CN109603695B - Separation system of slurry bed reactor - Google Patents
Separation system of slurry bed reactor Download PDFInfo
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- CN109603695B CN109603695B CN201910021907.9A CN201910021907A CN109603695B CN 109603695 B CN109603695 B CN 109603695B CN 201910021907 A CN201910021907 A CN 201910021907A CN 109603695 B CN109603695 B CN 109603695B
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- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
- B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
- C10G2/344—Apparatus, reactors with moving solid catalysts according to the "fluidised-bed" technique
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Abstract
A separation system of a slurry bed reactor relates to the technical field of gas-liquid-solid separation, and comprises a slurry bed reactor and a first separation device arranged in the slurry bed reactor; the first separation device is used for performing cyclone separation on airflow in the slurry bed reactor and then discharging the airflow out of the slurry bed reactor; the first separation device comprises at least two stages of cyclone separators, the air outlet of the previous stage of cyclone separator is communicated with the air inlet of the next stage of cyclone separator, and the air outlet of the last stage of cyclone separator is communicated to the outside of the slurry bed reactor. The separation system of slurry bed reactor of this application embodiment, it can carry out the inside air current of slurry bed reactor and discharge slurry bed reactor after cyclone, so, can reduce the solid matter and the liquid material that smuggle secretly in the air current that leaves slurry bed reactor.
Description
Technical Field
The application relates to the technical field of gas-liquid-solid separation, in particular to a separation system of a slurry bed reactor.
Background
Currently, Fischer-Tropsch (Fischer-Tropsch) synthesis technology is successfully applied in China. The fischer-tropsch synthesis technology consists mainly of 3 parts: firstly, a synthesis gas production technology; production technology of synthetic liquid hydrocarbon; and processing technology of synthetic products. The typical Fischer-Tropsch synthesis process flow is as follows: first, coal/natural gas is passed throughConverting into synthesis gas by chemical or partial oxidation and reforming, desulfurizing, deoxidizing and purifying the synthesis gas, and adjusting H according to the Fischer-Tropsch synthesis process condition and catalyst2The ratio of the carbon to the carbon monoxide is then fed into a Fischer-Tropsch synthesis reactor to prepare the mixed hydrocarbon. Finally, the synthetic product is separated, processed and modified to obtain different target products.
Because the Fischer-Tropsch synthesis is a strong exothermic reaction, the reaction heat must be removed in time in the reaction process, otherwise local hot spots are easy to appear in the bed layer, so that the catalyst is quickly deactivated and the selectivity of long-chain alkane products is reduced; in severe cases, instantaneous temperature runaway of the reactor can occur, and the plant has to be shut down. The use of slurry bed reactors is one of the effective solutions to this problem, especially for large industrial plants. However, slurry bed reactors also suffer from new problems during use.
Generally speaking, a slurry bed fischer-tropsch reactor is a gas-liquid-solid three-phase reactor, and the internal fluid properties are relatively complex. Unreacted gases and formed lower hydrocarbons and water exit the reactor through a reactor top outlet. After the catalyst in the reactor is broken and pulverized, the formed fine powder is easily carried away from the reactor from the top by high-temperature gas, and in addition, the catalyst with smaller particles is also easily carried away from the reactor from the top by the high-temperature gas, and particularly when the operation fluctuates. One of the problems to be solved is how to control the fine powder and even the catalyst particles not to be carried out of the reactor. In large industrial fischer-tropsch synthesis reactors, if the design is not reasonable or the operation is not good, the entrainment of liquid phase and catalyst in the gas phase stream at the upper part of the reactor will be excessive, which results in that the solid content in the condensed heavy oil separated by the product separation system is too high to be sent to a processing unit for further processing, especially when excessive foam and even flooding happen to the gas-liquid interface of the reactor. In the published reports, there is no reasonable solution to effectively solve the problem.
Disclosure of Invention
An embodiment of the application provides a separation system of a slurry bed reactor, which comprises a slurry bed reactor and a first separation device arranged in the slurry bed reactor; the first separation device is used for performing cyclone separation on airflow in the slurry bed reactor and then discharging the airflow out of the slurry bed reactor; the first separation device comprises at least two stages of cyclone separators, the air outlet of the previous stage of cyclone separator is communicated with the air inlet of the next stage of cyclone separator, and the air outlet of the last stage of cyclone separator is communicated to the outside of the slurry bed reactor.
Has the advantages that:
the separation system of slurry bed reactor of this application embodiment, it has set up multistage cyclone in slurry bed reactor's inside, and it can carry out the inside air current of slurry bed reactor and discharge slurry bed reactor after cyclone, so, the reducible solid matter and the liquid matter that smugglies in leaving slurry bed reactor's air current.
Drawings
The accompanying drawings are included to provide a further understanding of the claimed subject matter and are incorporated in and constitute a part of this specification, illustrate embodiments of the subject matter and together with the description serve to explain the principles of the subject matter and not to limit the subject matter.
