CN215353341U - Petroleum hydrocarbon fluidized catalytic conversion reactor - Google Patents
Petroleum hydrocarbon fluidized catalytic conversion reactor Download PDFInfo
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- CN215353341U CN215353341U CN202121636469.6U CN202121636469U CN215353341U CN 215353341 U CN215353341 U CN 215353341U CN 202121636469 U CN202121636469 U CN 202121636469U CN 215353341 U CN215353341 U CN 215353341U
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Abstract
The utility model relates to a petroleum hydrocarbon fluidized catalytic conversion reactor, which is divided into two independently controlled reaction zones connected in series from top to bottom, wherein the lower part is a lower reaction zone (10), and the upper part is an upper reaction zone (20); the lower reaction zone (10) and the upper reaction zone (20) are vertically arranged coaxially and are communicated with each other, and the lower reaction zone (10) and/or the upper reaction zone (20) are/is in the form of a riser, a fast fluidized bed or a turbulent fluidized bed or a combination of the riser, the fast fluidized bed and the turbulent fluidized bed. The reactor provides a proper catalyst fluidization mode and independent reaction conditions for crude oil or raw materials with different components, and simultaneously realizes independent selective catalytic cracking of different raw materials in one reactor, and is particularly suitable for crude oil catalytic cracking.
Description
Technical Field
The utility model belongs to the field of petroleum refining, and relates to a fluidized catalytic conversion reactor for petroleum hydrocarbon, in particular to a reactor for preparing low-carbon olefin by fluidized catalytic conversion of petroleum hydrocarbon.
Background
The fluidized catalytic conversion of petroleum hydrocarbon is a typical gas-solid two-phase fluidized reaction process. A common reactor includes a riser. The riser and the turbulent fluidized bed are connected in series, and the riser and the fast fluidized bed are connected in series.
Due to the complex composition of petroleum hydrocarbon, various chemical substances of reactants, multiple chemical conversion levels in the reaction catalytic conversion process and large change of the performance of a catalyst in the reaction process, particularly for preparing low-carbon olefin by catalytic cracking, multi-level and multi-stage cracking from heavy components of crude oil to components C1 and C2 is required; different new reactant reactions formed in different reaction stages of raw oil, different reaction raw materials, different fluidization modes of catalysts required by different target products are different, for example, researches prove that the yield of propylene can be improved by adopting a turbulent fluidized bed for preparing propylene by catalytic conversion of micromolecule petroleum hydrocarbon; the heavy oil macromolecule cracking order is due to large coke formation amount, the actual reaction activity of the catalyst needs to be improved as much as possible, and a conveying bed, namely a riser mode, is needed; the low-temperature fast fluidized bed condition can well strengthen the olefin conversion of the gasoline stage components, reduce the olefin content of the gasoline components and not influence the gasoline yield; the gas yield can be obviously limited by the ultra-short reaction time of the downstream conveying bed; maximizing the fluidization patterns in the reactor with the reactant materials and the desired form of the reaction should be an important way to increase the efficiency of the reaction and improve the results.
Especially when reacting a plurality of distinctly different reaction raw materials, how to adapt the reactor to different raw materials poses an important problem; one effective solution is to provide a plurality of reactors, in which one material is reacted, but this results in a complicated apparatus;
particularly, when the small molecular raw materials such as naphtha rich in alkane, C4, C5 and the like are catalytically cracked by taking ethylene as a target product, higher reaction temperature is needed, such as above 650 ℃; the industrial device practice proves that the high-temperature reaction product of the catalytic cracking route has unstable property, and can generate obvious subsequent property change after leaving the reactor under the high-temperature condition, so that a small amount of coke is removed to form equipment coking, and in the steam cracking process, the coke is periodically switched and cleaned by the cracking furnace to solve the problem that the product is unstable and separates out coke in the cracking process, but the fluidized catalytic cracking can not adopt the mode of switching the reactor, and the instability of the high-temperature reaction product influences the normal operation of the device. The subsequent equipment structure caused by the unstable property of the high-temperature fluidized catalytic cracking product is a key problem for restricting the catalytic cracking quality of the low-carbon olefin.
Studies have shown that high boiling fraction petroleum hydrocarbons are more susceptible to catalytic cracking than small molecule petroleum hydrocarbons, and that the fast fluidized bed mode produces higher yields of propylene than the riser mode at the same reaction temperature.
