CN112316858A

CN112316858A - Spiral flow slurry bed reactor

Info

Publication number: CN112316858A
Application number: CN202011410158.8A
Authority: CN
Inventors: 王子凡; 赵陆海波; 唐志永
Original assignee: Shanghai Ruicheng Carbon Energy Technology Co ltd
Current assignee: Shanghai Ruicheng Carbon Energy Technology Co ltd
Priority date: 2020-12-04
Filing date: 2020-12-04
Publication date: 2021-02-05

Abstract

The invention provides a spiral flow slurry bed reactor, which comprises a reactor shell, a slurry inlet and a slurry outlet positioned at the bottom of the shell, a gas outlet positioned at the top of the shell, and a gas-liquid separator, a heat exchange tube set and a gas distributor which are positioned in an inner space surrounded by the shell. According to the invention, the structure of the heat exchange tube set and/or the gas distributor is specially designed, so that the effects of gas-liquid mass transfer and heat transfer are obviously improved, and the Fischer-Tropsch reaction efficiency is improved.

Description

Spiral flow slurry bed reactor

Technical Field

The invention belongs to the field of chemical equipment devices, and particularly relates to a slurry bed reactor, which is provided with a structure capable of generating spiral flow and can guide gas-liquid fluid in the reactor to generate efficient internal circulation.

Background

In the fields of chemical industry, biological engineering, environmental protection and the like, processes such as chemical reaction, biological engineering cultivation and the like are often required to be carried out in a multiphase reaction system in which gaseous, liquid and solid materials exist simultaneously, specific examples of such processes may include biological fermentation, wastewater treatment, tail gas treatment, chemical synthesis, and the like, the gaseous and liquid materials used therein may include various reactants and process aids, the solid paste may be either a reactant, a culture substrate, or a reaction catalyst or other process aids, these biological or chemical processes are usually carried out using various three-phase reactors, such as stirred bubble-tank reactors, bubble column reactors, plate reactors, packed column reactors, tubular reactors, jet reactors, etc., of which one of the most important is a bubble reactor, e.g. a slurry bed reactor.

The major problems with slurry bed reactors are that the uniformity of the overall material concentration and flow velocity distribution is difficult to control, unavoidable and difficult to control turbulence, back-mixing, etc. may occur locally, and that dead zones may also be present, the above problems of uniform mass transfer and uniform heat transfer having a great adverse effect on the quality of the process product and on the routine operation and maintenance of the slurry bed. In order to overcome the above problems, a great deal of research has been conducted on slurry bed reactors so far, and the specific means adopted is not limited to arranging a greater number of nozzles, baffles, heat exchange pipes, reflux circulation structures and the like at different positions in the reactor so as to improve the material circulation and energy exchange at various positions in the slurry bed reactor. Although the above-mentioned improvement can alleviate the existing problems to some extent, these additional components can significantly increase the complexity of the design and operation of the slurry bed reactor, resulting in a substantial increase in capital and routine maintenance costs, and these newly added components can introduce many new blocking points inside the reactor, and even possibly bring new adverse effects to the mass and heat transfer in the reactor, and bring new problems while solving the original problems. The continuing development of this concept in accordance with the prior art has resulted in the fact that technicians are required to monitor and adjust more and more parameters while operating the plant, the complexity of the reaction system is increasing and the improvement in overall mass and heat transfer is in fact limited.

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

Disclosure of Invention

According to a first aspect of the present invention there is provided a helical 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 an interior space enclosed by the shell, wherein:

the heat exchange tube set comprises a coolant inlet, a coolant outlet, a flow guide cylindrical heat exchange tube set and one or more groups of spiral plate-shaped heat exchange tube sets, and the flow guide cylindrical heat exchange tube sets are communicated with the spiral plate-shaped heat exchange tube sets in a current collecting mode.

According to one embodiment of the invention, the guide shell heat exchange tube bank is generally cylindrical, the cylindrical wall of which comprises 3 to 100 guide shell heat exchange tubes, each guide shell heat exchange tube being spirally distributed about the longitudinal central axis of the guide shell heat exchange tube bank.

According to another embodiment of the invention, the collection of draft tube heat exchange tubes has a top heat exchange tube ring and a bottom heat exchange tube ring, each draft tube heat exchange tube being in fluid communication with the top heat exchange tube ring and in fluid communication with the bottom heat exchange tube ring, respectively.