FIG. 1 is a schematic diagram of a first separation device disposed in a slurry bed reactor in a separation system according to an embodiment of the present application;
FIG. 2 is a schematic top view of a first separation device disposed in a slurry bed reactor in a separation system according to an embodiment of the present application;
FIG. 3 is a schematic view of the first stage cyclone separator of the first separation device according to an embodiment of the present application;
FIG. 4 is a schematic top view of the structure of FIG. 3;
FIG. 5 is a schematic cross-sectional view of a first stage cyclone separator of a first separation device according to another embodiment of the present application;
FIG. 6 is a schematic view of a portion of a first stage cyclone separator of a first separation device according to yet another embodiment of the present application;
FIG. 7 is a schematic bottom view of the baffle assembly of FIG. 6;
FIG. 8 is a schematic diagram of a separation system according to an embodiment of the present application;
the reference signs are: 1. slurry bed reactor, 2, first separator, 3, gas outlet pipeline, 4, first heat exchanger, 5, gas-liquid separation tank, 6, second separator, 7, second heat exchanger, 8, oil-gas separation tank, 9, first stage cyclone separator, 10, second stage cyclone separator, 11, downcomer, 12, connecting pipeline, 13, cyclone separator, 14, shell, 15, gas inlet, 16, gas outlet, 17, slurry outlet, 18, upper cylinder, 19, lower cylinder, 20, roof, 21, exhaust pipe, 22, baffle component, 23, first baffle, 24, second baffle, 25, annular channel, 26, gas outlet, 27, downcomer, 28, gas inlet.
Detailed Description
The technical scheme of the application is further explained by the specific implementation mode in combination with the attached drawings. It is to be understood that the specific embodiments described herein are merely illustrative of the application and are not limiting of the application.
As shown in fig. 1, an embodiment of the present application provides a separation system of a slurry bed reactor, including a slurry bed reactor 1 and a first separation device 2 disposed in the slurry bed reactor 1; the first separation device 2 is used for performing cyclone separation on the airflow in the slurry bed reactor 1 and then discharging the airflow out of the slurry bed reactor 1; the first separation device 2 comprises at least two stages of cyclone separators 13, the air outlet of the previous stage of cyclone separator is communicated with the air inlet of the next stage of cyclone separator, and the air outlet of the last stage of cyclone separator is communicated to the outside of the slurry bed reactor 1.
The separation system of the slurry bed reactor of the embodiment of the present application, it has set up multistage cyclone 13 in slurry bed reactor 1's inside, and it can carry out the inside air current of slurry bed reactor 1 and discharge slurry bed reactor 1 after the cyclone, so, the reducible solid matter and the liquid substance that smugglies in leaving the air current of slurry bed reactor 1.
In this embodiment, the first separating device 2 may be provided with two, three or more stages of cyclones 13 according to the size of the slurry bed reactor 1, the amount of generated gas flow, and other factors, and the number of the cyclones 13 in each stage is not limited. The multi-stage cyclone separators 13 are used for separating liquid droplets, solid particles and powder entrained in the gas flow step by step, and the separated liquid and solid are returned to the slurry in the slurry bed reactor 1 from the slurry outlet of each cyclone separator 13.
As shown in fig. 2, the at least two-stage cyclone 13 includes, for example, a first-stage cyclone 9 and a second-stage cyclone 10, the number of the first-stage cyclones 9 is at least two, the number of the second-stage cyclones 10 is one, and an air outlet of the second-stage cyclone 10 is communicated to the outside of the slurry bed reactor 1.
The side wall of the cyclone separator 13 is provided with an air inlet 15, the air inlet 15 can be arranged along the tangential direction of the side wall of the cyclone separator 13, or the central axis of the air inlet 15 forms an included angle of 0-75 degrees with the tangential line of the side wall where the air inlet is located, the upper part of the cyclone separator 13 is provided with an air outlet 16, the lower part of the cyclone separator 13 is provided with a slurry outlet 17, and the slurry outlet 17 is a discharge port of solid particles, powder or/and liquid drops separated from the air flow. The gas flow enters the cyclone chamber inside the cyclone 13 through the gas inlet 15 of the cyclone 13, after cyclone separation in the cyclone chamber, the gas is discharged through the gas outlet 16 at the upper part, and the solid particles, powder or/and liquid drops separated from the gas flow are discharged from the slurry outlet 17 at the lower part. The cyclone chamber of the cyclone separator 13 is an area where the airflow is separated in a cyclone manner inside the cyclone separator.
The primary cyclone 9 and the secondary cyclone 10 are disposed in a gas phase region of the slurry bed reactor 1, such as an upper portion of the slurry bed reactor 1. In order to facilitate the gas flow in the slurry bed reactor 1 at all locations of the gas phase region to enter the first stage cyclone 9, the first stage cyclone 9 may be arranged along the circumferential direction of the inner wall of the slurry bed reactor 1, for example, may be arranged uniformly on a circumference. The number and the size of the first-stage cyclone separators 9 can be determined by calculation according to the size of the slurry bed reactor 1 and the outlet gas quantity of the reactor, such as 2-20. Supports for supporting and fixing the first stage cyclone 9 and the second stage cyclone 10 may be provided on the inner wall of the gas phase region of the slurry bed reactor 1.
The position of the air inlet of the second-stage cyclone separator 10 is higher than that of the air outlet of the first-stage cyclone separator 9, so that the air is discharged from the first-stage cyclone separator 9 and then upwards enters the second-stage cyclone separator 10. The second-stage cyclone separator 10 can be arranged above the first-stage cyclone separator 9, for example, the second-stage cyclone separator can be located at the center of the upper portion of the circumference of the first-stage cyclone separator 9, so that the gas discharged from each first-stage cyclone separator 9 can enter the second-stage cyclone separator 10 through the same path, the convergence and superposition of each gas flow in the second-stage cyclone separator 10 are facilitated, and the separation effect in the second-stage cyclone separator 10 is enhanced.
The number of the air inlets of the second-stage cyclone separators 10 is the same as that of the first-stage cyclone separators 9, and the air outlet of each first-stage cyclone separator 9 is communicated with the corresponding air inlet of the second-stage cyclone separator 10. In this way, the airflow discharged from the outlet of each first stage cyclone 9 can enter the second stage cyclone 10 from the corresponding inlet of the second stage cyclone 10. The second-stage cyclone separator 10 is provided with a plurality of air inlets, so that the air inlet area is increased, the air inlet efficiency is improved, the pressure loss of airflow caused by the flow resistance of the inlet can be reduced, and the separation efficiency is improved. The number of the air inlets of each first-stage cyclone separator 9 can be one or more, such as 1-2.
