CN116789510A - Method for preparing ethylene propylene by catalytic cracking - Google Patents

Method for preparing ethylene propylene by catalytic cracking Download PDF

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Publication number
CN116789510A
CN116789510A CN202210251215.5A CN202210251215A CN116789510A CN 116789510 A CN116789510 A CN 116789510A CN 202210251215 A CN202210251215 A CN 202210251215A CN 116789510 A CN116789510 A CN 116789510A
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China
Prior art keywords
catalyst
outlet
riser reactor
bed reactor
reactor
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CN202210251215.5A
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Chinese (zh)
Inventor
李晓红
高攀
彭飞
马晓克
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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Priority to CN202210251215.5A priority Critical patent/CN116789510A/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
    • B01J29/084—Y-type faujasite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/90—Regeneration or reactivation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/06—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using steam
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention provides a method for preparing ethylene propylene by catalytic cracking, in particular to a reactor for increasing yield of ethylene propylene by heavy oil catalytic cracking and a reaction method thereof, wherein heavy oil raw materials are converted into products mainly comprising gasoline and diesel oil in a riser reactor, and a certain amount of C4 blend and/or C5-C6 light gasoline with lower octane number is produced at the same time; the byproduct C4 blend and/or C5-C6 light gasoline enters a fast bed reactor and is converted into ethylene propylene under proper conditions. The riser reactor for converting heavy oil and the fast bed reactor for converting C4 blend and/or C5-C6 light gasoline are coupled together, so that the redundant heat in the heavy oil catalytic cracking process can be fully utilized, and the reaction temperature required by mixing the C4 and C5-C6 light gasoline can be satisfied.

Description

Method for preparing ethylene propylene by catalytic cracking
Technical Field
The present invention relates to a method for preparing ethylene propylene by catalytic cracking, and in particular to a method for preparing ethylene propylene by catalytic cracking heavy oil.
Background
Low-carbon olefins, i.e., ethylene and propylene, are two important basic chemical raw materials, and the demand of the low-carbon olefins is continuously increasing.
The gasoline and diesel oil in the traditional heavy oil catalytic cracking process are main products. Researches show that mixed C4 and C5-C6 light gasoline can be converted into ethylene and propylene on a Y-type molecular sieve catalyst under certain conditions, but the yield is lower, and in order to improve the added value of products in the heavy oil catalytic cracking process and the yield of ethylene and propylene, some patents directly carry out heavy oil catalytic cracking reaction or couple light hydrocarbon, light oil catalytic cracking and heavy oil catalytic cracking together, and a plurality of riser reactors are adopted to respectively crack the light hydrocarbon/light oil and heavy oil, and related patents comprise CN111718231, CN111689829, CN110551519 and the like.
CN110551519 converts heavy hydrocarbons, methanol and light hydrocarbons respectively using three cracking reactors; CN111689829 converts heavy petroleum hydrocarbon and light hydrocarbon respectively using two riser reactors; CN111718231 adopts two relatively independent riser reaction-regeneration systems and two catalysts, and the flow is complex. The reactors of the patents are relatively independent, and ethylene propylene is taken as a main target product, so that the production of gasoline and diesel is not considered.
Disclosure of Invention
One of the technical problems to be solved by the invention is to solve the technical defects of low yield and low added value of products of the existing ethylene and propylene, and provide a reaction method for increasing yield of ethylene and propylene by catalytic cracking of heavy oil, which has the advantages of both ethylene and propylene production and high added value of products.
