Spiral fluidized slurry bed reactor

Abstract

The present invention provides a spiral flow slurry bed reactor, which comprises a reactor shell, a slurry inlet and outlet located at the bottom of the shell, a gas outlet located at the top of the shell, and a gas-liquid separator, a heat exchange tube set and a gas distributor located in the internal space surrounded by the shell. The present invention achieves significant improvement in gas-liquid mass transfer and heat transfer effects by specially designing the structure of the heat exchange tube set and / or the gas distributor, thereby improving the Fischer-Tropsch reaction efficiency.

Description

Technical Field

[0001] The invention belongs to the field of chemical equipment and devices, and specifically relates to a slurry bed reactor. The slurry bed reactor is provided with a structure capable of generating a spiral flow, which can guide the gas-liquid fluid in the reactor to have an efficient internal circulation. Background Art

[0002] In the fields of chemical industry, bioengineering, environmental protection, etc., it is often necessary to carry out chemical reactions, bioengineering cultivation and other processes in a multiphase reaction system where gaseous, liquid and solid materials coexist. Specific examples of these processes may include biological fermentation, wastewater treatment, tail gas treatment, chemical synthesis, etc., wherein the gaseous and liquid materials used may include various reactants and process aids, and the solid paste may be either a reactant, a culture substrate, or a reaction catalyst or other process aid. These biological or chemical processes are usually carried out using various three-phase reactors, such as stirred bubbling tank reactors, bubbling tower reactors, plate reactors, packed tower reactors, tubular reactors, jet reactors, etc., among which the most important reactor is a bubbling reactor, such as a slurry bed reactor.

[0003] The main problem of the slurry bed reactor is that the uniformity of the overall material concentration and flow rate distribution is difficult to control, and there may be unavoidable and difficult to control turbulence and back mixing in some areas. There may also be dead zones. The above-mentioned uniform mass transfer and uniform heat transfer problems have a great adverse effect on the quality of the process products and the daily operation and maintenance of the slurry bed. In order to overcome the above problems, a lot of research has been conducted on slurry bed reactors so far. The specific means adopted are nothing more than setting more nozzles, baffles, heat exchange pipes, reflux circulation structures, etc. at different positions in the reactor to improve the material circulation and energy exchange at various locations inside the slurry bed reactor. Although the above-mentioned improvement methods can alleviate the existing problems to a certain extent, these additional components will significantly increase the complexity of the design and operation of the slurry bed reactor, resulting in a substantial increase in infrastructure and daily maintenance costs. In addition, these newly added components will introduce many new obstruction sites inside the reactor, and may even bring new adverse effects to the mass transfer and heat transfer in the reactor, bringing new problems while solving the original problems. The result of continuing with this research and development approach based on existing technology is that technicians need to monitor and adjust more and more parameters when operating the equipment, the complexity of the reaction system becomes increasingly higher, but in fact the improvement effect on overall mass transfer and heat transfer is very limited.

[0004] In order to solve the above problems, the inventors of the present application have conducted a lot of research and found that by specially designing the structure of the distributor, the draft tube, and / or the heat exchanger, the overall uniformity of mass transfer and heat transfer in the slurry bed reactor can be significantly improved, the contact and interaction (chemical reaction, biochemical reaction, biological action, physical adsorption, etc.) between the gas, liquid and solid phases can be effectively improved, and the back mixing and dead zone problems can be eliminated or greatly reduced. Based on the above research results, the technical purpose of the present invention is achieved. Summary of the invention

[0005] According to a first aspect of the present invention, a spiral flow slurry bed reactor is provided, the slurry bed reactor comprising a reactor shell, a slurry inlet and outlet at the bottom of the shell, a gas outlet at the top of the shell, a gas-liquid separator, a heat exchange tube assembly and a gas distributor located in the internal space surrounded by the shell, wherein:

[0006] The heat exchange tube set comprises a coolant inlet, a coolant outlet, a flow guiding cylindrical heat exchange tube set and one or more groups of spiral plate heat exchange tube sets, and the flow guiding cylindrical heat exchange tube set and the spiral plate heat exchange tube set are fluidly connected.

[0007] According to one embodiment of the present invention, the guide cylinder heat exchange tube assembly is generally cylindrical, and its cylindrical wall includes 3 to 100 guide cylinder heat exchange tubes, each of which is distributed in a spiral shape around the longitudinal center axis of the guide cylinder heat exchange tube assembly.

[0008] According to another embodiment of the present invention, the guide tube heat exchange tube assembly has a top heat exchange tube ring and a bottom heat exchange tube ring, and each guide tube heat exchange tube is respectively connected to the top heat exchange tube ring fluid and connected to the bottom heat exchange tube ring fluid.

[0009] According to another embodiment of the present invention, the guide tube heat exchange tube assembly further comprises a plurality of middle heat exchange tube rings, and each guide tube heat exchange tube is respectively in fluid communication with the middle heat exchange tube rings.

[0010] According to another embodiment of the present invention, the heat exchange tube set includes 1 to 16 groups of spiral plate heat exchange tube sets, and each group of spiral plate heat exchange tube sets includes 2 to 20 spiral plate heat exchange tubes. According to another embodiment of the present invention, at the bottom of the heat exchange tube set, the inlets of all heat exchange tubes in the same spiral plate heat exchange tube set are distributed along the radial direction of the guide cylindrical heat exchange tube set on the outside of the guide cylindrical heat exchange tube set. According to another embodiment of the present invention, at the top of the heat exchange tube set, the outlets of all heat exchange tubes in the same spiral plate heat exchange tube set are distributed along the radial direction of the guide cylindrical heat exchange tube set on the outside of the guide cylindrical heat exchange tube set. According to another embodiment of the present invention, the spiral plate heat exchange tubes in each group of spiral plate heat exchange tube sets spirally rise around the guide cylindrical heat exchange tube set in a manner parallel to each other.

[0011] According to another embodiment of the present invention, each guide tube heat exchange tube and each spiral plate heat exchange tube are in fluid communication with the coolant inlet and the coolant outlet.

[0012] According to another embodiment of the present invention, the heat exchange tube collection includes multiple coolant inlets and multiple coolant outlets, as well as multiple inlet heat exchange tubes and multiple outflow heat exchange tubes, each coolant inlet is connected to a group of spiral plate heat exchange tube collectors via an inlet heat exchange tube, and each coolant outlet is connected to a group of spiral plate heat exchange tube collectors via an outflow heat exchange tube.

[0013] According to another embodiment of the present invention, the spiral plate heat exchange tubes in the spiral plate heat exchange tube set have the same or different inner diameters. According to another embodiment of the present invention, the guide tube heat exchange tubes in the guide tube heat exchange tube set have the same or different inner diameters.

[0014] According to another embodiment of the present invention, at the bottom of the heat exchange tube assembly, the inlets of all heat exchange tubes in the same spiral plate heat exchange tube assembly are distributed at the same or different intervals along the radial direction of the flow-guiding cylindrical heat exchange tube assembly on the outside of the flow-guiding cylindrical heat exchange tube assembly. According to another embodiment of the present invention, at the top of the heat exchange tube assembly, the outlets of all heat exchange tubes in the same spiral plate heat exchange tube assembly are distributed at the same or different intervals along the radial direction of the flow-guiding cylindrical heat exchange tube assembly on the outside of the flow-guiding cylindrical heat exchange tube assembly.

[0015] According to a second aspect of the present invention, a spiral flow slurry bed reactor is provided, the slurry bed reactor comprising a reactor shell, a slurry inlet and outlet located at the bottom of the shell, a gas outlet located at the top of the shell, a gas-liquid separator, a heat exchange tube set and a gas distributor located in the internal space surrounded by the shell, wherein:

[0016] The gas distributor comprises one or more gas distributor inlets, one or more gas distributor upper straight pipes, one or more gas distributor lower straight pipes, one or more gas distributor spiral pipe sets, a plurality of gas distributor annular pipes and a plurality of gas distributor gas distribution pipes;

[0017] The upper straight tube and the lower straight tube of the gas distributor are respectively located in two mutually parallel planes, each upper straight tube and each lower straight tube extend radially in a cross section perpendicular to the longitudinal axis of the slurry bed reactor, and the radial extension directions of the upper straight tube and the lower straight tube are different;

[0018] Each upper straight tube and each lower straight tube are communicated via a set of spiral tube collectors.