SUMMERY OF THE UTILITY MODEL
The petroleum hydrocarbon is fluidized and catalytically cracked to prepare ethylene and propylene, which are one or several kinds of material, including crude oil, heavy oil, etc. and are cracked in several stages from macro molecule to C1 and C2 components to form several kinds of catalytic cracking reaction of the reactants.
The petroleum hydrocarbon comprises one or more of crude oil, heavy oil, VGO component, LCO component, HCO component, C5 and hydrocarbons with the following carbon numbers, hydrocarbons with the real boiling point of gasoline range, hydrocarbons with the real boiling point of naphtha component, hydrocarbons with the real boiling point of diesel oil component, hydrocarbons with the real boiling point of less than 180 ℃, or the above hydrocarbons;
the utility model provides a petroleum hydrocarbon fluidized catalytic conversion reactor, in particular to a reactor for preparing ethylene and propylene by composite catalytic cracking of different components formed in the reaction process of different raw materials or the same raw material, which adapts to the reaction requirements of different reactants by changing the fluidization mode of a catalyst in the reactor, is particularly suitable for preparing low-carbon olefin by direct catalytic cracking of crude oil, particularly the condition that a naphtha component and a heavy component are cracked respectively, so that the low-boiling-point component reacts under independent high-temperature conditions, and the heavy component or the high-boiling-point component reacts at a reaction temperature lower than that of the low-boiling-point component, thereby not only realizing the requirement of the catalytic cracking of the low-boiling-point component on the high reaction temperature, but also solving the problem of coking caused by unstable properties of the high-temperature cracking reaction product.
The utility model adopts the following technical scheme:
a petroleum hydrocarbon fluidized catalytic conversion reactor characterized by:
the reactor is divided into two independently controlled reaction zones which are connected in series up and down, the lower part is a lower reaction zone, and the upper part is an upper reaction zone; the lower reaction zone and the upper reaction zone are coaxially and vertically arranged and are communicated with each other; the lower reaction zone and/or the upper reaction zone are/is respectively in the form of a riser (or a conveying bed), a fast fluidized bed or a turbulent fluidized bed, or the combination of the riser, the fast fluidized bed and the turbulent fluidized bed;
a first regenerated catalyst or semi-regenerated catalyst inlet pipe is arranged at the lower part of the lower reaction zone to introduce the catalyst for the reaction in the lower reaction zone, so that a lower reaction zone for realizing the reaction catalyst, the catalyst-oil ratio and the temperature in the lower reaction zone is formed; the lower part of the upper reaction zone is provided with a second regenerated catalyst or semi-regenerated catalyst inlet pipe so as to introduce the catalyst for the reaction in the upper reaction zone and form an upper reaction zone which realizes the reaction catalyst, the catalyst-oil ratio and the temperature of the upper reaction zone different from those of the lower reaction zone; when the method is implemented specifically, catalysts required by reaction enter corresponding reaction zones from catalyst inlet pipes respectively, and the catalysts entering from the catalyst inlet pipes are regenerated catalysts or semi-regenerated catalysts; the lower reaction zone or/and the upper reaction zone can be provided with a catalyst or spent catalyst inlet after reaction, so that the catalyst or spent catalyst after reaction is introduced; a catalyst flow control valve, commonly called a slide valve, is arranged at a catalyst inlet pipe;
or the upper reaction zone is divided into a fast fluidized bed or turbulent fluidized bed reaction zone in the form of a fast fluidized bed and a riser reaction zone B in the form of a riser from bottom to top, and a second regenerated catalyst or semi-regenerated catalyst inlet pipe is arranged on the shell of the fast fluidized bed or turbulent fluidized bed reaction zone;
or the upper reaction zone is arranged from bottom to top in a riser reaction zone C in the form of a riser, a rapid fluidized bed or turbulent fluidized bed reaction zone in the form of a rapid fluidized bed or turbulent fluidized bed, and a riser reaction zone B in the form of a riser in series; the second regenerated catalyst or semi-regenerated catalyst inlet pipe is arranged on the shell of the riser reaction zone C or the fast fluidized bed or the turbulent fluidized bed reaction zone;
the lower reaction zone is provided with a liquid or gas material or reaction raw material inlet, or the lower reaction zone and the upper reaction zone are respectively provided with a liquid or gas material or reaction raw material inlet; one or more liquid or gas material or reaction raw material inlets are arranged in the lower reaction zone or the upper reaction zone; when a plurality of liquid or gas material or reaction raw material inlets are arranged in the lower reaction zone or the upper reaction zone, the liquid or gas material or reaction raw material inlets are preferably arranged in a layered manner; in specific implementation, when the upper reaction zone is provided with a liquid or gas material or reaction raw material inlet, the liquid or gas material or reaction raw material inlet is arranged below or above the second regenerated catalyst or semi-regenerated catalyst inlet pipe, and is preferentially arranged below the second regenerated catalyst or semi-regenerated catalyst inlet pipe;