To solve the above problems, the present invention provides a general method for preparing ethylene propylene by catalytic cracking, comprising:
a) Heavy oil raw materials enter the riser reactor through a riser reactor raw material inlet at the bottom of the riser reactor and contact and react with a first part of regenerated catalyst from a riser regenerated catalyst inlet to obtain a reaction product I and a first spent catalyst obtained by partial deactivation of the catalyst, and both the reaction product I and the first spent catalyst ascend through a riser reactor outlet structural member and enter the interior of the mixed stripping zone;
b) The raw materials containing light hydrocarbon enter the fast bed reactor through a fast bed reactor raw material inlet at the lower part of the fast bed reactor, contact and react with a second part of regenerated catalyst from a fast bed reactor regenerant inlet to obtain a reaction product II and a second spent catalyst obtained by partial deactivation of the catalyst, and both of the reaction product II and the second spent catalyst go upwards through an outlet structural member of the fast bed reactor to enter the interior of a mixed stripping zone; mixing the first spent catalyst and the second spent catalyst in a mixed stripping zone to form a mixed catalyst;
c) The stripping medium enters a mixed stripping zone through a stripping medium inlet to strip the mixed catalyst to obtain a stripped catalyst;
d) The stripped catalyst is used as a spent catalyst, and enters a regeneration system through a spent catalyst outlet of a mixed stripping zone to remove carbon deposit on particles so as to obtain a regenerated catalyst; and optionally
e) The reaction product rich in ethylene and propylene obtained in the reaction process enters a subsequent separation system through a reaction product outlet of a mixed stripping zone to obtain a C4 blend, C5-C6 light gasoline or a mixture thereof;
wherein the fast bed reactor, the mixed stripping zone, the riser reactor are coaxially arranged, and wherein the fast bed reactor radially surrounds the riser reactor.
In one embodiment, the regenerated catalyst resulting from the removal of carbon deposits on the particles by the regeneration system is partitioned into the second partially regenerated catalyst and the first partially regenerated catalyst.
In one embodiment, the light hydrocarbon-containing feedstock comprises, consists essentially of, or consists of: a C4 blend, a C5-C6 light gasoline, or a mixture thereof.
Generally, mixed C4, C5-C6 light gasoline can be converted into ethylene and propylene on a Y-type molecular sieve catalyst under certain conditions, but the yield is lower.
The invention provides a reactor for increasing ethylene and propylene yield by heavy oil catalytic cracking and a reaction method, wherein heavy oil raw materials are converted into products mainly comprising gasoline and diesel oil in a riser reactor, and a certain amount of C4 blend and/or C5-C6 light gasoline with lower octane number are produced at the same time; the byproduct C4 blend and/or C5-C6 light gasoline enters a fast bed reactor and is converted into ethylene propylene under proper conditions. The riser reactor for converting heavy oil and the fast bed reactor for converting C4 blend and/or C5-C6 light gasoline are coupled together, so that the redundant heat in the heavy oil catalytic cracking process can be fully utilized, and the reaction temperature required by mixing the C4 and C5-C6 light gasoline can be satisfied.
In the present invention, the reaction products involved in the various embodiments, including, for example, the reaction product I shown, reaction product I, and other reaction products that may be involved, represent each a material that is converted by a reaction intended to give an ethylene propylene product, and that is capable of yielding an ethylene propylene-enriched product by separation units known in the art, although the specific composition may vary somewhat from embodiment to embodiment due to variations in the feedstock, reaction conditions, etc. within the scope of the present invention.
According to one embodiment of the invention, a Y molecular sieve catalyst is used.
According to one embodiment of the invention, the overall yield of ethylene propylene carbon based can be more than 15 wt%, for example up to 18 wt%.
Drawings
FIG. 1 is a schematic illustration of a reaction system for a process for the catalytic cracking production of ethylene propylene according to one embodiment of the present invention;
fig. 2 is a schematic diagram of a riser reactor outlet structure 13 and a fast off-bed nested vessel outlet structure 14 according to one embodiment of the present invention.
Description of the drawings with partial reference numerals
1 is a regeneration system; 2 is a riser reactor; 3 is a fast bed reactor; 4 is a mixed stripping zone; 5 is a riser regenerated catalyst inlet; 7 is a spent catalyst outlet of the mixed stripping zone; 9 is a mixed stripping zone reaction product outlet; 10 is a fast bed reactor feed inlet; 11 is the riser reactor feed inlet; 13 is the riser reactor outlet structure; 14 is the exit structure of the fast bed reactor; 15 is the spent catalyst inlet of the regeneration system; reference numeral 16 denotes an outlet of the regenerated catalyst of the first portion of the regeneration system; 17 is the outlet of the regenerated catalyst of the second part of the regeneration system; 18 is a fast bed reactor regenerant inlet; 19 is the stripping medium inlet; 20 is the riser reactor outlet structure roof; 21 is the riser reactor outlet structure top support; and 22 is a distribution plate of outlet structural member holes of the fast-bed reactor.