The air inlet of second level cyclone 10 can be followed second level cyclone 10's circumference sets up, for example, can evenly set up in the circumference of second level cyclone 10's lateral wall, also can be central symmetric distribution setting (can see fig. 2, 8 connecting tube 12 are connected with 8 air inlets that second level cyclone 10 circumference set up respectively, the other end of every connecting tube 12 is connected with the gas outlet of a first order cyclone 9, set up 8 first order cyclones 9 altogether), every air inlet sets up along the tangential direction of lateral wall, or is the same contained angle setting with the tangent line of lateral wall. Therefore, each air flow discharged from each first-stage cyclone separator 9 can enter the second-stage cyclone separator 10 from the corresponding air inlet of the second-stage cyclone separator 10 respectively, each air flow is converged with the air flow of the other air inlet of the second-stage cyclone separator 10 after rotating and flowing for the same distance along the inner wall of the cyclone cavity of the second-stage cyclone separator 10, the air flows are coupled and superposed during intersection, uniform, stable and enhanced flow is formed in the cyclone cavity of the second-stage cyclone separator 10, and the separation effect is further improved.
The slurry outlet 17 at the bottom of the cyclone 13 is connected with a downcomer, such as downcomer 27 at the bottom of the first stage cyclone 9 and downcomer 11 at the bottom of the second stage cyclone 10 shown in fig. 1. The bottom end of the downcomer extends into the slurry in the slurry bed reactor 1 and can extend to 0.3-3 m below the liquid level of the slurry. The bottom end of the downcomer (downcomer 27 or/and downcomer 11) is closed, the wall of the downcomer in the slurry is provided with openings, and the number of the openings can be set according to requirements, such as 3-8. The solids and/or liquids separated by cyclone 13 can exit through openings in the side wall of the downcomer into the slurry in reactor 1. The bottom end of the downcomer is closed, so that gas in slurry in the reactor 1 can be prevented from entering the downcomer from the bottom end of the downcomer and flowing upwards, and the solid or/and liquid separated by the cyclone separator 13 is prevented from flowing downwards along the downcomer.
The downcomer extends from a slurry outlet 17 at the bottom of the cyclone separator 13 to the inner wall of the slurry bed reactor 1, and then vertically extends downwards close to the inner wall of the slurry bed reactor 1 until the bottom end of the downcomer extends below the liquid level of the slurry in the slurry bed reactor 1. Thus, the obstruction of the gas flow in the slurry bed reactor 1 by the plurality of downcomers can be reduced.
With regard to the cyclones 13 of the first separating apparatus 2, the arrangement of the cyclones 13 of different stages may be the same or different, except for the number of inlets which may be arranged differently.
In the separation system of the embodiment of the application, the first separation device 2 adopts a one-to-many two-stage series connection cyclone design structure, and the second-stage cyclone 10 is provided with a plurality of air inlet structures, so that the effective air inlet area is increased, the air inlet efficiency is improved, the pressure drop is reduced, the separation efficiency is improved, the continuous operation time is greatly prolonged, and high efficiency, energy conservation (low resistance) and long-period safe operation can be realized.
The cyclone separator 13 comprises a shell 14, a rotational flow cavity is arranged in the shell 14, an air inlet 15 for introducing air flow into the rotational flow cavity is arranged on the shell 14, an air outlet 16 is arranged at the upper end of the rotational flow cavity, and a slurry outlet 17 is arranged at the lower end of the rotational flow cavity. The shape of the main body portion of the housing 14 may be an upper cylinder-lower cone, or the main body portion may be cylindrical as a whole. Wherein the gas flow is subjected to cyclone separation in the cyclone chamber, solid particles, powder or/and liquid droplets which are cyclone-separated from the gas flow are discharged from the slurry outlet 17, and the gas is discharged from the gas outlet 16.
As shown in fig. 3, 4 and 5, the cyclone separator 13 exemplarily includes a housing 14 and an exhaust pipe 21 disposed in the housing 14, the housing 14 includes a cylindrical upper cylinder 18, a conical lower cylinder 19 connected to the upper cylinder 18, and a top plate 20 connected to the top of the upper cylinder 18, and the top plate 20, the upper cylinder 18 and the lower cylinder 19 are welded together. The areas of the upper cylinder 18 and the lower cylinder 19 outside the exhaust pipe 21 constitute the cyclone chamber of the cyclone 13 of the present embodiment.
The exhaust pipe 21 may be welded to the top plate 20, and its upper end may extend out of the casing 14 from an opening provided in the top plate 20 (the opening may be provided at a central position of the top plate 20), and forms an air outlet of the cyclone 13, and its lower end is located in the upper cylinder 18. Or, the exhaust pipe 21 is completely located in the housing 14, the top plate 20 is provided with the air outlet 16, the air outlet 16 may be located at the center of the top plate 20, the upper end of the exhaust pipe 21 is welded on the top plate 20 and is communicated with the air outlet 16, and the lower end thereof is located in the upper cylinder 18. The exhaust pipe 21 may have a circular pipe structure, which is located on the central axis of the housing 14.