the liquid or gas material or reaction raw material II introduced into the upper reaction zone reacts in the upper reaction zone, and the liquid or gas material or reaction raw material I introduced into the lower reaction zone reacts in the lower reaction zone and the upper reaction zone respectively; the lower reaction zone is provided with a temperature thermocouple, and the thermocouple signal is interlocked with the opening degree of a catalyst slide valve I on a first regenerated catalyst or semi-regenerated catalyst inlet pipe so as to realize the independent control of the reaction temperature of the lower reaction zone by controlling the catalyst flow; the temperature thermocouple is arranged in the upper reaction zone or the fast fluidized bed or turbulent fluidized bed reaction zone or the riser reaction zone B of the upper reaction zone, and the thermocouple signal is interlocked with the opening degree of a catalyst slide valve II on a second regenerated catalyst or semi-regenerated catalyst inlet pipe so as to realize the independent control of the temperature of the upper reaction zone or the fast fluidized bed or turbulent fluidized bed reaction zone by controlling the catalyst flow; in specific implementation, the catalyst slide valve II controls the flow of the catalyst to further provide heat for the upper reaction zone, so that the reaction temperature of the upper reaction zone is higher than that of the lower reaction zone.
In the above-mentioned petroleum hydrocarbon fluidized catalytic conversion reactor, preferably, the lower reaction zone is composed of a turbulent fluidized bed reaction zone in the form of a turbulent fluidized bed and a riser reaction zone a in the form of a riser from bottom to top in series; a first regenerated catalyst or semi-regenerated catalyst inlet pipe is disposed on the turbulent fluidized bed reaction zone housing. In specific implementation, the lower reaction zone is composed of a reaction zone designed according to the conditions of a turbulent fluidized bed or a fast fluidized bed and a conveying bed, namely a riser, which are connected in series from bottom to top; the uniform mixing characteristic of the catalyst in the turbulent fluidized bed or the fast fluidized bed in the reaction process is favorable for realizing the cracking of liquid or gas materials or reaction raw materials under the average catalyst condition after the coke is generated in the reaction, the yield of propylene is increased, and the reaction temperature of the liquid or gas materials or reaction raw materials is also favorable for reducing; in specific practice, the liquid or gaseous feed or reactant material inlet is provided at the bottom of the lower reaction zone or around the shell.
In the above-mentioned reactor for fluidized catalytic conversion of petroleum hydrocarbon, preferably, the temperature thermocouple disposed in the lower reaction zone is disposed in the turbulent fluidized bed reaction zone or the riser reaction zone a, and the thermocouple signal is linked with the opening of the catalyst slide valve i, so as to realize independent control of the temperature in the lower reaction zone or the turbulent fluidized bed reaction zone by controlling the flow rate of the catalyst.
In the above-mentioned fluidized catalytic conversion reactor for petroleum hydrocarbon, preferably, a porous partition plate is arranged between the lower reaction zone and the upper reaction zone, or a porous partition plate is arranged at the bottom of the reaction zone of the fast fluidized bed or turbulent fluidized bed in the upper reaction zone, so that the catalyst and gas in the lower reaction zone can enter the upper reaction zone through the openings of the porous partition plate. In specific implementation, the porous partition is designed according to the flow velocity of gas passing through the open pores is not more than 40 m/s.
In the above-mentioned petroleum hydrocarbon fluidized catalytic conversion reactor, when the reaction raw material is in a gaseous state or enters the lower reaction zone or the turbulent fluidized bed reaction zone after gasification, the inlet of the liquid or gaseous material or the reaction raw material i is arranged at the bottom of the lower reaction zone or the turbulent fluidized bed reaction zone, preferably, a tubular distributor or a distribution plate (i.e. a tubular or plate distributor) is arranged in the lower reaction zone or the turbulent fluidized bed reaction zone, so that the reaction raw material is uniformly distributed in the catalyst in the lower reaction zone or the turbulent fluidized bed reaction zone; and a shell positioned below the tubular distributor or the distribution plate in the lower reaction zone is provided with a liquid or gas material or reaction raw material I inlet.