[0019] According to another embodiment of the present invention, the gas distributor gas distribution pipe is at an angle of 5 to 60 degrees relative to the longitudinal axis of the slurry bed reactor. According to another embodiment of the present invention, the angle between the component of the gas distributor gas distribution pipe in the cross section perpendicular to the longitudinal axis of the slurry bed reactor and the annular tube is 3 to 45 degrees.

[0020] According to another embodiment of the present invention, each group of spiral tube assemblies includes 2 to 20 spiral tubes, which extend clockwise or counterclockwise from top to bottom in parallel with each other at equal or unequal intervals to connect each upper straight tube and each lower straight tube fluid.

[0021] According to another embodiment of the present invention, the spiral tubes in each set of spiral tubes are straight or curved.

[0022] According to another embodiment of the present invention, the inclination angle of the gas distribution pipe of the gas distributor is the same as the inclination angle of the spiral tubes in the spiral tube set.

[0023] According to another embodiment of the present invention, the gas distributor gas distribution pipes are evenly distributed on the lower surfaces of the plurality of annular tubes.

[0024] According to another embodiment of the present invention, the gas distributor gas distribution pipe is a channel formed in the wall of the lower surface of the annular pipe, or is a pipe protruding from the lower surface of the annular pipe.

[0025] According to another embodiment of the present invention, the plurality of annular tubes are located in the same plane and are arranged in the form of concentric circles, and all the annular tubes are connected to the spiral tube current collector through the lower straight tube.

[0026] According to another embodiment of the present invention, each spiral tube in each group of spiral tubes has the same or different inner diameters; each annular tube has the same or different inner diameters; each lower straight tube has the same or different inner diameters; each upper straight tube has the same or different inner diameters.

[0027] The third aspect of the present invention provides a method for carrying out a catalytic reaction, which is a gas-liquid phase reaction or a gas-liquid-solid phase reaction, preferably a Fischer-Tropsch reaction, and the method is carried out in the spiral fluidized slurry bed reactor of the present invention.

[0028] According to the fourth aspect of the present invention, the use of the above-mentioned slurry bed reactor is provided, which is used for a process selected from the following: physical adsorption process, such as automobile exhaust treatment and factory waste gas treatment; chemical reaction, such as Fischer-Tropsch synthesis reaction, hydrogenation reaction, oxidation reaction, chlorination reaction, sulfonation reaction, alkylation reaction, carbonylation reaction, esterification reaction, transesterification reaction, catalytic isomerization reaction, and chemical absorption of waste gas; bioengineering, such as biological fermentation, bacterial culture, algae culture, etc.

[0029] In the specific implementation section below, the structural design of the slurry bed reactor developed in this application is described in conjunction with the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] The accompanying drawings show some designs of the present invention and the prior art.

[0031] Figure 1 A slurry bed reactor according to one embodiment of the present invention is shown, wherein the reactor includes a heat exchange tube set and a gas distributor specially designed according to the present invention.

[0032] Figure 2 Shows Figure 1 Schematic diagram of the structure of the gas distributor in the slurry bed reactor shown.

[0033] Figure 3 A slurry bed reactor according to another embodiment of the present invention is shown, which includes the heat exchange tube assembly and the gas distributor with a porous plate structure of the present invention.

[0034] Figure 4 A slurry bed reactor according to another embodiment of the present invention is shown, which includes the gas distributor of the present invention, a draft tube with a solid wall structure, and a serpentine tube heat exchanger surrounding the draft tube.

[0035] Figure 5 A prior art slurry bed reactor is shown, which includes a draft tube with a solid wall structure, a serpentine tube heat exchanger surrounding the draft tube, and a gas distributor with a porous plate structure. DETAILED DESCRIPTION

[0036] "Range" disclosed herein is in the form of lower limit and upper limit. It can be one or more lower limits, and one or more upper limits respectively. A given range is defined by selecting a lower limit and an upper limit. The selected lower limit and upper limit define the boundaries of a particular range. All ranges that can be defined in this way are inclusive and combinable, i.e. any lower limit can be combined with any upper limit to form a range. For example, a range of 60-120 and 80-110 is listed for a particular parameter, and it is understood that a range of 60-110 and 80-120 is also expected. In addition, if the minimum range values ​​1 and 2 are listed, and if the maximum range values ​​3, 4 and 5 are listed, the following ranges can all be expected: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.

[0037] In the present invention, unless otherwise specified, the numerical range "ab" represents an abbreviation of any real number combination between a and b, where a and b are real numbers. For example, the numerical range "0-5" means that all real numbers between "0-5" have been listed in this document, and "0-5" is just an abbreviation of these numerical combinations.

[0038] In the present invention, unless otherwise specified, all embodiments and preferred embodiments mentioned herein can be combined with each other to form a new technical solution.

[0039] In the present invention, unless otherwise specified, all technical features and preferred features mentioned herein can be combined with each other to form a new technical solution.

[0040] In the present invention, unless otherwise specified, all steps mentioned herein may be performed sequentially or randomly, but are preferably performed sequentially. For example, the method includes steps (a) and (b), which means that the method may include steps (a) and (b) performed sequentially, or may include steps (b) and (a) performed sequentially. For example, the method may further include step (c), which means that step (c) may be added to the method in any order, for example, the method may include steps (a), (b) and (c), or may include steps (a), (c) and (b), or may include steps (c), (a) and (b), etc.

[0041] In the present invention, if there is no special explanation, the "including" mentioned herein means open or closed. For example, the "including" may mean that other components not listed may also be included, or only the listed components may be included.

[0042] In the present invention, when describing the spatial relationship of a specific component or object relative to other components or objects, the terms "inside", "outside", "above", "below", etc. are used to indicate that the former is located inside, outside, above or below the latter, and the two may be in direct contact, or be separated by a certain distance or separated by a third component or object.

[0043] It should be emphasized that what is shown in the drawings and described below are only some specific embodiments of the present invention, and the protection scope of the present invention is not limited to these specific embodiments. The protection scope of the present invention is defined by the claims of the present invention, and may include any technical solution within the scope of the claims, including but not limited to further improvements and substitutions to these specific embodiments.

[0044] In the following text, the mass transfer and heat transfer uniformity of some preferred slurry bed reactors are characterized mainly based on the Fischer-Tropsch reaction. However, it should be emphasized here that the use of the slurry bed reactor of the present invention is not limited to these reactions, but can also be used for any other processes that can be implemented in a gas-liquid-solid three-phase system or a gas-liquid two-phase system, and similarly enable these other processes to obtain technical improvements and benefits due to mass transfer and heat transfer. Examples of the other processes include physical adsorption processes, such as automobile exhaust treatment and factory waste gas treatment; chemical reactions, such as hydrogenation reactions, oxidation reactions, chlorination reactions, sulfonation reactions, alkylation reactions, carbonylation reactions, esterification reactions, ester exchange reactions, catalytic isomerization reactions, and chemical absorption of waste gases; bioengineering, such as biological fermentation, bacterial culture, etc.

[0045] Figure 1 The structure of a slurry bed reactor according to an embodiment of the present invention is shown, which includes a reactor shell 1, and includes, in order from bottom to top, a bottom slurry inlet and outlet 13, a gas distributor 4, a heat exchange tube set 3, a separator 2, a partition 12 and a gas outlet 11.