The outer wall of the upper cylinder 18 is provided with an air inlet 15 (the air inlet 15 may be a small section of air inlet pipeline arranged on the outer wall), and the air inlet 15 may be arranged along the tangential direction of the outer wall, or may be arranged to form an included angle of 0-75 degrees with the tangential line of the outer wall, that is, the included angle between the central axis of the air inlet 15 and the tangential line of the outer wall at the air inlet 15 is 0-75 degrees. The lower end of the lower cylinder 19 is provided with a slurry outlet 17.
Regarding the size of the cyclone separator, the height of the exhaust pipe 21 in the upper cylinder 18 is, for example, 60% to 100% of the height of the upper cylinder 18, the diameter of the exhaust pipe 21 is 20% to 70% of the diameter of the upper cylinder 18, and the height ratio of the upper cylinder 18 to the lower cylinder 19 is 0.6 to 1.2.
As another embodiment, reference may be made to the configuration of the second stage cyclone 10 of FIG. 1. The cyclone separator 13 comprises a shell 14 and an exhaust pipe 21 arranged in the shell 14, wherein the shell 14 comprises a cylinder main body, and an upper end enclosure and a lower end enclosure which are arranged at two ends of the cylinder main body and are respectively welded with the cylinder main body. The upper and lower heads may be elliptical heads, the exhaust pipe 21 is welded to the upper head, and its upper end extends out of the casing 14 through an opening in the upper head and forms an air outlet 16 of the cyclone separator 13. The outer wall of the cylinder main body is provided with an air inlet 15, and the bottom of the lower end enclosure is provided with a slurry outlet 17. The region inside the cylindrical body of the outer casing 14 of the exhaust pipe 21 constitutes the cyclone chamber of the cyclone 13 of the present embodiment. The exhaust pipe 21 can be a round pipe structure, and the depth of the exhaust pipe inserted into the shell 14 is 25% -75% of the height of the shell 14; the diameter of the exhaust pipe 21 may be 40% to 70% of the diameter of the cylinder main body. The upper end of an exhaust pipe 21 of the second-stage cyclone separator 10 can extend out of an opening at the top of the slurry bed reactor 1 and is connected with the gas outlet pipeline 3, and the diameter of the exhaust pipe 21 can be 70-110% of the diameter of the opening at the top of the slurry bed reactor 1. The cyclone separator of the present embodiment may be configured in the same manner as the cyclone separator shown in fig. 3 to 5 except that the shape of the housing 14 is different from that of the cyclone separator shown in fig. 3 to 5.
In order to reduce the secondary entrainment phenomenon in the cyclone separator 13, a baffle plate assembly 22 is arranged at the lower part in the cyclone cavity, the baffle plate assembly 22 comprises a first baffle plate 23, and an annular channel 25 is formed between the first baffle plate 23 and the wall of the cyclone cavity. Illustratively, as shown in fig. 5, the baffle assembly 22 is disposed in the conical lower cylinder 19, the baffle assembly 22 includes a first baffle 23, and an annular channel 25 is formed between the first baffle 23 and the inner wall of the lower cylinder 19, wherein the first baffle 23 may be a circular plate-shaped structure, and may be disposed horizontally, and the area of the first baffle 23 may be 1/4-3/4 of the cross-sectional area of the lower cylinder 19 at the same horizontal plane.
To further reduce the phenomenon of secondary entrainment, the baffle plate assembly 22 further comprises at least one second baffle plate 24, the second baffle plate 24 is disposed on the lower side of the first baffle plate 23, and the second baffle plate 24 is used for blocking the rotary motion of the airflow entering below the first baffle plate 23. Illustratively, as shown in fig. 6 and 7, one side of the second baffles 24 is fixed together, the other side is arranged in a dispersed manner, the upper ends of the second baffles 24 are fixed on the lower side of the first baffle 23, and the lower ends of the second baffles 24 are fixed on the casing 14 of the cyclone separator 13. Wherein the included angle between two adjacent second baffles 24 can be set to be the same or different, such as 25-120 degrees.
The airflow of the slurry leaving the slurry bed reactor 1 enters a cyclone cavity of the first-stage cyclone separator 9 through an air inlet on the side surface of the first-stage cyclone separator; because the liquid and solid particles or powder carried in the gas phase keep linear motion, the gas phase collides with the inner wall of the shell 14 and is resisted to slide; the light component mixed gas enters the cyclone cavity, wherein most of particles are in the outer area of the cyclone cavity, a few of particles with smaller particles rotate in the inner area of the cyclone cavity, the particles further accelerate downwards and then reach the bottom of the conical lower cylinder 19, most of gas turns back on the surface of the first baffle plate 23 of the baffle plate assembly 22 to form strong internal rotation upward gas flow, and finally enters the exhaust pipe 21 and leaves the cyclone separator 13 upwards. Thus, the secondary entrainment of the air flow to the particles caused by the air flow directly entering the bottom of the conical lower cylinder 19 can be avoided, and the separation efficiency of the cyclone separator 13 is improved; on the other hand, the air flow at the lower part of the lower cylinder 19 is reduced, which is beneficial to the sliding of the particles.
Liquid droplets and solid particles or powder in the gas stream are separated from the gas stream by centrifugal force, thrown against the wall of the cyclone 13, pass down the wall through the annular channel 25 between the first baffle 23 and the inner wall of the shell 14 into the bottom of the conical lower cylinder 19, and then return down the downcomer back into the slurry in the slurry bed reactor 1. The rest gas enters the bottom of the conical lower cylinder 19 from the annular channel 25 between the first baffle 23 and the inner wall of the shell 14, and due to the blocking effect of the second baffle 24, the gas entering the bottom of the lower cylinder 19 through the annular channel 25 loses the cyclone characteristic and is blocked by the first baffle 23 when turning back upwards, so that most of the gas moves downwards through the downcomer, and the secondary entrainment is further reduced.