In the above-mentioned petroleum hydrocarbon fluidized catalytic conversion reactor, preferably, the lower reaction zone is provided with a steam inlet, or the lower reaction zone and the upper reaction zone are respectively provided with a steam inlet.
In the above-mentioned petroleum hydrocarbon fluidized catalytic conversion reactor, preferably, the lower reaction zone is provided with C5 and below carbon number hydrocarbon inlets, or the lower reaction zone and the upper reaction zone are respectively provided with C5 and below carbon number hydrocarbon inlets.
In the above-mentioned petroleum hydrocarbon fluidized catalytic conversion reactor, preferably, the lower reaction zone and/or the upper reaction zone is provided with a water or quenching medium inlet; the water or quenching medium inlet is arranged at the outlet of the lower reaction zone or the upper reaction zone.
When the utility model is implemented, the reaction zone of the turbulent fluidized bed is designed according to the gas apparent flow velocity not more than 4.5 m/s; the fast fluidized bed or turbulent fluidized bed reaction zone is designed for a gas superficial velocity of 0.2m/s to 4.5m/s, preferably for a gas superficial velocity of 0.6m/s to 4.5 m/s.
Although not limited, when a plurality of reaction raw materials are used, it is preferable that the upper reaction zone is used for the reaction of the high boiling point component and the lower reaction zone is used for the reaction of the component having a boiling point of the major component lower than 300 ℃.
The technical personnel are familiar with the problems of arranging heat insulation, wear-resistant lining, manhole and supporting seat in the reactor.
The utility model provides different reaction conditions for different reaction raw materials with different properties or different reactants formed in different reaction stages of the same raw material in the same reactor by optimizing the structure of the reactor, and the reaction conditions are independently controlled; particularly, the reaction conditions of different components are mutually complemented by reasonably controlling the difference of the reaction conditions needed by the high-boiling-point component and the micromolecule, thereby not only ensuring the yield of the target product, but also solving the problem of instability of the high-temperature cracking product.
Drawings
FIG. 1 is a schematic view of an embodiment of the present invention;
FIG. 2 is a schematic view of a second embodiment of the present invention;
the actual implementation is not limited to the schematic form.
The numbering marks in the figure are as follows:
a lower reaction zone 10, a liquid or gas material or reaction raw material I (introduced into the lower reaction zone), a first regenerated catalyst or semi-regenerated catalyst inlet pipe (or called catalyst inlet pipe of the lower reaction zone), a tubular distributor or distribution plate 13, a liquid or gas material or reaction raw material I inlet, a turbulent fluidized bed reaction zone 15, a riser reaction zone A (or called transport bed A) 16, a catalyst slide valve I and a catalyst slide valve I are arranged in the upper reaction zone respectively; 20 upper reaction zone, 21 (introduced into the upper reaction zone) liquid or gaseous feed or reaction feed ii; 22 a second regenerated catalyst or semi-regenerated catalyst inlet pipe (or referred to as a reaction zone catalyst inlet pipe), 25 a fast fluidized bed or turbulent fluidized bed reaction zone, 26 a riser reaction zone B (or referred to as a transport bed B), 27 a riser reaction zone C (or referred to as a transport bed C), 28 a catalyst slide valve II; TIC temperature indicates the control signal.
Detailed Description
The following description is made by way of example and not by way of limitation with reference to the accompanying drawings.