According to another embodiment of the invention, the collection of draft tube heat exchange tubes further has a plurality of middle heat exchange tube rings, each draft tube heat exchange tube being in fluid communication with a respective one of the middle heat exchange tube rings.

According to another embodiment of the invention, the collection of heat exchange tubes comprises 1 to 16 sets of spiral plate shaped heat exchange tubes, each set comprising 2 to 20 spiral plate heat exchange tubes. According to another embodiment of the invention, at the bottom of the heat exchange tube set, the inlets of all the heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed outside the flow guide cylindrical heat exchange tube set along the radial direction of the flow guide cylindrical heat exchange tube set. According to another embodiment of the invention, the outlets of all heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed outside the flow guide cylindrical heat exchange tube set along the radial direction of the flow guide cylindrical heat exchange tube set at the top of the heat exchange tube set. According to another embodiment of the invention, the spiral-plate heat exchange tubes of each set of spiral-plate shaped heat exchange tubes are spiraled upwardly around the flow-guide cylindrical heat exchange tube set in a parallel manner to each other.

According to another embodiment of the invention, each draft tube heat exchange tube and each spiral plate heat exchange tube is in fluid communication with the coolant inlet and the coolant outlet.

According to another embodiment of the present invention, the heat exchange tube set includes a plurality of coolant inlets and a plurality of coolant outlets, and a plurality of inflow heat exchange tubes and a plurality of outflow heat exchange tubes, each coolant inlet being in communication with a set of spiral plate-shaped heat exchange tube current collectors via one inflow heat exchange tube, and each coolant outlet being in communication with a set of spiral plate-shaped heat exchange tube current collectors via one outflow heat exchange tube.

According to another embodiment of the invention, the spiral plate heat exchange tubes of the set of spiral plate heat exchange tubes have the same or different inner diameters. According to another embodiment of the invention, the guide shell heat exchange tubes of the guide shell heat exchange tube set have the same or different inner diameters.

According to another embodiment of the invention, at the bottom of the heat exchange tube set, the inlets of all the heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed at the same or different intervals along the radial direction of the flow guide cylindrical heat exchange tube set outside the flow guide cylindrical heat exchange tube set. According to another embodiment of the invention, the outlets of all the heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed at the same or different intervals along the radial direction of the flow guide cylindrical heat exchange tube set outside the flow guide cylindrical heat exchange tube set at the top of the heat exchange tube set.

According to a second aspect of the present invention there is provided a helical flow 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 set and a gas distributor in an interior space enclosed 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, a plurality of gas distributor annular pipes and a plurality of gas distributor gas distribution pipes;

the upper straight pipe and the lower straight pipe of the gas distributor are respectively positioned in two planes which are parallel to each other, each upper straight pipe and each lower straight pipe radially extend in a cross section which is vertical to the longitudinal axis of the slurry bed reactor, and the radial extension directions of the upper straight pipe and the lower straight pipe are different;

each upper straight pipe and each lower straight pipe are communicated through a set of spiral pipe current collectors.

According to another embodiment of the invention, the gas distributor gas distribution pipe is at an angle of 5 to 60 degrees with respect to the longitudinal axis of the slurry bed reactor. According to another embodiment of the invention, the gas distributor gas distribution pipe has a component in a cross section perpendicular to the longitudinal axis of the slurry bed reactor, which forms an angle of 3 to 45 degrees with the annular pipe.

According to another embodiment of the present invention, each set of coils comprises 2 to 20 coils extending in a clockwise or counterclockwise manner from top to bottom in parallel with each other in an equally or unequally spaced manner to fluidly communicate each upper straight tube with each lower straight tube.

According to another embodiment of the invention, the coils of each set of coils are straight or curved.

According to another embodiment of the invention, the gas distributor gas distribution pipe has an inclination angle which is the same as the inclination angle of the spiral pipe in which the spiral pipes are concentrated.

According to another embodiment of the invention, the gas distributor gas distribution tubes are evenly distributed over the lower surface of the plurality of annular tubes.

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

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

According to another embodiment of the invention, the individual coils of each set of coils have the same or different inside diameters; each annular tube has the same or different inner diameter; each lower straight pipe has the same or different inner diameter; each upper straight pipe has the same or different inner diameter.

In a third aspect the invention provides a process 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, in a helical flow slurry bed reactor according to the invention.