In order to further separate and utilize energy of the airflow leaving the first separation device 2, the separation system further comprises a first heat exchanger 4 and a gas-liquid separation tank 5, wherein the first heat exchanger 4 is used for enabling the airflow discharged from the last stage cyclone separator to exchange heat with the gas entering the slurry bed reactor 1, and the gas-liquid separation tank 5 is used for collecting the airflow discharged from the last stage cyclone separator after the airflow is subjected to heat exchange through the first heat exchanger 4.
Some chemical reactions occurring in the slurry bed reactor 1 are exothermic reactions, the gas flow leaving the slurry bed reactor 1 has a higher temperature, and after the high-temperature gas flow is discharged from the first separation device 2, the temperature of the gas flow can be reduced through the heat exchange of the first heat exchanger 4, so that on one hand, high-boiling-point substances in the gas flow are condensed to form liquid drops with unseparated solid particles or powder, and then the liquid drops are separated from the gas flow in the gas-liquid separation tank 5, and on the other hand, the gas entering the slurry bed reactor 1 can be heated.
In order to further separate liquid drops or solid particles and powder carried in the airflow, a second separating device 6 is arranged in the gas-liquid separating tank 5, the second separating device 6 is used for performing cyclone separation on the airflow in the gas-liquid separating tank 5 and then discharging the airflow out of the gas-liquid separating tank 5, and the second separating device 6 comprises at least one stage of cyclone separator. The second separator 6 of the present embodiment is provided at an upper portion in the gas-liquid separation tank 5, and the liquid droplets, solid particles, and powder separated by the second separator 6 can be collected in the gas-liquid separation tank 5.
The second separating means 6 may be of the same construction as the first separating means 2, for example, two stages of cyclones may be provided, the first stage being provided in two or more stages and the second stage being provided in one stage. The structure and arrangement of the cyclones of the second separating means 6 can be as described with reference to the first separating means 2.
The gas flow from the first heat exchanger 4 can enter the gas-liquid separation tank 5 from an inlet arranged at the side part of the gas-liquid separation tank 5, after the condensed liquid drops in the gas flow are separated in the gas-liquid separation tank 5, the gas flow enters the second separation device 6 for separation, and is discharged out of the gas-liquid separation tank 5 after being separated by the second separation device 6.
In this embodiment, the separation system may further include a second heat exchanger 7 and an oil-gas separation tank 8, where the second heat exchanger 7 is configured to exchange heat between the gas flow discharged from the gas-liquid separation tank 5 and the gas entering the slurry bed reactor 1, and the oil-gas separation tank 8 is configured to collect the gas flow discharged from the gas-liquid separation tank 5 after the heat exchange by the second heat exchanger 7.
The gas stream exiting the knockout drum 5 may also have a relatively high temperature, and the temperature of the gas stream may be further reduced by the second heat exchanger 7 to condense the high boiling point materials in the gas stream and form liquid droplets with the unseparated solid particles or powder, and on the other hand, the gas entering the slurry bed reactor 1 may be preheated, and the gas is preheated by the second heat exchanger 7 and then sent to the first preheater. The oil-gas separation tank 8 is used for carrying out oil, water and gas three-phase separation, and gas discharged from the gas-liquid separation tank 5 enters the oil-gas separation tank 8 for carrying out oil, water and gas three-phase separation after exchanging heat through the second heat exchanger 7.
The separation system of this application embodiment can effectively solve and smuggly catalyst granule or powder in the high temperature oil gas that flows at 1 top of current industrial device slurry bed reactor many, leads to the obstructed difficult problem of separation system, is applicable to large-scale slurry bed ft synthesis device, can guarantee ft synthesis system's continuous stable operation.
An example of the separation system of the embodiment of the present application applied to a fischer-tropsch synthesis system is given below.
Referring to fig. 8 and 1, in the process of preparing mixed hydrocarbons from synthesis gas, there is H suitable for fischer-tropsch synthesis2The synthesis gas S3 having a/CO molar ratio is preheated to a predetermined temperature, enters the slurry bed reactor 1 from a reaction gas inlet at the bottom of the slurry bed reactor 1, passes through a gas distributor, becomes bubbles, is dispersed and ascended into the reactor (i.e., the slurry bed reactor 1), and contacts with catalyst particles suspended in liquid wax to react to produce hydrocarbon mixtures. The operating conditions of the reactor may be: the pressure is 1.5-4.0 MPa, the temperature is 190-310 ℃, and the fresh synthesis gas H2The mol ratio of/CO is 1.3-2.4. The mixture of light oil gas, water and unreacted synthetic gas and other high temperature oil gas formed in the reaction moves upwards after leaving the slurry. The high-temperature oil gas inevitably entrains a certain amount of liquid drops, catalyst particles or powder in the rising process. If a large amount of catalyst particles or powder is entrained by high-temperature gas from the top of the reactor and leaves the reactor, the solid content of condensed heavy oil separated by a product separation system is higher, the condensed heavy oil cannot be sent to a processing unit for further processing, and in addition, the entrained catalyst particles or powder not only aggravates the abrasion of a pipeline and a pump, but also is easy to deposit in the pipeline and separation equipment, and the stable operation of the device is influenced.