The first implementation mode comprises the following steps:
as shown in fig. 1, a fluidized catalytic conversion reactor for petroleum hydrocarbon, which is divided into two independently controlled reaction zones connected in series, wherein the lower part is a lower reaction zone 10, the upper part is an upper reaction zone 20, and the lower reaction zone 10 and the upper reaction zone 20 are arranged coaxially and vertically and are communicated with each other;
the lower reaction zone 10 is composed of a turbulent fluidized bed reaction zone 15 in a turbulent fluidized bed form and a riser reaction zone A16 in a riser form in series from bottom to top, a shell of the turbulent fluidized bed reaction zone 15 is provided with a first regenerated catalyst or semi-regenerated catalyst inlet pipe, and a first regenerated catalyst or semi-regenerated catalyst inlet pipe 12 is provided with a catalyst slide valve I18; a tubular distributor or a distribution plate 13 is arranged in a turbulent fluidized bed reaction zone 15, a shell below the tubular distributor or the distribution plate 13 is provided with a liquid or gas material or reaction raw material I inlet 14, and a liquid or gas material or reaction raw material I11 is introduced into a lower reaction zone 10; a flow temperature thermocouple is arranged in the riser reaction zone A16, and the thermocouple signal is interlocked with the opening degree of the catalyst slide valve I18 so as to realize independent control of the temperature of the lower reaction zone 10 or the turbulent fluidized bed reaction zone 15 by controlling the flow of the catalyst;
the lower part of the upper reaction zone 20 is provided with a second regenerated catalyst or semi-regenerated catalyst inlet pipe 22, the second regenerated catalyst or semi-regenerated catalyst inlet pipe 22 is provided with a catalyst slide valve II 28, the upper reaction zone 20 is divided into a fast fluidized bed or turbulent fluidized bed reaction zone 25 (expanding zone) in the form of a fast fluidized bed and a riser reaction zone B26 in the form of a riser from bottom to top, and the second regenerated catalyst or semi-regenerated catalyst inlet pipe 22 is arranged on the shell of the fast fluidized bed or turbulent fluidized bed reaction zone 25; a porous partition plate 19 is arranged at the bottom of a reaction area 25 of the fast fluidized bed or the turbulent fluidized bed, and a liquid or gas material or reaction raw material II 21 is introduced above the porous partition plate 19; a flow temperature thermocouple is arranged in the riser reaction zone B26, and the thermocouple signal is interlocked with the opening degree of the catalyst slide valve II 28 so as to realize independent control of the temperature of the upper reaction zone 20 by controlling the flow of the catalyst;
in specific implementation, the liquid or gas material or reaction raw material II 21 introduced into the upper reaction zone 20 reacts in the upper reaction zone 20, and the liquid or gas material or reaction raw material I11 introduced into the lower reaction zone 10 reacts in the lower reaction zone 10 and the upper reaction zone 20 respectively; liquid or gas materials or reaction raw materials I11 enter a lower reaction zone 10 from a liquid or gas material or reaction raw material I inlet 14, are uniformly distributed in a catalyst entering a turbulent fluidized bed reaction zone 15 from a first regenerated catalyst or semi-regenerated catalyst inlet pipe 12 through a tubular distributor or distribution plate 13, and sequentially react in the turbulent fluidized bed reaction zone 15 and a riser reaction zone A16 to realize the cracking of the liquid or gas materials or reaction raw materials 11 under the condition of average catalyst after coke generation by reaction, and in the reaction process, the opening degree of a catalyst slide valve I18 is controlled to control the flow of the catalyst, so that the independent control of the temperature of the lower reaction zone 15 or turbulent fluidized bed reaction zone 15 is realized; the catalyst and gas reacted in the lower reaction zone 10 enter the upper reaction zone 20 through the openings of the porous partition plate 19 to continue reacting along the fast fluidized bed or turbulent fluidized bed reaction zone 25 and the riser reaction zone B26, the second regenerated catalyst or semi-regenerated catalyst enters the fast fluidized bed or turbulent fluidized bed reaction zone 25 along the second regenerated catalyst or semi-regenerated catalyst inlet pipe 22, meanwhile, the liquid or gas material or reaction raw material II 21 enters the upper reaction zone 20, the catalyst flow is controlled by the catalyst slide valve II 28 to provide heat for the upper reaction zone 20, and the reaction temperature of the upper reaction zone 20 is higher than that of the lower reaction zone 10; the reacted product and catalyst flow out of the reactor.
Example 1:
the reactor is used for preparing ethylene and propylene by catalytic cracking of crude oil at 300t/h, the reaction raw material of the lower reaction zone is naphtha separated from the crude oil and other gas components at 45t/h, and the reaction raw material of the upper reaction zone is a mixture of other components at 255 t/h; the reaction raw materials in the lower reaction zone are in a gas state; the reactor of FIG. 1 was used.