Detailed Description
The following describes specific embodiments of the present invention in detail with reference to the drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
In the description of the present invention, it should be understood that the directions or positional relationships indicated by the terms "radial," "inner," "outer," etc. are based on the directions or positional relationships shown in the drawings, only for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the apparatus or element in question must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present invention.
In the present invention, like reference numerals generally refer to like/corresponding objects.
In the present invention, the pressures are gauge pressures unless otherwise indicated. In the present invention, the content, proportion, ratio, etc. are calculated on a weight/mass basis without particular indication.
In the present invention, the "spent catalyst" means a catalyst which is deactivated in the reaction system and is required to be used for the reaction system by regeneration.
In the present invention, the "regenerated (catalyst)" means a catalyst which is regenerated in a regenerating device to be used for a reaction system.
As shown in FIG. 1, the invention provides a method for preparing ethylene propylene by catalytic cracking, and the reaction system and general flow are shown in FIG. 1.
Referring to fig. 1, in one embodiment, the present invention provides an overall process for the catalytic cracking of ethylene propylene comprising:
a) Heavy oil raw materials enter the riser reactor (2) through a riser reactor raw material inlet (11) at the bottom of the riser reactor (2) and contact and react with a first part of regenerated catalyst from a riser regenerated catalyst inlet (5) to obtain a reaction product I and a first to-be-regenerated catalyst obtained by partial deactivation of the catalyst, and the reaction product I and the first to-be-regenerated catalyst both ascend through a riser reactor outlet structural member (13) and enter the interior of the mixed stripping zone (4); spent catalyst
b) The light hydrocarbon-containing raw material enters the fast bed reactor (3) through a fast bed reactor raw material inlet (10) at the lower part of the fast bed reactor (3) and reacts with a second part of regenerated catalyst from a fast bed reactor regenerant inlet (18) in a contact way to obtain a reaction product II and a second spent catalyst obtained by partial deactivation of the catalyst, and both the reaction product II and the second spent catalyst ascend through a fast bed reactor outlet structural member (14) to enter the interior of a mixed stripping zone (4); mixing the first spent catalyst and the second spent catalyst in a mixed stripping zone to form a mixed catalyst;
c) The stripping medium enters a mixed stripping zone through a stripping medium inlet (19) to strip the mixed catalyst to obtain a stripped catalyst;
d) The stripped catalyst is used as a spent catalyst, and enters a regeneration system (1) through a spent catalyst outlet (7) of a mixed stripping zone to remove carbon deposit on particles so as to obtain a regenerated catalyst; and optionally
e) Mixing the reaction product I and the reaction product II in a mixed stripping zone, and enabling the obtained reaction product rich in ethylene and propylene to enter a subsequent separation system through a reaction product outlet (9) of the mixed stripping zone to obtain a C4 blend, C5-C6 light gasoline or a mixture thereof;
wherein the fast bed reactor, the mixed stripping zone, the riser reactor are coaxially arranged, and wherein the fast bed reactor radially surrounds the riser reactor.
Accordingly, according to the present invention, all of the stripped catalyst acts as the spent catalyst. And accordingly, no mixed catalyst or stripped catalyst is recycled back to the fast bed reactor.
In one embodiment, riser reactor 2, fast bed reactor 3, and mixed stripping zone 4 are coaxial, with fast bed reactor 3 surrounding riser reactor 2; the outlet of the riser reactor 2 is connected with a riser reactor outlet structural member 13, and the top of the fast-bed reactor 3 is connected with a fast-bed reactor outlet structural member 14; the riser reactor outlet structure 13 and the fast bed reactor outlet structure 14 are both located within the mixed stripping zone 4. In one embodiment, riser reactor outlet structure 13 is located above fast bed reactor outlet structure 14.
In one embodiment, the inside of the mixed stripping zone 4 is provided with an annular distributor surrounding and coaxial with the upper lifting zone of the fast-bed reactor 3, for conveying the gas with fluidization (for example steam) upwards into the inside of the mixed stripping zone 4 and acting on the first and the first spent catalyst.
In the present invention, a cyclone separator may be provided in the mixed stripping zone 4, or any other device capable of achieving a similar function (in particular, for example, separation of catalyst from product).