The high-temperature oil gas leaving the slurry firstly enters the first-stage cyclone separator 9 and enters the cyclone cavity of the first-stage cyclone separator 9 through the air inlet on the side surface of the first-stage cyclone separator; because the liquid, solid particles and powder carried in the gas phase keep linear motion, the gas phase touches the inner wall of the shell and slides down due to resistance; the light component gas mixture enters the cyclone cavity, wherein most of the particles are in the outer area of the cyclone cavity, and a few of the particles with smaller particles rotate in the inner area of the cyclone cavity, and further accelerate downwards to reach the bottom of the conical lower cylinder, most of the gas turns back on the surface of the first baffle plate 23 of the baffle plate assembly 22 to form strong internal rotation upward gas flow, and finally enters the exhaust pipe 21 and leaves the first-stage cyclone separator 9 upwards. Thus, the secondary entrainment of the air flow to the particles caused by the air flow directly entering the bottom of the conical lower cylinder 19 can be avoided, and the separation efficiency of the cyclone separator is improved; on the other hand, the air flow at the lower part of the lower cylinder 19 is reduced, which is beneficial to the sliding of the particles.
Liquid droplets and solid particles or powder in the gas stream are separated from the gas stream under the action of centrifugal force, thrown to the wall surface of the cyclone separator, pass through an annular channel 25 between the first baffle 23 and the inner wall of the shell 14 downwards along the wall surface to enter the bottom of the conical lower cylinder 19, and then return downwards along the downcomer to the slurry in the slurry bed reactor 1. The rest gas enters the bottom of the conical lower cylinder 19 from the annular channel 25 between the first baffle 23 and the inner wall of the shell 14, and due to the blocking effect of the second baffle 24, the gas entering the bottom of the lower cylinder 19 through the annular channel 25 loses the cyclone characteristic and is blocked by the first baffle 23 when turning back upwards, so that most of the gas moves downwards through the downcomer, and the secondary entrainment is further reduced.
The solid-liquid mixture and a part of entrained gas separated by the first stage cyclone 9 enter the downcomer 27 from the slurry outlet of the conical lower cylinder 19 and return downward to the slurry in the reactor 1. Most of the gas leaves the first stage cyclone 9 through the gas outlet at the top of the first stage cyclone 9 and enters the second stage cyclone 10. After separation in the second stage cyclone 10, it leaves the first separator means 2 upwardly from the outlet 26 at the top of the second stage cyclone 10 and exits the reactor 1. Wherein small amounts of liquid and solid particles or powder not separated in the first stage cyclone 9 are further separated in the second stage cyclone 10, thereby further reducing entrained liquid and solid particles or powder in the gas.
The high temperature oil gas S5 leaving the slurry bed reactor 1 enters the first heat exchanger 4. In the first heat exchanger 4, the high-temperature oil gas S5 exchanges heat with the circulating gas S3 entering the bottom of the slurry bed reactor 1 and is cooled, so that high-boiling-point substances in the high-temperature oil gas are condensed and form liquid drops with unseparated catalyst particles or powder. And simultaneously heating the circulating gas S3 to raise the temperature.
The oil gas S6 which is subjected to heat exchange and temperature reduction through the first heat exchanger 4 enters the gas-liquid separation tank 5 from the side, condensed liquid drops move downwards in the gas-liquid separation tank 5, and the oil gas enters the second separation device 6 upwards. After being separated by the second separation device 6, liquid drops, catalyst particles or powder in the oil gas are further separated, flow into the gas-liquid separation tank 5 through a downcomer, and are discharged from the bottom of the gas-liquid separation tank 5.
The oil gas S7 leaving the gas-liquid separation tank 5 enters the second heat exchanger 7. In the second heat exchanger 7, the oil gas S7 exchanges heat with the circulating gas S1 entering the second heat exchanger 7, the temperature is reduced, so that light oil and synthetic water in the oil gas are condensed, and meanwhile, the circulating gas S1 is preheated and heated.
And (3) sending the oil-water-gas mixture from the second heat exchanger 7 into an oil-gas separation tank 8, and performing oil-water-gas three-phase separation on the oil-water-gas mixture in the oil-gas separation tank 8 to obtain synthetic water S10, light oil S11 and Fischer-Tropsch synthesis tail gas S12.
In one embodiment, the operating conditions of the slurry bed reactor 1 are: the pressure is 3.0MPa, the temperature is 273 ℃, and the fresh synthesis gas H2The mol ratio of/CO is 1.9. 12 first-stage cyclone separators 9 of the first separation device 2 are symmetrically arranged, and 1 second-stage cyclone separator is arranged. The bottom of the exhaust pipe 21 of the first-stage cyclone separator 9 is inserted into the upper cylinder 18 to a depth of 70% of the height 18 of the upper cylinder; the diameter of the exhaust pipe 21 is 50% of the diameter of the upper cylinder 18. The height ratio of the upper cylinder 18 to the conical lower cylinder 19 was 0.9. The area of the first baffle 23 of the baffle assembly 22 is 3/4 of the cross-sectional area of the lower cylinder 19 on the same horizontal plane. The lower end of the downcomer is closed, the downcomer extends 1 meter below the level of the slurry in the reactor 1, and 4 rectangular openings are formed in the side wall of the lower end of the downcomer. And 1 gas inlet is formed in the side surface of the upper cylinder 18 of the first-stage cyclone separator 9, and the included angle between the gas flow direction of the inlet and the tangent line of the cylinder is 5 degrees. 12 uniformly distributed gas inlet pipes are arranged on the side surface of the shell of the second-stage cyclone separator 10 and are respectively communicated with the gas outlets at the top of the corresponding first-stage cyclone separator 9; the included angle between the flow direction of the inlet gas and the tangent line of the cylinder body is 15 degrees. The depth of the bottom of the exhaust pipe 21 of the second-stage cyclone separator 10 inserted into the separator shell is 45% of the height of the shell; the diameter of the exhaust pipe 21 is 55% of the diameter of the cylinder of the separator body and 100% of the diameter of the top opening of the slurry bed reactor 1. First separating means 6The number of the stage cyclone separators is 6, the number of the second stage cyclone separators is 1, and the structure and the arrangement form of the second stage cyclone separators are the same as those of the first separation device 2.