According to a fourth aspect of the present invention there is provided the use of a slurry bed reactor as described above, for a process selected from the group consisting of: physical adsorption processes, such as automobile exhaust treatment and plant exhaust treatment; chemical reactions such as fischer-tropsch synthesis, hydrogenation, oxidation, chlorination, sulfonation, alkylation, carbonylation, esterification, transesterification, catalytic isomerization, and chemical absorption of the off-gas; bioengineering, such as biological fermentation, bacterial culture, algae culture, etc.

In the following detailed description section, the structural design of the slurry bed reactor developed in the present application is described with reference to the accompanying drawings.

Drawings

The drawings show some of the designs of the present invention and prior art.

Fig. 1 shows a slurry bed reactor according to one embodiment of the present invention, which comprises both a heat exchange tube set and a gas distributor, which are specifically designed according to the present invention.

Fig. 2 shows a schematic diagram of the structure of a gas distributor in the slurry bed reactor shown in fig. 1.

Fig. 3 shows a slurry bed reactor according to another embodiment of the present invention, in which a gas distributor comprising a heat exchange tube assembly and a porous plate structure of the present invention is included.

Fig. 4 shows a slurry bed reactor according to another embodiment of the present invention, comprising a gas distributor according to the present invention and a guide shell of solid wall structure and a serpentine heat exchanger surrounding the guide shell.

Fig. 5 shows a prior art slurry bed reactor comprising a draft tube of solid wall structure, a coiled tube heat exchanger surrounding the draft tube, and a gas distributor of perforated plate structure.

Detailed Description

The "ranges" disclosed herein are in the form of lower and upper limits. There may be one or more lower limits, and one or more upper limits, respectively. The given range is defined by the selection of a lower limit and an upper limit. The selected lower and upper limits define the boundaries of the particular range. All ranges that can be defined in this manner are inclusive and combinable, i.e., any lower limit can be combined with any upper limit to form a range. For example, ranges of 60-120 and 80-110 are listed for particular parameters, with the understanding that ranges of 60-110 and 80-120 are also contemplated. Furthermore, 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 are all contemplated: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.

In the present invention, unless otherwise stated, the numerical range "a-b" represents a shorthand representation of any combination of real numbers between a and b, where a and b are both real numbers. For example, a numerical range of "0 to 5" indicates that all real numbers between "0 to 5" have been listed herein, and "0 to 5" is only a shorthand representation of the combination of these numbers.

In the present invention, all embodiments and preferred embodiments mentioned herein may be combined with each other to form a new technical solution, if not specifically stated.

In the present invention, all the technical features mentioned herein and preferred features may be combined with each other to form a new technical solution, if not specifically stated.

In the present invention, all the steps mentioned herein may be performed sequentially or randomly, if not specifically stated, but preferably sequentially. For example, the method comprises steps (a) and (b), meaning that the method may comprise steps (a) and (b) performed sequentially, and may also comprise steps (b) and (a) performed sequentially. For example, reference to the process further comprising step (c) means that step (c) may be added to the process in any order, for example, the process may comprise steps (a), (b) and (c), may also comprise steps (a), (c) and (b), may also comprise steps (c), (a) and (b), etc.

In the present invention, the term "comprising" as used herein means either an open type or a closed type unless otherwise specified. For example, the term "comprising" may mean that other components not listed may also be included, or that only listed components may be included.

In the present invention, when describing the spatial relationship of a particular component or object relative to other components or objects, the terms "inner", "outer", "above", "below", and the like, are used to indicate that the former is located inside, outside, above or below the latter, which may be in direct contact with each other, may be separated by a certain distance, or may be separated by a third component or object.

It is emphasized here that the embodiments shown in the figures and described below are merely exemplary embodiments of the invention, to which the scope of protection of the invention is not limited. The scope of the invention is defined by the claims and may include any embodiments within the scope of the claims, including but not limited to further modifications and alterations to these embodiments.

The uniformity of mass and heat transfer of some preferred slurry bed reactors is characterized hereinafter primarily on the basis of the fischer-tropsch reaction, but it is emphasized here that the use of the slurry bed reactor of the present invention is not limited to these reactions only, but can also be used in any other process that can be carried out in a gas-liquid-solid three-phase system or a gas-liquid two-phase system, and that it also allows these other processes to gain technological improvements and gains from mass and heat transfer, examples of which include physical adsorption processes, such as automobile exhaust gas treatment and plant exhaust gas treatment; chemical reactions such as hydrogenation, oxidation, chlorination, sulfonation, alkylation, carbonylation, esterification, transesterification, catalytic isomerization, and chemical absorption of the off-gas; bioengineering, such as biological fermentation, bacterial culture, etc.