[0046] According to one embodiment of the present invention, the separator 2 is an optional component, that is, in the slurry bed reactor of the present invention, the separator 2 may be present or may not be included. According to one embodiment, solid materials, or a mixture of solids and liquids, or liquid materials are pre-existing in the slurry bed reactor before the reaction begins. At the beginning of the reaction, during the reaction and / or at the end of the reaction, slurry materials and / or liquid materials are fed in and / or output from the slurry inlet and outlet 13 below, and gas materials are fed in through the gas distributor 4. The gas materials are dispersed into smaller bubbles under the action of the gas distributor 4, and enter the internal space of the reactor above the gas distributor 4 with a specific size distribution and a spiral flow pattern. While rising, the gas, liquid, and (optional) solid materials in the internal space contact each other, and a target reaction occurs, such as a "Fischer-Tropsch reaction", to generate target products, such as hydrocarbons of different chain lengths. Then the material continues to rise and leave the reaction zone. In the case where liquid-gas (and optional solid material) material separation is required, a gas separator 2 can be provided at the upper part of the reactor. Under the action of the gas separator 2, gaseous substances such as hydrocarbon target products or gaseous byproducts, gaseous residual raw materials, etc. are separated and output from the outlet 11 at the top to a subsequent process or storage container, while other materials (such as liquid reaction raw materials, optional solid raw materials, etc.) can be returned to the inner space of the reactor for continued reaction. According to a preferred embodiment, in the above-mentioned reaction process, the gaseous raw materials are input via the gas distributor 4 in a continuous or intermittent manner, and the gaseous raw materials are more preferably input via the gas distributor 4 in a continuous manner. According to another preferred embodiment, during the above reaction process, the liquid material (e.g., liquid raw material or liquid solvent) is introduced into the slurry bed reactor in a continuous or intermittent manner through the slurry inlet and outlet 13 at the bottom of the reactor, and one or more openings optionally arranged at the bottom periphery of the slurry bed reactor or at the side wall of the slurry bed reactor at different heights (e.g., middle, lower or bottom). Preferably, the liquid material (e.g., liquid raw material or liquid solvent) is introduced into the slurry bed reactor in a continuous or intermittent manner only through the slurry inlet and outlet 13 at the bottom. According to another embodiment of the present invention, during the above reaction process, the liquid material (e.g., liquid reaction product, liquid solvent, liquid by-product, residual liquid raw material, etc.) in the slurry bed reactor is drawn out in a continuous or intermittent manner through the slurry inlet and outlet 13 at the bottom of the reactor, and one or more openings optionally arranged at the bottom periphery of the slurry bed reactor or at the side wall of the slurry bed reactor at different heights (e.g., middle, lower or bottom). These drawn materials can be subsequently recovered and purified, and the by-products can be separated, recovered and further processed, or directly discharged or burned. Most preferably, the liquid level in the slurry bed reactor remains substantially unchanged throughout the reaction process.

[0047] According to one embodiment of the present invention, the reactor shell 1 of the slurry bed reactor is used to enclose an internal space for reaction, and may be a stainless steel shell, for example. Figure 1 In the reactor shown, the cross-sectional diameter of the shell is substantially constant, but the scope of the present invention is not limited thereto. The reactor shell of the present application may have any desired shape and size, such as a cylinder with a varying cross-sectional diameter from top to bottom, or a Figure 2 The cross section shown is in the form of a square or rectangle. According to a preferred embodiment of the present invention, the longitudinal (axial) height of the reactor is 5-100 meters, for example 10-80 meters, preferably 20-50 meters, more preferably 20-35 meters. According to a preferred embodiment of the present invention, the reactor has the same cross-sectional diameter from top to bottom along the longitudinal axis, for example, the cross-sectional diameter of the reactor can be 0.5-10 meters, for example 0.8-8 meters, or 0.9-7 meters, or 1-5 meters, or 1.2-3 meters, or 1.5-2 meters, or 1.6-1.8 meters. According to another preferred embodiment of the present invention, the reactor has a variable cross-sectional diameter from top to bottom along the longitudinal axis, for example, the cross-sectional diameter of the upper part of the reactor may be larger than the cross-sectional diameter of the lower part of the reactor; in the case where the cross-sectional diameters of the upper and lower parts of the reactor are different, the reactor has a smaller cross-sectional diameter at a height of 1 / 5 to 4 / 5, for example, 1 / 3 to 1 / 2, along the longitudinal axis, for example, an inner diameter of 0.5-10 meters, for example, 0.8-8 meters, or 0.9-7 meters, or 1-5 meters, or 1.2-3 meters, or 1.5-2 meters, or 1.6-1.8 meters; and a larger cross-sectional diameter of 0.8-15 meters, for example, 1-12 meters, or 1.5-10 meters, or 1.8-8 meters, or 2-6 meters, or 1.5-5 meters, or 1.6-4 meters, or 1.7-3 meters at the top. According to one embodiment of the present invention, Figure 1 As shown, the area between the bottom of the reactor and the liquid surface in the reactor is called the "gas-slurry mixing zone", in which the gas and liquid or slurry are mixed with each other and react during the circulation reflux process. In this area, at least the heat exchange tube collection and gas distributor of the present invention are arranged, and the heat exchange tube collection and gas distributor are completely submerged below the liquid surface. According to one embodiment of the present invention, the lower end opening of the gas-liquid separator 2 also extends below the liquid surface, and preferably the lower end opening of the gas-liquid separator 2 extends downward along the central axis of the reactor to a height lower than the upper end of the guide cylindrical heat exchange tube collection. According to one embodiment of the present invention, Figure 1As shown in FIG. 1 , the area between the upper surface of the liquid and the lower surface of the partition 12 is called the "gas-slurry separation area". In this area, the gas leaves the liquid / slurry and rises. During the rising process, the small amount of liquid carried in the gas will fall back into the liquid below. The main body of the gas-liquid separator 2 is arranged in this area, preferably along the central axis of the reactor. According to one embodiment of the present invention, as Figure 1 As shown, the area between the partition 12 and the top of the reactor is called the "gas phase zone". The gas is separated in this zone to remove the remaining small amount of liquid droplets and then discharged from the gas outlet 11 at the top of the reactor. The recovered liquid flows into the liquid phase of the gas-slurry mixing zone through the gas-liquid separator 2.

[0048] According to one embodiment of the present invention, the top and bottom of the reactor shell 1 are hemispherical, or part of a hemispherical shape, for example, 90%, 80%, 70%, 60%, 50% or 40% of the hemispherical shape.

[0049] exist Figure 1 In the embodiment shown, the slurry inlet and outlet 13 is simply connected to a pipe, but it can be further modified as needed. For example, one or more devices selected from the following can be set at the pipe connected to the inlet and outlet 13: valves, flow meters, heat exchange devices, baffles, flanges, threads, pins, fins, and any combination thereof. In addition, multiple slurry inlets and outlets 13 can be set at the bottom of the reactor. These multiple inlets and outlets can be set at the bottom of the reactor in any manner, such as uniformly set at the periphery or central position of the bottom of the reactor, and can be in the form of simple openings or nozzles. In the embodiment where the cross-section of the reactor is square or rectangular, the inlet and outlet arrangement described above can also be used.

[0050] A gas distributor is provided above the inlet. According to a less preferred embodiment of the present invention, the gas distributor may be a gas distributor in various forms, such as a perforated plate type gas distributor, the perforated plate having two upper and lower plates and openings in the plates, the gas raw material is input from the space between the two plates through a connecting pipe, and is mixed with the liquid phase in the form of fine bubbles through the openings in the plates; another example may be in the form of an array of multiple conduits with openings, specifically, the multiple conduits are arranged in the form of parallel tube rows, cross tube grids, concentric circles or concentric squares, and each conduit is connected to at least one gas inlet pipe, and each conduit may be isolated from the other conduits or fluidically connected to each other.

[0051] According to a preferred embodiment, the gas distributor has Figure 2 The structure shown, such as Figure 2As shown, the gas distributor 4 includes a gas distributor inlet 41, a gas distributor upper straight pipe 42, a gas distributor spiral pipe set 43, a gas distributor lower straight pipe 44, a gas distributor annular pipe 45, and a gas distributor gas distribution pipe 46.

[0052] According to one embodiment of the present invention, the upper straight tube and the lower straight tube of the gas distributor are respectively located in two mutually parallel planes, each upper straight tube and each lower straight tube extend radially in a cross section perpendicular to the longitudinal axis of the slurry bed reactor, and the radial extension directions of the upper straight tube and the lower straight tube are different, and each upper straight tube and each lower straight tube are connected via a group of spiral tube collectors. According to a preferred embodiment of the present invention, the gas distributor includes 2 to 20 groups, such as 3 to 12 groups, or 3 to 9 groups, or 3 to 6 groups of spiral tube collections, preferably, these spiral tube collections have the same shape and structure as each other, and are arranged in a centrally symmetrical manner relative to the longitudinal axis of the reactor. Each group of spiral tube collections is fluidically connected to a corresponding upper straight tube 42 and a corresponding lower straight tube 44, that is, there are as many upper straight tubes 42 and lower straight tubes 44 as there are groups of spiral tube collections 43. According to one embodiment of the present invention, when observing vertically downward along the longitudinal axis of the reactor, it can be seen that the upper straight tube 42 and the lower straight tube 44 connected to the same group of spiral tube sets do not overlap, and the upper straight tube 42 and the lower straight tube 44 each extend radially along the cross-section of the reactor (the cross-section perpendicular to the longitudinal axis of the reactor) and have an angle of 1 to 40 degrees between each other, for example, an angle of 5 to 35 degrees, or an angle of 8 to 30 degrees, or an angle of 10 to 28 degrees, or an angle of 12 to 25 degrees, or an angle of 15 to 20 degrees, or an angle of 16 to 18 degrees, or the angle can be within the numerical range obtained by combining any two of the above numerical values. According to one embodiment of the present invention, all upper straight tubes 42 have the same length, which is 70-150%, or 80-120%, or 85-110%, or 90-105%, or 95-102%, or 98-101% of the radius of the reactor cross section (a cross section perpendicular to the longitudinal axis of the reactor), or can be within the numerical range obtained by combining any two of the above values. When the length of the upper straight tube exceeds the radius of the reactor cross section, the excess portion of the upper straight tube passes through the side wall of the reactor and extends to the outside of the reactor (such as Figure 1As shown in the figure, and connected to a gas source arranged outside the reactor; when the length of the upper straight pipe exceeds the radius of the reactor cross section, the gas delivery pipe of the external gas source is introduced into the reactor and connected to the outer end of the upper straight pipe. According to one embodiment of the present invention, all lower straight pipes 44 have the same length, which is 50-99%, or 60-95%, or 70-90%, or 75-85%, or 78-82%, or 70-80% of the radius of the reactor cross section (a cross section perpendicular to the longitudinal axis of the reactor), or can be within the numerical range obtained by combining any two of the above numerical values.