The high-temperature oil gas S5 exchanges heat with the circulating gas S3 flowing through the shell side of the first heat exchanger 4 through the tube side of the first heat exchanger 4. The temperature of oil gas S6 leaving the first heat exchanger 4 is controlled to be 160 ℃; the temperature of the recycle gas S3 entering the first heat exchanger 4 was 120 degrees.
The temperature of oil gas S7 leaving the gas-liquid separation tank 5 is controlled to 120 ℃. The oil gas S7 exchanges heat with the circulating gas S1 flowing through the shell side of the second heat exchanger 7 through the tube side of the second heat exchanger 7. The temperature of the oil-water-gas mixture S9 leaving the second heat exchanger 7 is controlled at 65 ℃.
In the above embodiment, when the high-temperature oil gas leaves the slurry bed reactor 1, the mass ratio of the entrained solid catalyst particles and powder to the total hydrocarbon is less than 0.01%; no solid particles or powder can be detected in the oil gas flowing out from the top of the gas-liquid separation tank 5.
The embodiment of the application clearly illustrates the advantages of the use method and the device of the separation system, the solid catalyst particles and powder carried by high-temperature oil gas are effectively removed, and the problem that the heat exchange device is frequently blocked in the conventional device is solved.
In the description of the embodiments of the present application, unless otherwise explicitly stated or limited, the terms "connected," "fixedly connected," "mounted," and "assembled" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; the terms "mounted," "connected," and "fixedly connected" may be directly connected or indirectly connected through intervening elements, or may be connected through the interconnection between two elements. Specific meanings of the above terms in the embodiments of the present application can be understood in specific cases by those of ordinary skill in the art.
Claims (11)
1. A separation system for a slurry bed reactor, characterized by: the device comprises a slurry bed reactor and a first separation device arranged in the slurry bed reactor;
the first separation device is used for performing cyclone separation on airflow in the slurry bed reactor and then discharging the airflow out of the slurry bed reactor;
the first separation device comprises at least two stages of cyclone separators, the air outlet of the previous stage of cyclone separator is communicated with the air inlet of the next stage of cyclone separator, and the air outlet of the last stage of cyclone separator is communicated to the outside of the slurry bed reactor;
the cyclone separator comprises a shell, a rotational flow cavity is arranged in the shell, an air inlet used for introducing airflow into the rotational flow cavity is arranged on the shell, an air outlet is arranged at the upper end of the rotational flow cavity, a slurry outlet is arranged at the lower end of the rotational flow cavity, a baffle plate assembly is arranged at the lower part in the rotational flow cavity and comprises a first baffle plate, and an annular channel is formed between the first baffle plate and the wall of the rotational flow cavity;
the cyclone separator also comprises an exhaust pipe arranged in the shell, the upper end of the exhaust pipe extends out of the shell to form an air outlet of the cyclone separator, and the lower end of the exhaust pipe is positioned in the shell; or the exhaust pipe is completely positioned in the shell, the upper end of the exhaust pipe is communicated with the air outlet, and the lower end of the exhaust pipe is positioned in the shell;
the exhaust pipe is used for exhausting the airflow which is formed by the gas in the cyclone cavity after being turned back by the first baffle and is in the strong inward rotation direction out of the cyclone separator;
the position of the air inlet on the shell is higher than the position of the lower end of the exhaust pipe;
the baffle plate assembly further comprises at least one second baffle plate, the second baffle plate is arranged on the lower side of the first baffle plate, and the second baffle plate is used for blocking the rotary motion of the airflow entering the lower portion of the first baffle plate;
it is a plurality of one side of second baffle is fixed together, and the another side is the dispersed form setting, and is a plurality of the upper end of second baffle is fixed the downside of first baffle, and is a plurality of the lower extreme of second baffle is fixed on the casing.
2. The separation system of claim 1, wherein: the at least two stages of cyclone separators comprise at least two first-stage cyclone separators and one second-stage cyclone separator, and the air outlet of each second-stage cyclone separator is communicated to the outside of the slurry bed reactor.
3. The separation system of claim 2, wherein: the number of the air inlets of the second-stage cyclone separators is consistent with that of the first-stage cyclone separators, and the air outlet of each first-stage cyclone separator is communicated with the corresponding air inlet of the second-stage cyclone separator.
4. The separation system of claim 3, wherein: and the air inlet of the second-stage cyclone separator is arranged along the circumferential direction of the second-stage cyclone separator.
5. The separation system of claim 2, wherein: the first-stage cyclone separator is arranged along the circumferential direction of the inner wall of the slurry bed reactor, and the position of the air inlet of the second-stage cyclone separator is higher than the position of the air outlet of the first-stage cyclone separator.
6. The separation system of claim 2, wherein: the side wall of the first-stage cyclone separator is provided with the air inlet, and the included angle between the central axis of the air inlet and the tangent line of the side wall at the air inlet is 0-75 degrees.
7. The separation system of claim 2, wherein: the slurry outlet at the bottom of the cyclone separator is connected with a downcomer, the bottom end of the downcomer extends into the slurry in the slurry bed reactor, the bottom end of the downcomer is closed, and an opening is formed in the pipe wall of the downcomer, which is positioned in the slurry.