Referring to the illustrated embodiment of fig. 1-2, according to one embodiment of the present invention, the riser reactor outlet structure (13) consists of a riser reactor outlet structure roof (20) and a riser reactor outlet structure roof support (21); the outlet of the riser reactor (2) is directly connected with a structural member top support (21) of the outlet of the riser reactor, and the structural member top support (21) of the outlet of the riser reactor is directly connected with a structural member top (20) of the outlet of the riser reactor; the riser reactor outlet structural member top support (21) is positioned above the riser reactor (2), and the riser reactor outlet structural member top (20) is positioned above the riser reactor outlet structural member top support (21); the ratio of the maximum distance h at the edge of the top (20) of the outlet structure of the riser reactor to the outlet diameter r of the fast-bed reactor (2) is (1-3): 1.
According to one embodiment of the invention, the fast-bed reactor outlet structure (14) consists of a fast-bed reactor outlet structure hole distribution plate (22); the central angle alpha of the hole distribution plate (22) of the outlet structural member of the fast bed reactor is 30 o -150 o The method comprises the steps of carrying out a first treatment on the surface of the The porosity of the rapid bed reactor outlet structure hole distribution plate (22) is 50-95%.
According to one embodiment of the invention, the upper part of the riser reactor 2 extends beyond the top of the lifting zone of the upper part of the fast bed reactor such that the riser reactor outlet structure 13 is located above the fast bed reactor outlet structure 14. An embodiment which may be referred to as a "top-to-bottom arrangement" in the present invention is shown, for example, in fig. 1 and 2.
According to one embodiment of the invention, the mixed stripping zone (4) is provided with an external or internal heat extractor to reduce the temperature of the catalyst in the mixed stripping zone (4).
According to one embodiment of the invention, the fast-bed reactor (3) is provided with an external or internal heat extractor to reduce the temperature of the catalyst in the fast-bed reactor (3).
It will be appreciated by those skilled in the art that in the present invention, the primary function of the external heat extractor is to effect a temperature reduction of the mixed catalyst to suit the reaction requirements in the fast bed reactor. Thus, according to one embodiment of the invention, the external heat collector may be replaced by any other device capable of performing the main function, provided that it does not significantly detract from the purpose of the invention. Accordingly, the outer heat collector may be replaced with an inner heat collector.
In one embodiment, the regenerated catalyst resulting from removal of carbon deposits on the particles by the regeneration system is distributed in a ratio of (1-20): 1, preferably (5-15): 1, between the first partially regenerated catalyst and the second partially regenerated catalyst.
In the present invention, the heavy oil feedstock is a heavy distillate, such as straight run vacuum distillate, coker heavy distillate, solvent deasphalted oil, hydrotreated heavy oil.
In the present invention, the light hydrocarbon-containing raw material is not particularly required, and light hydrocarbon-containing raw materials commonly used in the art can be used in the present invention, and according to one embodiment of the present invention, the light hydrocarbon-containing raw material is a C4 blend, a C5-C6 light gasoline or a mixture thereof, and preferably the light hydrocarbon-containing raw material includes at least a part or all of the C4 blend, the C5-C6 light gasoline or a mixture thereof obtained by the separation unit of the present invention.
According to one embodiment of the invention, the proportion of the C4 blend, the C5-C6 light gasoline or the mixture thereof obtained from the separation unit in the light hydrocarbon-containing raw material is more than 20% by weight, and the rest of the C4 blend, the C5-C6 light gasoline or the mixture thereof can be obtained from a catalytic cracking and/or steam cracking unit according to the situation.
According to one embodiment of the invention, 30% to 100% by weight, preferably 50% to 100% by weight, of the C4 blend, C5-C6 light gasoline or mixture thereof obtained from the separation unit is used for the light hydrocarbon-containing feedstock.
According to one embodiment of the invention, the total C4 blend, C5-C6 light gasoline or mixtures thereof obtained from the separation unit of the invention is used as the total light hydrocarbon-containing feedstock.
In the present invention, the composition of the C4 blend, the C5-C6 light gasoline, or a mixture thereof may be, for example, one or more of isobutylene, 1-butene, n-butane, isobutane, isopentene, n-pentene, n-pentane, n-hexene, and isohexene.