[0053] According to one embodiment of the present invention, each group of spiral tube sets 43 includes 2 to 20 spiral tubes, for example, the number of spiral tubes in each group of spiral tube sets 43 can be 3-15, or 4-12, or 4-10, or 4-8, or 4-6, or 4-5. These spiral tubes extend clockwise or counterclockwise from top to bottom in an equidistant or unequally spaced manner, parallel or non-parallel to each other, so as to connect each upper straight tube with each lower straight tube fluid. Preferably, the extension direction of the spiral tube matches the extension direction of a corresponding group of spiral plate-shaped heat exchange tube sets in the heat exchange tube set above it.

[0054] There are multiple gas distributor annular pipes 45 below the gas distributor 4, for example, 2 to 15 annular pipes 45 are arranged in a concentric circle manner with equal or non-equal spacing, for example, 3-12 annular pipes 45, or 3-10 annular pipes 45, or 3-9 annular pipes, or 3-8 annular pipes, or 3-6 annular pipes, or 3-5 annular pipes, or 3-4 annular pipes. Each annular pipe is in fluid communication with all lower straight pipes 44. 8 to 100 gas distributor gas distribution pipes 46 are evenly arranged on the lower surface of each annular pipe (preferably at the lowest vertex of the circular cross section of the annular pipe), for example, 10 to 90, or 15 to 85, or 20 to 80, or 25 to 75, or 30 to 70, or 35 to 65, or 40 to 60, or 45 to 55, or 50 to 52. According to one embodiment of the present invention, all the gas distribution pipes 46 are evenly arranged on the lower surface of the annular tube (preferably at the lowest vertex of the circular cross section of the annular tube), more preferably, the spacing between any two adjacent gas distribution pipes 46 on each annular tube is the same, and more preferably, the spacing between any two adjacent gas distribution pipes 46 on all annular tubes is the same. According to a preferred embodiment of the present invention, the gas distribution pipes of the gas distributor are at an angle of 5 to 60 degrees relative to the longitudinal axis of the slurry bed reactor, for example, 8-55 degrees, or 10-52 degrees, or 12-50 degrees, or 15-45 degrees, or 18-42 degrees, or 20-40 degrees, or 22-35 degrees, or 25-30 degrees, or can be within the numerical range obtained by combining any two of the above numerical values. The angle between the component of the gas distributor gas distribution pipe in the cross section perpendicular to the longitudinal axis of the slurry bed reactor and the annular tube is 3-45 degrees, for example, 5-42 degrees, or 8-40 degrees, or 10-38 degrees, or 12-35 degrees, or 15-32 degrees, or 18-30 degrees, or 20-28 degrees, or 24-26 degrees, or it can be within the numerical range obtained by combining any two of the above values. According to a preferred embodiment of the present invention, all gas distribution pipes 46 have the same direction. According to a most preferred embodiment, the direction of all gas distribution pipes 46 matches the extension direction of the spiral tubes in the spiral tube set 43, and the overall spiral trend in the same direction can be formed. According to one embodiment of the present invention, the gas distributor gas distribution pipe is a channel formed in the lower surface wall of the annular tube, or a tube protruding from the lower surface of the annular tube. In other words, each gas distribution pipe 46 may be a channel formed in the annular pipe wall and not protruding from the annular pipe wall, or each gas distribution pipe 46 may be a pipe formed on the lower surface of the annular pipe and protruding from the annular pipe wall.

[0055] According to one embodiment of the present invention, each group of spiral tube assemblies 43 is completely identical with other groups of spiral tube assemblies and are centrally symmetrical to each other, and the upper straight tubes 42 and lower straight tubes 44 connected to each group of spiral tube assemblies 43 are also completely identical with other upper straight tubes and lower straight tubes and are centrally symmetrical to each other.

[0056] According to an embodiment of the present invention, the gas distributor inlet 41 is located at the outer end of the upper straight pipe 42 of the gas distributor; the gas distributor ring pipe 45 and the lower straight pipe 44 of the gas distributor are at the same level; and the gas distributor gas distribution pipe 46 is installed below the gas distributor ring pipe 45. Figure 2 In the embodiment of the present invention shown, there are three groups of gas distributor spiral tube sets 43, so there are three gas distributor inlets 41, three gas distributor upper straight tubes 42, and three gas distributor lower straight tubes 44. According to one embodiment of the present invention, each group of gas distributor spiral tube sets rises in a clockwise or counterclockwise manner from the lower straight tube to the upper straight tube, and the number of turns of the spiral (i.e., the number of turns completed by the spiral set from the lower straight tube to the upper straight tube, where the number of turns represents the proportion of the trace formed by the spiral on the interface perpendicular to the central longitudinal axis when the spiral is observed vertically downward along the central longitudinal axis of a spiral to a complete circle, i.e., a complete spiral of one cycle, expressed as a decimal) can be 0.01 to 0.3 turns, or 0.05 to 0.25 turns, or 0.08 to 0.20 turns, or 0.09 to 0.15 turns, or 0.1 to 0.12 turns. According to one embodiment of the present invention, all lower straight tubes are in the same plane, which is perpendicular to the longitudinal axis of the reactor, and all upper straight tubes are in the same plane, which is perpendicular to the longitudinal axis of the reactor. According to one embodiment of the present invention, the ratio of the vertical height from the plane where all lower straight tubes are located to the plane where all upper straight tubes are located to the total longitudinal height of the reactor is 0.1 to 9%, or 0.5 to 8%, or 1 to 7%, or 2 to 6%, or 3 to 5%, or 4 to 5%. According to one embodiment of the present invention, the ratio of the diameter of the outermost ring tube to the cross-sectional diameter of the reactor can be 50-99%, or 60-95%, or 70-90%, or 75-85%, or 78-82%, or 70-80%, or can be within the numerical range obtained by combining any two of the above numerical values. According to one embodiment of the present invention, the ratio of the diameter of the innermost ring tube to the cross-sectional diameter of the reactor can be 5-60%, or 8-55%, or 10-50%, or 12-45%, or 15-40%, or 18-35%, or 20-30%, or 22-25%, or can be within the numerical range obtained by combining any two of the above values. The remaining ring tubes (if any) are arranged in an equidistant manner between the outermost ring tube and the innermost ring tube.

[0057] In the present invention, "the inner diameter of the tube" means the inner diameter (for the case where the tube cross section is circular) or the inner equivalent diameter (for the case where the tube cross section is square, rectangular, elliptical or other shapes) after removing the wall thickness on the cross section perpendicular to the central longitudinal axis of the tube. "Equivalent diameter" means the diameter of a circle with the same area as a non-circular shape. For example, if a square cross section with a side length of 1 mm has an area of ​​1 square millimeter, its equivalent diameter is the diameter of a circle with an area of ​​1 square millimeter [e.g. equivalent diameter d = (2 / π 2 )]. The equivalent diameters of other geometric shapes can be calculated in the same way.

[0058] According to one embodiment of the present invention, the aspect ratio (ratio of length to inner diameter) of the upper straight tube 42 is 50 to 4, or 40 to 4.5, or 30 to 4.8, or 20 to 5, or 15 to 5.2, or 12 to 5.5, or 10 to 6, or 9 to 6, or 8 to 6, or 7 to 6, or can be within the numerical range obtained by combining any two of the above numerical values.

