of the downward reactor is 620-700°C, the catalyst-oil ratio is 10-50, and the reaction time is 0.1-5 seconds; The reaction temperature of the riser reactor is 520-620°C; the catalyst-oil ratio is 2-25; and the reaction time is 1-15 seconds. The height between the inlet of the first half regenerated agent on the riser reactor and the bottom of the riser reactor is 30-70% of the total height of the riser reactor.

11. The catalytic conversion method according to claim 10, wherein: The reaction temperature of the downward reactor is 640-680°C, the catalyst-oil ratio is 20-30, and the reaction time is 0.5-3 seconds; The reaction temperature of the riser reactor is 540-600°C; the catalyst-oil ratio is 3-20; and the reaction time is 2-10 seconds. The height between the inlet of the first half regenerated agent on the riser reactor and the bottom of the riser reactor is 40-60% of the total height of the riser reactor.

12. The catalytic conversion method according to claim 1, wherein: The cutting point temperature between the light distillate oil and the heavy distillate oil is any temperature between 280° C. and 350° C.

13. The catalytic conversion method according to claim 12, wherein: The method further includes: separating and recycling light fractions from the first reaction oil gas and / or the third reaction oil gas, and introducing the recycled light fractions from the top of the downward reactor for recycling; the initial distillation point of the recycled light fractions is any temperature between 10 and 40°C, and the final distillation point is any temperature between 50 and 80°C.

14. A system for the catalytic conversion method of crude oil to produce light olefins and light aromatics according to any one of claims 1 to 13, characterized in that: The system includes a crude oil flash tank, a down-type reactor, a riser reactor, a settler and a regenerator; The top discharge port of the crude oil flash tank is connected to the oil and gas inlet at the upper end of the down-type reactor, and the bottom discharge port of the crude oil flash tank is connected to the oil and gas inlet at the lower end of the riser reactor; A first gas-solid separator is provided at the lower end of the down-type reactor, and a solid outlet of the first gas-solid separator is connected to a first semi-regenerated agent inlet in the middle of the riser reactor; The settler is provided with a settler partition and a catalyst separator, wherein the settler partition divides the settler into a first settling zone at the upper portion and a second settling zone at the lower portion; a material inlet of the catalyst separator is connected to the upper end of the riser reactor, and the catalyst separator further has a first material outlet opened in the first settling zone and a second material outlet opened in the second settling zone; The outside of the first settling zone is further connected to a first stripper, and the lower part of the second settling zone is further connected to a second stripper; A regenerator partition is provided in the regenerator, which divides the regenerator into a first regeneration zone and a second regeneration zone; a first regenerated catalyst delivery connection is provided between the first stripper and the first regeneration zone; a second regenerated catalyst delivery connection is provided between the second stripper and the second regeneration zone; a first regenerated catalyst delivery connection is provided between the first regeneration zone and the downward reactor; and a second regenerated catalyst delivery connection is provided between the second regeneration zone and the riser reactor.

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