According to one embodiment of the present invention, the mass ratio of the heavy oil feedstock to the light hydrocarbon-containing feedstock is (2-8): 1, preferably (3-6): 1.
The kind of the stripping medium fed through the stripping medium inlet 19 is not particularly limited in the present invention, and may be any medium that is currently available and can be applied to the process of producing ethylene propylene from heavy oil, such as water or nitrogen.
In the present invention, the operation conditions in the fast bed reactor 3 are not particularly limited, and those commonly used in the art can be employed. According to one embodiment of the invention, the operating conditions of the fast-bed reactor (3) comprise a catalyst bed temperature of 550-650 ℃ and a catalyst bed gas line speed of 1-3The density of the catalyst bed layer is 50-200 kg/m 3 . According to one embodiment of the invention, the operating conditions of the riser reactor (2) comprise an outlet catalyst temperature of 470-540 ℃, an outlet gas linear velocity of 10-25 m/s, an outlet catalyst density of 5-50 kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The pressure in the mixed stripping zone (4) is 0.05-0.3MPaG.
According to the present invention, preferably, the catalyst is a molecular sieve catalyst.
According to the present invention, preferably, the molecular sieve catalyst is at least one of a SAPO-34 molecular sieve catalyst, a Y molecular sieve catalyst and a beta molecular sieve catalyst, more preferably a Y molecular sieve catalyst.
According to one embodiment of the invention, the regenerated catalyst has a carbon content of not more than 1% based on the total mass of the catalyst. In one embodiment, the regenerated catalyst has a carbon content of 0.01 to 0.3% based on the total mass of regenerated catalyst.
The invention is mainly characterized in that the process of the reaction system is changed, and other operation equipment, conditions, methods and steps which are not specifically described can be performed by adopting conventional methods, conditions and steps. In particular, the present invention is not particularly limited with respect to the specific dimensions of the equipment (including riser reactors, fast bed reactors, mixed stripping zones, regeneration systems, etc.), and may be determined in detail as appropriate according to conventional means in the art, as long as it meets the limitations and requirements that the present invention has made with respect to the entire reaction system, in particular, the operating conditions required for the riser reactor (2) and the fast bed reactor (3) according to the present invention.
In the present invention, the total yield of ethylene and propylene is calculated as ethylene propylene total yield = ethylene propylene mass/carbon matrix amount of heavy oil feed x 100%.
Examples
The invention is further illustrated, but not limited, by the following examples. In an embodiment, reference is made primarily to fig. 1; wherein the riser reactor outlet structure, the fast bed reactor outlet structure, etc. refer to the embodiment shown in fig. 2.
Example 1
The apparatus of fig. 1 was employed.
The ratio of the maximum distance h at the edge of the riser reactor outlet structure roof (20) to the outlet diameter r of the fast-bed reactor (2) is 1:1.
The fast bed reactor outlet structure (14) is comprised of a fast bed reactor outlet structure aperture distribution plate (22). The central angle alpha of the hole distribution plate (22) of the outlet structural member of the fast bed reactor is 30 o . The porosity of the rapid bed reactor outlet structure hole distribution plate (22) is 50%.
Heavy oil raw material enters the riser reactor (2) through a raw material inlet (11) of the riser reactor and is in contact reaction with a first part of regenerated catalyst from a regenerated catalyst inlet (5) of the riser, and a first spent catalyst obtained by ascending enters the interior of the mixed stripping zone (4) through an outlet structural member (13) of the riser reactor.
The light hydrocarbon-containing raw material enters the fast bed reactor (3) through a fast bed reactor raw material inlet (10) and reacts with a second part of regenerated catalyst from a fast bed reactor regenerant inlet (18) in a contact way, and the second spent catalyst is obtained by ascending, and enters the interior of the mixed stripping zone (4) through a fast bed reactor outlet structural member (14).
The stripping medium enters the mixed stripping zone (4) through the stripping medium inlet (19), and the spent catalyst enters the regeneration system (1) through the mixed stripping zone spent catalyst outlet (7) to remove carbon deposit on the spent catalyst to obtain regenerated catalyst.
The reaction product obtained in the reaction process enters a subsequent separation system through a reaction product outlet (9) of the mixed stripping zone to obtain C5-C6 light gasoline or a mixture thereof, which is used as the raw material containing light hydrocarbon.