[0059] According to one embodiment of the present invention, each spiral tube in the spiral tube set 43 has the same inner diameter. According to one embodiment of the present invention, the ratio of the inner diameter of each spiral tube in the spiral tube set 43 to the inner diameter of the upper straight tube 42 is 0.1 to 0.8, or 0.2-0.7, or 0.3-0.6, or 0.4-0.5, or can be within the numerical range obtained by combining any two of the above values. According to one embodiment of the present invention, each lower straight tube 44 has the same inner diameter. According to one embodiment of the present invention, the ratio of the inner diameter of the lower straight tube 44 to the inner diameter of the upper straight tube 42 is 0.3 to 0.9, or 0.4-0.8, or 0.5-0.7, or 0.45-0.6, or can be within the numerical range obtained by combining any two of the above values. According to one embodiment of the present invention, each ring tube 45 has the same inner diameter. According to one embodiment of the present invention, the ratio of the inner diameter of the annular tube 45 to the inner diameter of the upper straight tube 42 is 0.1 to 0.8, or 0.2-0.7, or 0.3-0.6, or 0.4-0.5, or can be within the numerical range obtained by combining any two of the above values. According to one embodiment of the present invention, each of the air distribution pipes 46 has the same inner diameter as each other. According to one embodiment of the present invention, the ratio of the inner diameter of the air distribution pipe 46 to the inner diameter of the upper straight tube 42 is 0.01 to 0.3, or 0.02-0.25, or 0.05-0.2, or 0.08-0.1, or can be within the numerical range obtained by combining any two of the above values.

[0060] According to a preferred embodiment of the present invention, the positions of the respective spiral tubes and the respective ring tubes in the spiral tube set are aligned with each other.

[0061] For example, Figure 2 In the illustrated embodiment, the number of the gas distributor ring tubes 45 is 4, and the cylindrical surfaces where the circular ring lines of the four gas distributor ring tubes 45 are located coincide with the cylindrical surfaces where the four spiral linear gas pipes of the gas distributor spiral tube assembly 43 are located from the inside to the outside, that is, each gas distributor ring tube 45 is located directly below each spiral linear gas pipe.

[0062] In this embodiment, the axis of the gas distributor gas distribution pipe 46 is tangent to the cylindrical surface where the circular ring line of the gas distributor ring pipe 45 is located; the inclination angle of the gas distributor gas distribution pipe 46 is the same as the helix angle of the helix line of the spiral gas pipe directly above it.

[0063] In the internal space above the gas distributor 4, especially below the liquid level of the slurry bed, gas-liquid two-phase materials and optionally solid-phase materials contact each other and react, for example, Fischer-Tropsch reaction.

[0064] According to a less preferred embodiment of the present invention, a guide tube can be arranged above the gas distributor 4, and the guide tube can be formed by a non-porous wall, so that during the reaction, the gas-liquid mixture flows basically upward outside the guide tube and basically flows downward inside the guide tube, thereby establishing a material circulation flow in the reactor. According to a less preferred embodiment of the present invention, one or more heat exchangers surrounding the guide tube can be arranged in the space between the outer surface of the guide tube and the inner surface of the reactor shell, and the heat exchanger can be of any structure, such as one or more spiral, serpentine, annular or linear heat exchange tubes.

[0065] However, according to a preferred embodiment of the present invention, a specially designed heat exchange tube assembly 3 of the present invention is arranged above the gas distributor. According to a preferred embodiment of the present invention, the heat exchange tube assembly 3 includes a guide tube heat exchange tube assembly 34 and one or more groups of spiral plate heat exchange tube assembly 33, and the guide tube heat exchange tube assembly 34 and the spiral plate heat exchange tube assembly 33 are fluidically connected. According to a preferred embodiment of the present invention, the heat exchange tube assembly 3 is arranged above the gas distributor 4 and located in the gas-slurry mixing zone, and the top of the upper part of the heat exchange tube assembly is submerged below the liquid surface or slurry surface, for example, 0.1-100 cm, or 0.5-90 cm, or 1-80 cm, or 2-70 cm, or 5-60 cm, or 8-50 cm, or 10-40 cm, or 20-30 cm below the liquid surface or slurry surface, or within the numerical range obtained by combining any two of the above end values.

[0066] According to a preferred embodiment of the present invention, the heat exchange tube assembly 3 includes a spiral plate heat exchange tube assembly 33, a guide cylinder heat exchange tube assembly 34, an upper heat exchange straight tube 35, an upper heat exchange ring tube 36, a lower heat exchange straight tube 38, a lower heat exchange ring tube 37, a coolant inlet 32 ​​and a coolant outlet 31, or the heat exchange tube assembly 3 consists of a spiral plate heat exchange tube assembly 33, a guide cylinder heat exchange tube assembly 34, an upper heat exchange straight tube 35, an upper heat exchange ring tube 36, a lower heat exchange straight tube 38, a lower heat exchange ring tube 37, a cooling water inlet 32 ​​and a cooling water outlet 31.

[0067] According to a preferred embodiment of the present invention, the central axis of the heat exchange tube assembly 3 overlaps with the central axis of the reactor. According to a preferred embodiment of the present invention, the guide tube heat exchange tube assembly 34 is composed of a plurality of spiral heat exchange tubes (hereinafter also referred to as "guide tube heat exchange tubes") located in the same cylindrical surface. According to an embodiment of the present invention, the number of guide tube heat exchange tubes in the guide tube heat exchange tube assembly 34 can be 3-100, for example, 6-90, or 12-80, or 15-70, or 16-60, or 18-50, or 20-40, or 25-35, or 30-32, or within the numerical range obtained by combining any two of the above end values. According to a preferred embodiment of the present invention, all these "guide tube heat exchange tubes" spirally rise along a common cylindrical profile in a uniform manner, thereby jointly forming a cylindrical structure, which is similar in shape to a conventional guide tube, so the overall combination of these guide tube heat exchange tubes is called a guide tube heat exchange tube assembly 34. However, the difference between the guide tube heat exchange tube assembly 34 and the conventional guide tube is that the periphery of the tube assembly is composed of multiple heat exchange tubes, and the heat exchange tubes are not closed, so the slurry can enter and exit from the gaps between the heat exchange tubes to a certain extent. According to a preferred embodiment of the present invention, all the "flow tube heat exchange tubes" in the flow tube heat exchange tube assembly 34 are spirally ascended in a clockwise or counterclockwise manner along the cylindrical contour of the outer circumference of the tube assembly 34 in a manner parallel to each other, and the number of turns of the spiral (i.e., the number of turns completed by a flow tube heat exchange tube from the lower ring tube 37 to the upper ring tube 36, the number of turns here represents the trajectory of the spiral observed vertically downward along the central longitudinal axis of a spiral, and the proportion of the trace formed by the observed spiral on the interface perpendicular to the central longitudinal axis to a complete circle - that is, a complete spiral of one cycle - expressed as a decimal) can be 0.5 to 3 turns, or 0.8 to 2.5 turns, or 0.9 to 2 turns, or 1 to 1.8 turns, or 1 to 1.5 turns, or within the numerical range obtained by combining any two of the above end values. According to the present invention Figure 1In the preferred embodiment shown, each guide tube heat exchange tube extends upward in a counterclockwise spiral, and the spiral period of each guide tube heat exchange tube is 1. According to a preferred embodiment of the present invention, the upper and lower ends of all guide tube heat exchange tubes are connected to the upper heat exchange ring tube 36 (also called the top heat exchange tube ring, in this article, the upper heat exchange ring tube and the top heat exchange tube ring can be used interchangeably) and the lower heat exchange ring tube 37 (also called the bottom heat exchange tube ring, in this article, the lower heat exchange ring tube and the bottom heat exchange tube ring can be used interchangeably), and are respectively in fluid communication with the upper heat exchange ring tube 36 and the lower heat exchange ring tube 37. According to an embodiment of the present invention, in addition to the above-mentioned top and bottom heat exchange tube rings, one or more middle heat exchange tube rings can be optionally provided at different heights of the guide tube heat exchange tube assembly, and each guide tube heat exchange tube is respectively in fluid communication with the middle heat exchange tube ring. For example, the number of middle heat exchange tube rings can be 1-10, or 2-6, or 3-5, or within the numerical range obtained by combining any two of the above end values. These middle heat exchange tubes can be arranged at different heights of the guide tube heat exchange tube collection 34 at uniform intervals, each of which is fluidly connected to each guide tube heat exchange tube in the guide tube heat exchange tube collection 34, and can optionally have a coolant inlet and / or a coolant outlet for additionally introducing / leading out coolant at different heights.