The inner diameter of a catalyst inlet pipe 12 is 1200mm, the inner diameter of a turbulent fluidized bed reaction zone 15 is 3000mm, the height of the turbulent fluidized bed reaction zone is 2000mm, and the diameter of a riser reaction zone A16 (a conveying bed) is 600mm, and the height of the riser reaction zone A is 6000 mm; the diameter of the fast fluidized bed reaction zone 25 is 5000mm, the height is 3500mm, and the diameter of the riser reaction zone B26 is 2000 mm; the aperture ratio of the distribution plate 13 is 3 percent, and the aperture is 100 mm; catalyst inlet tube 22 diameter 1300 mm; the diameter of the opening of the partition 19 was 80mm, and the flow rate of the gas passing therethrough was 17 m/s.
The equipment shell is internally provided with a heat-insulating wear-resistant lining.
The second embodiment:
as shown in FIG. 2, the reactor is divided into two independently controlled reaction zones connected in series, the lower part is a lower reaction zone 10, the upper part is an upper reaction zone 20, the upper reaction zone 20 is arranged from bottom to top in the form of a riser reaction zone C27, a fast fluidized bed or turbulent fluidized bed reaction zone 25, and a riser reaction zone B26 connected in series; a second regenerated or semi-regenerated catalyst inlet pipe 22 is disposed in the shell of the riser reaction zone C27; introducing a liquid or gas material or reaction raw material II 21 below a second regenerated catalyst or semi-regenerated catalyst inlet pipe 22;
the other parts of the device structure are the same as the first embodiment.
Example 2:
the reactor shown in FIG. 2 is used for preparing ethylene and propylene by catalytic cracking of crude oil, the diameter of a riser reaction zone C27 is 1600mm, and a partition plate 19 is not arranged between a lower reaction zone 10 and an upper reaction zone 20. The rest is the same as in example 1.
Claims (8)
1. A petroleum hydrocarbon fluidized catalytic conversion reactor characterized by:
the reactor is divided into two independently controlled reaction zones which are connected in series, the lower part is a lower reaction zone (10), and the upper part is an upper reaction zone (20); the lower reaction zone (10) and the upper reaction zone (20) are vertically arranged coaxially and vertically and are communicated with each other; the lower reaction zone (10) and/or the upper reaction zone (20) are/is in the form of a riser, a fast fluidized bed, or a turbulent fluidized bed, or a combination of the forms of a riser, a fast fluidized bed, and a turbulent fluidized bed, respectively;
a first regenerated catalyst or semi-regenerated catalyst inlet pipe (12) is arranged at the lower part of the lower reaction zone (10) to introduce the catalyst for the reaction in the lower reaction zone (10) to form the lower reaction zone (10) for realizing the reaction catalyst, the catalyst-oil ratio and the temperature in the lower reaction zone (10); a second regenerated catalyst or semi-regenerated catalyst inlet pipe (22) is arranged at the lower part of the upper reaction zone (20) to introduce the catalyst for the reaction of the upper reaction zone (20) to form the upper reaction zone (20) which realizes the reaction catalyst, the catalyst-oil ratio and the temperature of the upper reaction zone (20) different from those of the lower reaction zone (10);
or the upper reaction zone (20) is divided into a fast fluidized bed or turbulent fluidized bed reaction zone (25) in the form of a fast fluidized bed and a riser reaction zone B (26) in the form of a riser from bottom to top, and a second regenerated catalyst or semi-regenerated catalyst inlet pipe (22) is arranged on the shell of the fast fluidized bed or turbulent fluidized bed reaction zone (25);
or the upper reaction zone (20) is arranged from bottom to top in the form of a riser reaction zone C (27) in the form of a riser, a fast fluidized bed or turbulent fluidized bed reaction zone (25) in the form of a fast fluidized bed or turbulent fluidized bed, and a riser reaction zone B (26) in the form of a riser in series; a second regenerated catalyst or semi-regenerated catalyst inlet pipe (22) is arranged on the shell of the riser reaction zone C (27) or the fast fluidized bed or turbulent fluidized bed reaction zone (25);
the lower reaction zone (10) is provided with a liquid or gas material or reaction raw material inlet, or the lower reaction zone (10) and the upper reaction zone (20) are respectively provided with a liquid or gas material or reaction raw material inlet; one or more liquid or gas material or reaction raw material inlets are arranged in the lower reaction zone (10) or the upper reaction zone (20); when a plurality of liquid or gas material or reaction raw material inlets are arranged in the lower reaction zone (10) or the upper reaction zone (20), the liquid or gas material or reaction raw material inlets are arranged in a layered manner;
the lower reaction zone (10) is provided with a temperature thermocouple, and the thermocouple signal is interlocked with the opening degree of a catalyst slide valve I (18) on a first regenerated catalyst or semi-regenerated catalyst inlet pipe (12) so as to realize the independent control of the reaction temperature of the lower reaction zone (10) by controlling the catalyst flow rate; the upper reaction zone (20) or the fast fluidized bed or turbulent fluidized bed reaction zone (25) or the riser reaction zone B (26) is provided with a temperature thermocouple, and the thermocouple signal is interlocked with the opening degree of a catalyst slide valve II (28) on a second regenerated catalyst or semi-regenerated catalyst inlet pipe (22) so as to realize independent control of the temperature of the upper reaction zone (20) or the fast fluidized bed or turbulent fluidized bed reaction zone (25) by controlling the flow rate of the catalyst.