The heavy oil raw material is normal pressure wax oil from Daqing oil field. The stripping medium is steam.
The catalyst is a catalyst containing a Y molecular sieve. The carbon content of the regenerated catalyst was 0.01% based on the total mass of the regenerated catalyst.
The ratio of the first partially regenerated catalyst to the second partially regenerated catalyst is 1:1.
The temperature of the catalyst bed layer of the fast bed reactor (3) is 550 ℃, the linear velocity of the gas of the catalyst bed layer is 1 m/s, and the density of the catalyst bed layer is 200 kg/m 3 . The outlet catalyst temperature of the riser reactor (2) was 470 ℃, the outlet gas line velocity was 10 m/s, and the outlet catalyst density was 50 kg/m 3 . The pressure in the mixed stripping zone (4) was 0.3MPaG.
In this example, the ethylene and propylene yields were up to 15.3 wt%.
Example 2
With the apparatus of example 1, except that the ratio of the maximum distance h at the edge of the riser reactor outlet structure roof (20) to the outlet diameter r of the fast-bed reactor (2) was 3:1. The central angle alpha of the hole distribution plate (22) of the outlet structural member of the fast bed reactor is 150 o . The porosity of the rapid bed reactor outlet structure hole distribution plate (22) was 95%.
The heavy oil raw material is normal pressure wax oil from Daqing oil field. The light hydrocarbon-containing raw material is a C4 blend. The stripping medium is steam.
The catalyst is a catalyst containing a Y molecular sieve. The carbon content of the regenerated catalyst was 0.3% based on the total mass of the regenerated catalyst.
The ratio of the first partially regenerated catalyst to the second partially regenerated catalyst is 20:1.
The temperature of the catalyst bed layer of the fast bed reactor (3) is 650 ℃, the linear velocity of the gas of the catalyst bed layer is 3 m/s, and the density of the catalyst bed layer is 50 kg/m 3 . The outlet catalyst temperature of the riser reactor (2) is 540 ℃, the line speed of outlet gas is 25 m/s, and the density of outlet catalyst is 5 kg/m 3 . The pressure in the mixed stripping zone (4) was 0.05MPaG.
In this example, the ethylene and propylene yields were 16.2 wt%.
Example 3
With the apparatus of example 1, except that the ratio of the maximum distance h at the edge of the riser reactor outlet structure roof (20) to the outlet diameter r of the fast bed reactor (2) was 2:1. The central angle alpha of the hole distribution plate (22) of the outlet structural member of the fast bed reactor is 100 o . Fast bed reactor outletThe porosity of the mouth structure hole distribution plate (22) is 70%.
The heavy oil raw material is normal pressure wax oil from Daqing oil field. The light hydrocarbon-containing raw materials are C4 blend and C5-C6 light gasoline, and the mass ratio of the C4 blend to the C5-C6 light gasoline is 2:1. The stripping medium is steam.
The catalyst is a catalyst containing a Y molecular sieve. The carbon content of the regenerated catalyst was 0.15% based on the total mass of the regenerated catalyst.
The ratio of the first partially regenerated catalyst to the second partially regenerated catalyst is 6:1.
The temperature of the catalyst bed layer of the fast bed reactor (3) is 600 ℃, the linear velocity of the gas of the catalyst bed layer is 1.5 m/s, and the density of the catalyst bed layer is 100 kg/m 3 . The temperature of the catalyst at the outlet of the riser reactor (2) is 500 ℃, the linear velocity of the outlet gas is 17 m/s, and the density of the catalyst at the outlet is 20 kg/m 3 . The pressure in the mixed stripping zone (4) was 0.1MPaG.
In this example, the ethylene and propylene yields were up to 18.2 wt%.
Example 4
With the apparatus of example 1, except that the ratio of the maximum distance h at the edge of the riser reactor outlet structure roof (20) to the outlet diameter r of the fast-bed reactor (2) was 1.5:1. The central angle alpha of the hole distribution plate (22) of the outlet structural member of the fast bed reactor is 90 o . The porosity of the rapid bed reactor outlet structure hole distribution plate (22) is 90%.