[0068] According to a preferred embodiment of the present invention, 1 to 16 groups, such as 2-15 groups, or 3-12 groups, or 3-9 groups, or 3-6 groups of spiral plate heat exchange tube sets are arranged in a centrally symmetrical manner around the central guide cylindrical heat exchange tube set, and each group of spiral plate heat exchange tube sets includes 2 to 20, such as 3-18, or 3-15, or 3-12, or 3-9, or 4-6 spiral plate heat exchange tubes. According to one embodiment of the present invention, at the bottom of the heat exchange tube set, the inlets of all heat exchange tubes in the same spiral plate heat exchange tube set are distributed along the radial direction of the guide cylinder heat exchange tube set outside the guide cylinder heat exchange tube set, and are respectively connected to the same heat exchange lower straight tube 38 fluid; at the top of the heat exchange tube set, the outlets of all heat exchange tubes in the same spiral plate heat exchange tube set are distributed along the radial direction of the guide cylinder heat exchange tube set outside the guide cylinder heat exchange tube set, and are respectively connected to the same heat exchange upper straight tube 35 fluid; the spiral plate heat exchange tubes in each group of spiral plate heat exchange tube sets are evenly spaced from each other and spirally rise around the guide cylinder heat exchange tube set in a parallel manner. It can be seen that all the spiral plate heat exchange tubes in each group of spiral plate heat exchange tube sets are connected to one heat exchange upper straight tube 35 and one heat exchange lower straight tube 38 fluid, and there are as many heat exchange upper straight tubes and heat exchange lower straight tubes as there are spiral plate heat exchange tube sets. According to a preferred embodiment of the present invention, the outer end of each upper heat exchange straight tube 35 has a coolant outlet 31, and the outer end of each lower heat exchange straight tube 38 has a coolant inlet 32. According to a preferred embodiment of the present invention, the size and shape of all groups of spiral plate heat exchange tube sets are the same. According to a preferred embodiment of the present invention, the size and shape of each spiral plate heat exchange tube in each group of spiral plate heat exchange tube sets are the same. All the spiral plate heat exchange tubes in the heat exchange tube set can spirally extend from the lower heat exchange straight tube 38 below to the upper heat exchange straight tube 35 above in a clockwise or counterclockwise manner. According to a preferred embodiment of the present invention, the number of turns of each spiral plate heat exchange tube in each group of spiral plate heat exchange tubes (i.e., the number of spiral turns completed by a spiral plate heat exchange tube from the lower straight tube 38 to the upper straight tube 35, where the number of turns represents the trajectory of the spiral observed vertically downward along the central longitudinal axis of a spiral, and the proportion of the trace formed by the observed spiral on the interface perpendicular to the central longitudinal axis to a complete circle - that is, a complete spiral of one cycle - expressed as a decimal) can be 0.5 to 3 turns, or 0.8 to 2.5 turns, or 0.9 to 2 turns, or 1 to 1.8 turns, or 1 to 1.5 turns, or within the numerical range obtained by combining any two of the above end values. According to the present invention Figure 1 In the preferred embodiment shown, each spiral plate heat exchange tube extends in a counterclockwise spiral, and the spiral period of each spiral plate heat exchange tube is 1.

[0069] According to one embodiment of the present invention, the ratio of the vertical height from the plane where the lower heat exchange ring tube 37 is located to the plane where the upper heat exchange ring tube 36 is located relative to the total longitudinal height of the reactor is 10 to 90%, or 15 to 80%, or 20 to 70%, or 30 to 60%, or 40 to 55%, or 45 to 50%, or within the numerical range obtained by combining any two of the above end values. According to one embodiment of the present invention, the lower heat exchange ring tube 37 and the upper heat exchange ring tube 36 are aligned with each other and have the same size, and the ratio of the diameter of the lower heat exchange ring tube 37 and the upper heat exchange ring tube 36 (i.e., the diameter of the cross section of the guide cylindrical heat exchange tube set 34) to the cross-sectional diameter of the reactor can be 10-70%, or 15-65%, or 20-60%, or 25-55%, or 30-50%, or 35-40%, or within the numerical range obtained by combining any two of the above values.

[0070] According to one embodiment of the present invention, the aspect ratio (ratio of length to inner diameter) of the upper straight heat exchange tube 35 and the lower straight heat exchange tube 37 is 50 to 4, or 40 to 4.5, or 30 to 4.8, or 20 to 5, or 15 to 5.2, or 12 to 5.5, or 10 to 6, or 9 to 6, or 8 to 6, or 7 to 6, or can be within the numerical range obtained by combining any two of the above values. According to one embodiment of the present invention, the inner diameter of the upper straight heat exchange tube 35 and the lower straight heat exchange tube 37 can be 1-30 mm, for example, 2-25 mm, or 3-22 mm, or 5-20 mm, or 8-18 mm, or 10-15 mm, or 12-14 mm, or can be within the numerical range obtained by combining any two of the above values.

[0071] According to one embodiment of the present invention, the heat exchange upper ring tube 36 and the heat exchange lower ring tube 37 have exactly the same size and shape. According to one embodiment of the present invention, the ratio of the inner diameter of the heat exchange upper straight tube 35 to the inner diameter of the heat exchange upper ring tube 36 and the heat exchange lower ring tube 37 is 0.5 to 1.5, such as 0.55 to 1.4, or 0.6 to 1.3, or 0.65 to 1.2, or 0.7 to 1.1, or 0.75 to 1, or 0.80 to 0.95, or 0.85 to 0.9, or can be within the numerical range obtained by combining any two of the above numerical values.

[0072] According to one embodiment of the present invention, each spiral tube in the guide tube heat exchange tube collection 34 has the same inner diameter. According to one embodiment of the present invention, the ratio of the inner diameter of each spiral tube in the guide tube heat exchange tube collection 34 to the inner diameter of the upper heat exchange ring tube 36 is 0.1 to 0.8, or 0.2-0.7, or 0.3-0.6, or 0.4-0.5, or can be within the numerical range obtained by combining any two of the above values. According to one embodiment of the present invention, the ratio of the inner diameter of each heat exchange tube in the spiral plate heat exchange tube collection 33 to the inner diameter of the upper heat exchange ring tube 36 is 0.1 to 0.8, or 0.2-0.7, or 0.3-0.6, or 0.4-0.5, or can be within the numerical range obtained by combining any two of the above values.

[0073] According to a preferred embodiment, the heat exchange tube can be made of a material selected from the following: stainless steel, organic glass, copper, iron, ceramic, glass, aluminum, etc. During the reaction process, a heat exchange fluid (such as water, heat exchange oil, carbon dioxide, etc.) flows through the heat exchange tube to finely adjust the temperature in the reactor.

[0074] Without wishing to be limited to any specific theory, the inventors have surprisingly discovered through research that the above-mentioned arrangement of the heat exchange tubes can not only improve the heat transfer efficiency, but also, due to its specific structural design, effectively combine the mixing and flow-guiding functions of the guide tube with the heat transfer function of the heat exchange tube, thereby reducing the influence of unfavorable factors such as back-mixing, dead zones, eddies, large bubbles, etc. in the reaction system, which ultimately results in a further improvement in the catalytic reaction effect in the reactor.

[0075] A separator can be optionally provided at the upper part of the internal space of the reactor as required. After the reaction (e.g., Fischer-Tropsch reaction) is carried out, the gas material flow mixed with a portion of liquid and solid rises to the separator. The separator can be any separator known in the art that can be used for gas, liquid, and solid three-phase separation, preferably a cyclone separator 2. According to a preferred embodiment, the cyclone separator 2 is coaxially arranged with the reactor shell 1; the cyclone separator 2 includes a cyclone separator gas phase outlet 21 located in the gas phase zone, a cyclone separator inlet 22 located in the gas-slurry separation zone, and a cyclone separator slurry outlet 23 located in the gas-slurry mixing zone from top to bottom. According to a preferred embodiment, the rotation direction of the fluid in the cyclone separator 2 is clockwise when viewed from top. According to a preferred embodiment, the downstream of the separator also includes devices such as baffles and defoamers. After the liquid and solid are separated and removed in the separator, the gaseous material rises from the separator through the baffle and is then discharged from the top outlet 11 of the reactor. The liquid and solid components separated in the separator flow downward back into the slurry. According to a preferred embodiment, the separator is a cyclone separator 2, which comprises a feed leg, the lower end of which extends below the liquid level in the reactor. In a preferred embodiment of the present invention, the reactor of the present invention comprises 1-20, preferably 1-10 separation devices, which are evenly distributed around the inner wall below the partition.