8. The separation system of claim 2, wherein: the exhaust pipe is positioned on the central axis of the shell;
the shell comprises a cylindrical upper cylinder and a conical lower cylinder, the height of the exhaust pipe in the upper cylinder is 60% -100% of the height of the upper cylinder, the diameter of the exhaust pipe is 20% -70% of the diameter of the upper cylinder, and the height ratio of the upper cylinder to the lower cylinder is 0.6-1.2.
9. The separation system of claim 1, wherein: the separation system further comprises a first heat exchanger and a gas-liquid separation tank, the first heat exchanger is used for enabling the airflow discharged by the last-stage cyclone separator to exchange heat with the gas entering the slurry bed reactor, and the gas-liquid separation tank is used for collecting the airflow discharged by the last-stage cyclone separator after the airflow is subjected to heat exchange through the first heat exchanger.
10. The separation system of claim 9, wherein: and a second separation device is arranged in the gas-liquid separation tank, is used for performing cyclone separation on the gas flow in the gas-liquid separation tank and then discharging the gas flow out of the gas-liquid separation tank, and comprises at least one stage of cyclone separator.
11. The separation system of claim 9, wherein: the separation system further comprises a second heat exchanger and an oil-gas separation tank, wherein the second heat exchanger is used for enabling the airflow discharged by the gas-liquid separation tank to exchange heat with the gas entering the slurry bed reactor, and the oil-gas separation tank is used for collecting the airflow discharged by the gas-liquid separation tank after the heat exchange of the second heat exchanger.
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| CN111841161A (en) * | 2020-07-29 | 2020-10-30 | 濮阳市盛源能源科技股份有限公司 | Gas-liquid separation device and pressure removal reaction kettle |
| CN112619911A (en) * | 2020-11-13 | 2021-04-09 | 国家能源集团宁夏煤业有限责任公司 | Separating device |
| IT202100033044A1 (en) * | 2021-12-30 | 2023-06-30 | Versalis Spa | PROCEDURE FOR THE PYROLYSIS OF SUBSTANTIALLY PLASTIC MATERIAL OF NON-CONSTANT COMPOSITION, RELATED REACTOR, APPARATUS AND PRODUCT OBTAINED |
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| US4786400A (en) * | 1984-09-10 | 1988-11-22 | Farnsworth Carl D | Method and apparatus for catalytically converting fractions of crude oil boiling above gasoline |
| EP1512362A3 (en) * | 1999-07-27 | 2006-05-03 | G.B.D. Corporation | Apparatus and method for separating particles from a cyclonic fluid flow |
| CN1389446A (en) * | 2002-05-20 | 2003-01-08 | 清华大学 | Methane synthesizing method and equipment with slurry bed member |
| JP4444673B2 (en) * | 2004-01-08 | 2010-03-31 | ダイヤニトリックス株式会社 | Method for producing acrylonitrile |
| CN102009003B (en) * | 2009-09-07 | 2013-02-06 | 中国石油化工股份有限公司 | Slurry-bed reaction and separation system and method as well as application thereof in Fischer-Tropsch synthesis technology |
| CN102078784B (en) * | 2010-11-25 | 2012-12-12 | 浙江合盛硅业有限公司 | Spout type fluidized bed reactor for synthesis of organic silicon |
| CN102698662B (en) * | 2012-06-01 | 2015-02-04 | 神华集团有限责任公司 | Slurry bed reactor |
| CN102952596B (en) * | 2012-09-19 | 2014-07-02 | 赛鼎工程有限公司 | Process and device for synthesizing natural gas through methanation based on slurry bed |
| CN102921568A (en) * | 2012-10-18 | 2013-02-13 | 宝鸡石油机械有限责任公司 | Deep-sea underwater gas-liquid cyclone separator |
| CN103170284B (en) * | 2013-04-03 | 2016-02-17 | 神华集团有限责任公司 | Fischer-Tropsch synthesis system and process of high-temperature and high-pressure slurry bed reactor |
| CN104549566B (en) * | 2013-10-17 | 2017-07-25 | 中国石油化工股份有限公司 | Catalytic conversion catalyst regenerator and renovation process |
| CN104593047B (en) * | 2013-10-31 | 2016-03-23 | 中国石油化工股份有限公司 | A kind of adsorption desulfurize reaction unit and a kind of desulfurizing method by adsorption |
| CN106943965A (en) * | 2017-03-25 | 2017-07-14 | 青岛京润石化设计研究院有限公司 | A kind of gas-solid fluidized bed reactor gas-solid separating method |
| CN207981117U (en) * | 2018-01-23 | 2018-10-19 | 阳煤丰喜肥业（集团）有限责任公司 | A kind of non-pressure process melamine reactor internal cyclone structure |
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Address after: 100084 Tsinghua Yuan, Beijing, Haidian District Patentee after: TSINGHUA University Patentee after: National Energy Group Ningxia Coal Industry Co.,Ltd. Patentee after: Beijing low carbon clean energy Research Institute Address before: 100084 Tsinghua Yuan, Beijing, Haidian District Patentee before: TSINGHUA University Patentee before: SHENHUA NINGXIA COAL INDUSTRY GROUP Co.,Ltd. Patentee before: NATIONAL INSTITUTE OF CLEAN-AND-LOW-CARBON ENERGY |
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Address after: 168 Beijing Middle Road, Jinfeng District, Yinchuan City, Ningxia Hui Autonomous Region Patentee after: National Energy Group Ningxia Coal Industry Co.,Ltd. Patentee after: TSINGHUA University Patentee after: Beijing low carbon clean energy Research Institute Address before: 100084 Tsinghua Yuan, Beijing, Haidian District Patentee before: TSINGHUA University Patentee before: National Energy Group Ningxia Coal Industry Co.,Ltd. Patentee before: Beijing low carbon clean energy Research Institute |