The heavy oil raw material is coked heavy distillate oil. The light hydrocarbon-containing raw materials are C4 blend and C5-C6 light gasoline, and the mass ratio of the C4 blend to the C5-C6 light gasoline is 1:1.5. The stripping medium is nitrogen.
The catalyst is a catalyst containing a Y molecular sieve. The carbon content of the regenerated catalyst was 0.1% based on the total mass of the regenerated catalyst.
The ratio of the first partially regenerated catalyst to the second partially regenerated catalyst is 15:1.
The temperature of the catalyst bed layer of the fast bed reactor (3) is 630 ℃, the linear velocity of the gas of the catalyst bed layer is 2.5 m/s, and the density of the catalyst bed layer is 80 kg/m 3 . Riser reactionThe temperature of the catalyst at the outlet of the device (2) is 520 ℃, the linear velocity of the outlet gas is 15 m/s, and the density of the catalyst at the outlet is 30 kg/m 3 . The pressure in the mixed stripping zone (4) was 0.13MPaG.
In this example, the ethylene and propylene yields were up to 14.7 wt%.
Comparative example 1
Essentially referring to the apparatus and process of example 3, only a riser reactor was used without the fast bed reactor and its corresponding structure.
Heavy oil raw materials enter a riser reactor (2) through a raw material inlet (11) of the riser reactor and react with regenerated catalyst from a regenerated catalyst inlet (5) of the riser in a contact way, and the catalyst to be regenerated is obtained by ascending and enters the interior of the mixed stripping zone (4) through an outlet structural member (13) of the riser reactor. The stripping medium enters the mixed stripping zone (4) through the stripping medium inlet (19) to strip the mixed catalyst in the mixed stripping zone (4), the spent catalyst in the mixed stripping zone (4) enters the regeneration system (1) through the spent catalyst outlet (7) of the mixed stripping zone to remove carbon deposit on the spent catalyst to obtain the regenerated catalyst. The reaction product obtained in the reaction process enters a subsequent separation system through a reaction product outlet (9) of the mixed stripping zone.
The heavy oil raw material is normal pressure wax oil from Daqing oil field. The stripping medium is steam.
The catalyst is a catalyst containing a Y molecular sieve. The carbon content of the regenerated catalyst was 0.15% based on the total mass of the regenerated catalyst.
The temperature of the catalyst at the outlet of the riser reactor (2) is 500 ℃, the linear velocity of the outlet gas is 17 m/s, and the density of the catalyst at the outlet is 20 kg/m 3 . The pressure in the mixed stripping zone (4) was 0.1MPaG.
In this example, the ethylene and propylene yields were 8.6 wt%.
Comparative example 2
With the apparatus of example 3, except that the ratio of the maximum distance h at the edge of the riser reactor outlet structure roof (20) to the outlet diameter r of the fast-bed reactor (2) was 0.5:1.
In this example, the ethylene and propylene yields were 13.9 wt%.
Comparative example 3
With the apparatus of example 3, except that the catalyst bed temperature of the fast bed reactor (3) was 520℃and the catalyst bed gas line velocity was 4 m/s, the catalyst bed density was 30 kg/m 3 。
In this example, the ethylene and propylene yields were 11.7 wt%.
The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of individual specific technical features in any suitable way. The various possible combinations of the invention are not described in detail in order to avoid unnecessary repetition. Such simple variations and combinations are likewise to be regarded as being within the scope of the present disclosure.