[0076] exist Figure 1 In the embodiment shown, the gas phase outlet 11 is simply connected to a pipe, but it can be further modified as needed. For example, the pipe connected to the outlet can be provided with one or more devices selected from the following: valves, flow meters, heat exchange devices, baffles, flanges, threads, pins, fins, and any combination thereof.

[0077] Apart from Figure 1In addition to the devices shown, the reactor of the present invention may also include other devices as needed, such as: a settling tube, which may be a ratio tube with an inner diameter smaller than the diameter of the cross section of the reactor, arranged in the internal space of the reactor along a direction parallel to the longitudinal axis of the reactor, and used to guide the material to settle downward in the tube; a material circulation system, which includes a circulation inlet on the shell wall located in the middle of the reactor, a circulation pipeline located outside or inside the reactor shell, and a circulation outlet located at the bottom of the reactor (but located above the inlet at the bottom of the shell), and the circulation system is used to lead a part of the material in the reactor from the circulation inlet during the reaction, and transport it to the circulation outlet at the bottom through the circulation pipeline, thereby establishing additional material circulation in the reactor to promote mass transfer and heat transfer; a heating / cooling device; a temperature / pressure / flow rate sensor; a flow control component, such as a baffle, a guide plate, a fin, a stirring blade, etc. One or more of the above devices can be added to the slurry bed reactor as needed, but according to a preferred embodiment of the present invention, through the preferred design of the distribution plate, the required excellent mass transfer and heat transfer performance is achieved without using the above other devices.

[0078] According to a preferred embodiment of the present invention, the reactor of the present invention is as follows Figure 1 and Figure 2As shown, and it operates in the following manner: before the reactor starts to operate, liquid material or solid-liquid mixed slurry is loaded from the slurry inlet and outlet 13, and the slurry liquid level is higher than the highest point of the heat exchange tube set 3, and then the reactor is placed under suitable reaction conditions. After the reactor starts to operate, the gas phase reactant is introduced from the gas distributor inlet 41, sprayed from the gas distributor gas distribution pipe 46, and transmits its kinetic energy to the slurry below the gas distributor gas distribution pipe 46. Since the gas distribution direction of the gas distributor gas distribution pipe 46 is clockwise or counterclockwise downward, under the joint action of all the gas distributor gas distribution pipes 46, the slurry below the gas distributor gas distribution pipe 46 begins to flow in a clockwise spiral. After the gas phase is sprayed from the gas distributor gas distribution pipe 46, bubbles are formed in the slurry. Driven by the buoyancy, the vertical speed of the bubble changes from downward to upward, and drives the slurry around the bubble to flow upward. Due to the presence of the guide tube heat exchanger tube assembly 34, the slurry flows upward outside the guide tube heat exchanger tube assembly 34 and flows downward inside the guide tube heat exchanger tube assembly 34, thereby producing a better circulation effect in the entire reactor. Outside the guide tube heat exchanger tube assembly 34, due to the presence of the gas distributor spiral tube assembly 43 and the spiral heat exchanger tube assembly 33, and the spiral tube assembly has a greater blocking effect on the slurry and a smaller blocking effect on the bubbles, most bubbles will pass through the gaps of the spiral tube assembly during the rising process, and most slurries will rise along the spiral tube assembly, thereby increasing the speed difference between the bubbles and the slurry and enhancing the mass transfer effect. When the slurry outside the guide tube heat exchanger tube assembly 34 flows to the top of the heat exchanger tube assembly 3, it will turn into the guide tube heat exchanger tube assembly 34 in the form of a vortex. The speed difference between the gas phase and the slurry at the vortex is extremely large, and the mass transfer effect is excellent.

[0079] The cyclone separator 2 is located at the top of the reactor, and its gas phase outlet 21 extends above the partition 12, and the cyclone separator liquid phase outlet 23 is submerged below the slurry bed liquid level and extends into the cylindrical surface where the guide cylindrical heat exchange tube set 34 is located. This technical solution can directly pour the slurry separated by the cyclone separator 2 into the guide cylindrical heat exchange tube set 34 with higher density, promoting the fluid circulation inside and outside the guide cylindrical heat exchange tube set 34.

[0080] Due to the action of centrifugal force, the slurry spirally rising outside the guide cylindrical heat exchange tube set 34 will expel some bubbles into the guide cylindrical heat exchange tube set 34. These bubbles driven upward by buoyancy and the slurry flowing downward in the guide cylindrical heat exchange tube set 34 flow in the opposite direction, thereby enhancing the mass transfer effect.

[0081] Since Fischer-Tropsch synthesis is a highly exothermic reaction, heat needs to be removed in time through the heat exchange tube set 3 to maintain the slurry temperature in the range of 250-300° C., and the typical preferred temperature is 255-265° C. The purpose of controlling heat removal can be achieved by controlling the flow rate and temperature of the cooling water introduced.

[0082] Any two or more of all the above-mentioned embodiments of the present invention may be arbitrarily combined with each other, and these combinations are also included in the overall technical concept of the present invention.

[0083] Example

[0084] The preferred embodiments of the present invention are specifically listed in the following examples, but it should be understood that the protection scope of the present invention is not limited thereto.

[0085] In the following examples and comparative examples, a plurality of reaction systems were constructed, and the effects of these reaction systems on the Fischer-Tropsch reaction were investigated by designing the reactor structure, distribution plate and heat exchanger therein.

[0086] Examples 1-3 and Comparative Example 1

[0087] In the following examples 1-3, respectively, Figure 1 , Figure 3 and Figure 4 The slurry bed reactor shown carries out Fischer-Tropsch reaction. The shell of the reactor is made of stainless steel. The "gas-slurry mixing zone" below that contains the slurry is 9 meters high from the bottom of the reactor to the liquid surface. The shell of the reactor is uniformly cylindrical from top to bottom, with an inner diameter of 2 meters. The total axial height of the reactor is 11.5 meters. A gas-liquid / solid cyclone separation device is arranged on the top of the reactor. Before the reaction starts, the gas-slurry mixing zone in the reactor is pre-loaded with 36 tons of liquid paraffin and 1.8 tons of cobalt-based catalyst (the chemical formula of the cobalt-based catalyst is Co2C, synthesized according to the steps recorded in the document DOI: 10.1038 / nature19786), and the mass percentage of the catalyst in the slurry is 5wt%.

[0088] At the beginning of the reaction, the raw gas was fed at a rate of 0.18 m·s -1The apparent gas flow rate is fed into the reactor from the inlet at the bottom of the reactor, so that 503 standard cubic meters of raw gas are input into the reactor per hour, and the raw gas contains 49% volume of hydrogen, 49% volume of CO and 2% volume of nitrogen. During the reaction, the pressure in the reactor is maintained at 1.0MPa, and the target temperature is set at 260℃. The raw gas input from the gas distributor is distributed by the distribution plate, and then dispersed and formed in the slurry bed layer to rise. The bubbles drive the slurry and catalyst in the bed layer to flow upward to the surface of the slurry. In this process, the raw gas, liquid paraffin and catalyst are in contact with each other. The raw gas undergoes a Fischer-Tropsch synthesis reaction under the action of the catalyst to generate wax and hydrocarbon oil, and at the same time, some by-product light hydrocarbons are produced. The gaseous material detaches from the surface of the slurry, carrying a part of the droplets and fine solids to rise. After separation by the cyclone separator, the mixture of the product and the by-product is discharged from the outlet. The product is characterized and analyzed using a GC-14C gas chromatograph produced by Shimadzu Corporation. The results are summarized in Table 1. Most of the liquid and solid materials move laterally toward the reactor shell at the slurry surface, descend along the shell and return to the distribution plate, repeating the above-mentioned slurry bed reaction process. The liquid and solid recovered at the cyclone separator return to the liquid surface of the slurry bed through the lower leg of the cyclone separator, and also move laterally toward the reactor shell, descend along the shell and return to the distribution plate, repeating the above-mentioned slurry bed reaction process.