2. A petroleum hydrocarbon fluidized catalytic conversion reactor as defined in claim 1, wherein: the lower reaction zone (10) is formed by connecting a turbulent fluidized bed reaction zone (15) in a turbulent fluidized bed form and a riser reaction zone A (16) in a riser form in series from bottom to top; a first regenerated catalyst or semi-regenerated catalyst inlet pipe (12) is disposed on the shell of the turbulent fluidized bed reaction zone (15).
3. A petroleum hydrocarbon fluidized catalytic conversion reactor as defined in claim 2, wherein: the temperature thermocouple arranged in the lower reaction zone (10) is arranged in the turbulent fluidized bed reaction zone (15) or the riser reaction zone A (16), and the signal of the thermocouple is interlocked with the opening degree of the catalyst slide valve I (18) so as to realize the independent control of the temperature of the lower reaction zone (10) or the turbulent fluidized bed reaction zone (15) by controlling the flow rate of the catalyst.
4. A petroleum hydrocarbon fluidized catalytic conversion reactor as defined in claim 1, wherein: a porous partition (19) is provided between the lower reaction zone (10) and the upper reaction zone (20), or a porous partition (19) is provided at the bottom of the fast fluidized bed or turbulent fluidized bed reaction zone (25) of the upper reaction zone (20), to allow the catalyst and gas of the lower reaction zone (10) to pass through the openings of the porous partition (19) into the upper reaction zone (20).
5. A petroleum hydrocarbon fluidized catalytic conversion reactor as claimed in claim 1 or claim 2, wherein: a tubular distributor or a distribution plate (13) is arranged in the lower reaction zone (10) or the turbulent fluidized bed reaction zone (15) so as to uniformly distribute reaction raw materials in the catalyst in the lower reaction zone (10) or the turbulent fluidized bed reaction zone (15); an inlet (14) for liquid or gaseous material or reaction raw material I is arranged on the shell of the lower reaction zone (10) below the tubular distributor or distribution plate (13).
6. A petroleum hydrocarbon fluidized catalytic conversion reactor as defined in claim 1, wherein: the lower reaction zone (10) is provided with a steam inlet, or the lower reaction zone (10) and the upper reaction zone (20) are respectively provided with a steam inlet.
7. A petroleum hydrocarbon fluidized catalytic conversion reactor as defined in claim 1, wherein: the lower reaction zone (10) is provided with hydrocarbon inlets with carbon number of C5 and below, or the lower reaction zone (10) and the upper reaction zone (20) are respectively provided with hydrocarbon inlets with carbon number of C5 and below.
8. A petroleum hydrocarbon fluidized catalytic conversion reactor as defined in claim 1, wherein: the lower reaction zone (10) and/or the upper reaction zone (20) is provided with a water or quenching medium inlet; the water or quenching medium inlet is arranged at the outlet of the lower reaction zone (10) or the upper reaction zone (20).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253934A (en) * | 2022-07-18 | 2022-11-01 | 中国石油大学(北京) | Propane catalytic dehydrogenation fluidized bed reaction-regeneration coupling device and propane catalytic dehydrogenation process method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253934A (en) * | 2022-07-18 | 2022-11-01 | 中国石油大学(北京) | Propane catalytic dehydrogenation fluidized bed reaction-regeneration coupling device and propane catalytic dehydrogenation process method |
| CN115253934B (en) * | 2022-07-18 | 2023-10-24 | 中国石油大学(北京) | Propane catalytic dehydrogenation fluidized bed reaction-regeneration coupling device and propane catalytic dehydrogenation process method |
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