Claims (10)

1. A process for the preparation of ethylene propylene by catalytic cracking comprising:
a) Heavy oil raw materials enter a riser reactor (2) through a riser reactor raw material inlet (11) at the bottom of the riser reactor and contact and react with a first part of regenerated catalyst from a riser regenerated catalyst inlet (5) to obtain a reaction product I and a first to-be-regenerated catalyst obtained by partial deactivation of the catalyst, and the reaction product I and the first to-be-regenerated catalyst both ascend through a riser reactor outlet structural member (13) and enter the interior of the mixed stripping zone (4); spent catalyst
b) The raw materials containing light hydrocarbon enter a fast bed reactor (3) through a fast bed reactor raw material inlet (10) at the lower part of the fast bed reactor, contact and react with a second part of regenerated catalyst from a fast bed reactor regenerant inlet (18) to obtain a reaction product II and a second spent catalyst obtained by partial deactivation of the catalyst, and both of the reaction product II and the second spent catalyst ascend through a fast bed reactor outlet structural member (14) to enter the interior of a mixed stripping zone (4); mixing the first spent catalyst and the second spent catalyst in a mixed stripping zone to form a mixed catalyst;
c) The stripping medium enters a mixed stripping zone through a stripping medium inlet (19) to strip the mixed catalyst to obtain a stripped catalyst;
d) The stripped catalyst is used as a spent catalyst, and enters a regeneration system (1) through a spent catalyst outlet (7) of a mixed stripping zone to remove carbon deposit on particles so as to obtain a regenerated catalyst; and optionally
e) Mixing the reaction product I and the reaction product II in a mixed stripping zone, and enabling the obtained reaction product rich in ethylene and propylene to enter a subsequent separation system through a reaction product outlet (9) of the mixed stripping zone to obtain a C4 blend, C5-C6 light gasoline or a mixture thereof;
wherein the fast bed reactor, the mixed stripping zone, the riser reactor are coaxially arranged, and wherein the fast bed reactor radially surrounds the riser reactor.
2. The method according to claim 1, wherein the riser reactor outlet structure (13) is located above a fast bed reactor outlet structure (14).
3. The method according to claim 1, characterized in that the riser reactor outlet structure (13) consists of a riser reactor outlet structure roof (20) and a riser reactor outlet structure roof support (21); the outlet of the riser reactor (2) is directly connected with a structural member top support (21) of the outlet of the riser reactor, and the structural member top support (21) of the outlet of the riser reactor is directly connected with a structural member top (20) of the outlet of the riser reactor; the riser reactor outlet structure top support (21) is located above the riser reactor (2) and the riser reactor outlet structure top (20) is located above the riser reactor outlet structure top support (21).
4. A method according to claim 3, characterized in that the ratio of the maximum distance h at the edge of the riser reactor outlet structure roof (20) to the outlet diameter r of the fast-bed reactor (2) is (1-3): 1.
5. A method according to claim 3, characterized in that the fast-bed reactor outlet structure (14) consists of a fast-bed reactor outlet structure hole distribution plate (22); the porosity of the rapid bed reactor outlet structure hole distribution plate (22) is 50-95%.
6. A method according to claim 3, characterized in that the fast bed reactor outlet structure hole distribution plate (22) has a central angle α, α of 30 o -150 o 。
7. The method according to claim 1, characterized in that the regenerated catalyst obtained by removing carbon deposits on the particles by the regeneration system is distributed in a ratio of (1-20): 1, preferably (5-15): 1 for the first partially regenerated catalyst and the second partially regenerated catalyst.
8. The method according to claim 1, characterized in that the light hydrocarbon-containing feedstock is a C4 blend, a C5-C6 light gasoline or a mixture thereof; preferably, the heavy oil feedstock has a proportion of C4 blends, C5-C6 light gasolines or mixtures thereof from the separation unit of greater than 20 wt.%; it is also preferred that the separation unit yields 30 wt% to 100 wt%, preferably 50 wt% to 100 wt%, of the C4 blend, C5-C6 light gasoline or mixture thereof for the heavy oil feedstock; for example, the entire C4 blend, C5-C6 light gasoline, or mixtures thereof from the separation unit is used as the entire heavy oil feedstock.
9. The method according to claim 1, characterized in that the mass ratio of heavy oil feedstock to light hydrocarbon-containing feedstock is (2-8): 1, preferably (3-6): 1.
10. The method according to claim 1, characterized in that:
the temperature of the catalyst bed layer of the fast bed reactor (3) is 550-650 ℃, the linear velocity of the gas of the catalyst bed layer is 1-3 m/s, and the density of the catalyst bed layer is 50-200 kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the And/or
The temperature of the catalyst at the outlet of the riser reactor (2) is 470-540 ℃, the linear velocity of the outlet gas is 10-25 m/s, and the density of the catalyst at the outlet is 5-50 kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The pressure in the mixed stripping zone (4) is 0.05-0.3MPaG.
CN202210251215.5A 2022-03-15 2022-03-15 Method for preparing ethylene propylene by catalytic cracking Pending CN116789510A (en)

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