[0089] The different designs of the comparative examples and embodiments of the present invention are as follows:

[0090] Example 1

[0091] The slurry bed reactor of Example 1 is designed in the manner described above, wherein Figure 2The gas distributor 4 shown in the figure has an upper straight tube 42 with an axial length of 1000 mm and an inner diameter of 132 mm; an axial length of a lower straight tube 44 with an inner diameter of 112 mm; when viewed downward along the central axis of the reactor, the upper straight tube 42 and the lower straight tube 44 extend along the axial direction of the reactor cross section, respectively, and the angle between the upper straight tube 42 and the lower straight tube 44 is 30 degrees; all the upper straight tubes 42 are in the same plane, all the lower straight tubes 44 are in the same plane, and the vertical height between the plane where the upper straight tubes 42 and the plane where the lower straight tubes 44 are located is 600 mm; and the gas distributor comprises three groups of spiral tube sets 44. Each group includes four spiral tubes, each spiral tube has a spiral degree of 0.1 turn, and the inner diameter of the spiral tube is 92mm; it includes four annular tubes 45, the diameter of the outermost annular tube 45 is 1600mm, the diameter of the innermost annular tube 45 is 400mm, and the remaining two annular tubes are arranged between the outermost and innermost annular tubes at equal intervals. The numbers of air distribution tubes 46 arranged on the lower surface from the outermost to the innermost annular tubes are 120, 90, 60 and 30 respectively, and the inclination angle of each air distribution tube 46 is the same as the inclination direction of the guide tube heat exchange tube at the bottom of the guide tube heat exchange tube set above it, and the inner diameter of the air distribution tube 46 is 3mm.

[0092] The inner diameter of the upper straight heat exchange tube 36 and the lower straight heat exchange tube 37 in the heat exchange tube set 3 is 60mm. There are three upper straight heat exchange tubes and three lower straight heat exchange tubes in total. All upper straight heat exchange tubes 36 are in the same plane, and all lower straight heat exchange tubes 37 are in the same plane. The vertical height between the plane where the upper straight heat exchange tube 36 and the plane where the lower straight heat exchange tube 37 are located is 6000mm; the diameter of the upper heat exchange ring tube 36 and the lower heat exchange ring tube 37 is 800mm, and the inner diameter is 60mm. The guide cylinder heat exchange tube set is equipped with 24 heat exchange tubes, each of which has a spiral degree of 1 circle and an inner diameter of 60mm. There are three groups of spiral plate heat exchange tube sets 33 in total, each group has four spiral heat exchange tubes, and the spiral degree of these four heat exchange tubes is 1 circle and the inner diameter is 60mm. The vertical distance between the upper end of the heat exchange tube set 3 and the liquid surface is 400mm. Condensate water at room temperature is supplied into the heat exchange tube at a flow rate of 3.23 m / s.

[0093] Example 2

[0094] The slurry bed reactor of Example 2 is designed in the same manner as Example 1, except that no Figure 2Instead of the gas distributor 4 shown in the figure, a porous plate gas distributor 5 is used, which is composed of a gas phase inlet 51, a gas chamber 52 and a porous plate 53 from bottom to top. These components are components of the reactor shell 1 instead of independent components like the gas distributor 4 in Example 1. The slurry inlet and outlet 13 in Example 1 becomes a gas phase inlet 51 in Example 2, and its inner diameter is 80mm. Above the gas phase inlet 51 is an air chamber 52, which has a thickness of 160mm and a diameter equal to the inner diameter of the reactor shell 1. The air chamber 52 is separated from the gas-slurry mixing zone above it by a porous plate 53. The diameter of the porous plate 53 is equal to the inner diameter of the reactor shell 1, and four circles of holes are distributed on it. The circle diameter and the number of holes of each circle correspond one by one to the diameter of the annular tube 45 of the gas distributor 4 and the number of gas distribution pipes set on the lower surface of each annular tube. The aperture of the porous plate 53 is also equal to the inner diameter of the gas distribution pipe 46 of the gas distributor. The slurry inlet and outlet 13 in Example 1 was moved to the cylindrical side of the reactor shell 1, above the porous plate 53 in Example 2. The inner cylindrical surface of the slurry inlet and outlet 13 was tangent to the upper surface of the porous plate 53, and the inner diameter of the slurry inlet and outlet 13 was 100 mm.

[0095] Example 3

[0096] The slurry bed reactor of Example 3 is designed in the same manner as that of Example 1, except that no Figure 1 The heat exchange tube set 3 shown in the embodiment is replaced by a conventional draft tube 7 and a serpentine heat exchange tube 6. The position, diameter and height of the draft tube 7 are the same as those of the draft tube heat exchange tube set 34 in embodiment 1. The number of the serpentine heat exchange tube 6 is 1, the height is the same as that of the draft tube 7, the number of turns is 40.25, and the inner diameter is 30 mm.

[0097] Comparative Example 1

[0098] The slurry bed reactor of Comparative Example 1 is designed in the same manner as Example 1, with the only difference being the use of the perforated plate gas distributor 5 described in Example 2 above and the conventional draft tube 7 and serpentine heat exchange tube 6 described in Example 3 above.

[0099] The applicant characterized the products of all the above-mentioned invention embodiments and comparative examples, and used a GC-14C gas chromatograph produced by Shimadzu Corporation to characterize and analyze the components of the products drawn out from the reactor outlet. In addition, in order to monitor the temperature distribution in the reactor, starting from the distribution plate, a temperature sensor was set up against the wall every 6 meters in the slurry bed layer in the reactor. After the reaction was stable, the reading of each temperature sensor was read, and the average value T of all temperature sensors was taken. 均 , and then obtain the above temperature sensor readings and the T 均 The average ΔT of the absolute values ​​of all differences is used as the “average temperature fluctuation absolute value” to rate the heat transfer efficiency within the system.

[0100] Table 1

[0101]

[0102] From the experimental results shown in the above table, it can be seen that the present invention achieves significant improvements in catalytic reaction results and temperature uniformity by using specially designed heat exchange tube sets and gas distributors compared to existing conventional designs (Example 2 and Example 3 are compared with Comparative Example 1, respectively); in addition, Example 1 of the present invention compared with Example 2 / Example 3 shows that if the specially designed heat exchange tube sets and gas distributors of the present invention are simultaneously used in a slurry bed reactor, the catalytic reaction results and temperature uniformity can be further significantly improved.

Claims

1. A spiral flow slurry bed reactor, comprising a reactor shell, a slurry inlet and outlet located at the bottom of the shell, a gas outlet located at the top of the shell, a gas-liquid separator, a heat exchange tube set and a gas distributor located in the inner space surrounded by the shell, wherein: The gas distributor comprises one or more gas distributor inlets, one or more gas distributor upper straight pipes, one or more gas distributor lower straight pipes, one or more groups of gas distributor spiral pipe sets, multiple gas distributor annular pipes and multiple gas distributor gas distribution pipes; The upper straight tube and the lower straight tube of the gas distributor are respectively located in two mutually parallel planes, each upper straight tube and each lower straight tube extend radially in a cross section perpendicular to the longitudinal axis of the slurry bed reactor, and the radial extension directions of the upper straight tube and the lower straight tube are different; Each upper straight tube and each lower straight tube are connected via a set of spiral tube collectors; Each set of spiral tubes includes 2 to 20 spiral tubes, which extend clockwise or counterclockwise from top to bottom in parallel with each other in equal or unequal spacing to connect each upper straight tube with each lower straight tube; The spiral tubes in each set of spiral tubes are straight or curved; The multiple annular tubes are located in the same plane and are arranged in the form of concentric circles, and all the annular tubes are connected to the spiral tube current collector through the lower straight tube.

2. The spiral fluidized slurry bed reactor according to claim 1, characterized in that: The gas distributor gas distribution pipe forms an angle of 5 to 60 degrees relative to the longitudinal axis of the slurry bed reactor; and The angle between the component of the gas distributor gas distribution pipe in the cross section perpendicular to the longitudinal axis of the slurry bed reactor and the annular pipe is 3-45 degrees.

3. The spiral fluidized slurry bed reactor according to claim 1, characterized in that: The inclination angle of the gas distribution pipe of the gas distributor is the same as the inclination angle of the spiral tube in the spiral tube set.

4. The spiral fluidized slurry bed reactor according to claim 1, characterized in that: The gas distributor gas distribution pipes are evenly distributed on the lower surfaces of the multiple annular tubes.

5. The spiral fluidized slurry bed reactor according to claim 1, characterized in that: The gas distribution pipe of the gas distributor is a channel formed in the wall of the lower surface of the annular pipe, or is a pipe protruding from the lower surface of the annular pipe.

6. The spiral fluidized slurry bed reactor according to claim 1, characterized in that: Each spiral tube in each set of spiral tubes has the same or different inner diameters; each annular tube has the same or different inner diameters; each lower straight tube has the same or different inner diameters; each upper straight tube has the same or different inner diameters.

7. A method for carrying out a catalytic reaction, wherein the catalytic reaction is a gas-liquid phase reaction or a gas-liquid-solid phase reaction, and the method is carried out in a spiral fluidized slurry bed reactor as claimed in any one of claims 1 to 6.

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