Fig. 1 shows the structure of a slurry bed reactor according to an embodiment of the present invention, which comprises a reactor shell 1, and sequentially comprises a slurry inlet/outlet 13 at the bottom, a gas distributor 4, a heat exchange tube set 3, a separator 2, a partition 12, and a gas outlet 11 in this order from bottom to top.

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 the separator 2 may not be included. According to one embodiment, solid material, or a mixture of solid and liquid, or liquid material is pre-present in the slurry bed reactor before the reaction starts. At the beginning of the reaction, during the reaction and/or at the end of the reaction, the slurry material and/or the liquid material is fed in and/or out from the lower slurry inlet 13, while the gas material is fed in through the gas distributor 4. The gas material is dispersed into bubbles with smaller size under the action of the gas distributor 4, enters the inner space of the reactor above the gas distributor 4 with specific size distribution and spiral flow mode, and gas, liquid and (optional) solid materials in the inner space contact with each other while ascending, so that the target reaction, such as 'Fischer-Tropsch reaction', is generated to generate the target product, such as hydrocarbons with different chain lengths. The material then continues to rise out of the reaction zone and, in the event that liquid-gas (and optionally solid material) material separation is required, a gas separator 2 may be provided in the upper part of the reactor, gaseous materials, such as hydrocarbon target products or gaseous by-products, gaseous residual feedstocks, etc., are separated by the gas separator 2 and output from the outlet 11 at the top to a subsequent process or storage vessel, while other materials (e.g., liquid reaction feedstock, optionally solid feedstock, etc.) may descend back into the interior space of the reactor for continued reaction. According to a preferred embodiment, the gaseous starting material is fed in a continuous or intermittent manner via the gas distributor 4 during the above-mentioned reaction, more preferably in a continuous manner via the gas distributor 4. According to another preferred embodiment, during the above reaction, the liquid material (e.g. liquid feedstock or liquid solvent) is introduced into the slurry bed reactor in a continuous or intermittent manner through the slurry inlet/outlet 13 at the bottom of the reactor and optionally one or more openings provided at the periphery of the bottom of the slurry bed reactor or at the side walls of the slurry bed reactor at different heights (e.g. middle, lower or bottom), preferably the liquid material (e.g. liquid feedstock or liquid solvent) is introduced into the slurry bed reactor in a continuous or intermittent manner only through the slurry inlet/outlet 13 at the bottom. According to another embodiment of the present invention, during the above reaction, liquid materials (e.g. liquid reaction products, liquid solvents, liquid by-products, residual liquid raw materials, etc.) in the slurry bed reactor are withdrawn continuously or intermittently through the slurry inlet and outlet 13 at the bottom of the reactor and optionally one or more openings provided at the periphery of the bottom of the slurry bed reactor or at the side walls of the slurry bed reactor at different heights (e.g. middle, lower or bottom), and these withdrawn materials can be subjected to subsequent product recovery and purification, and the by-products can be separated, recovered and further processed, or directly discharged or burned. Most preferably, the slurry bed reactor level remains substantially constant throughout the reaction.

According to one embodiment of the invention, the reactor shell 1 of the slurry bed reactor is used to enclose an inner space for carrying out the reaction, and may be, for example, a stainless steel shell. In the reactor shown in fig. 1, the shell cross-sectional diameter is substantially constant, but the scope of the invention is not limited in this respect, and the reactor shell of the present application may have any desired shape and size, such as a cylinder having a varying cross-sectional diameter from top to bottom, or may be in the form of a square or rectangle in cross-section as shown in fig. 2. According to a preferred embodiment of the invention, the reactor has a longitudinal (axial) height of 5 to 100 meters, such as 10 to 80 meters, preferably 20 to 50 meters, more preferably 20 to 35 meters. According to a preferred embodiment of the invention, the reactor has the same cross-sectional diameter along the longitudinal axis from top to bottom, for example the cross-sectional diameter of the reactor may be 0.5 to 10 meters, for example 0.8 to 8 meters, or 0.9 to 7 meters, or 1 to 5 meters, or 1.2 to 3 meters, or 1.5 to 2 meters, or 1.6 to 1.8 meters. According to another preferred embodiment of the invention, the reactor has a varying cross-sectional diameter along the longitudinal axis from top to bottom, 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; for reactor upper and lower cross-sectional diameters that differ, the reactor has a smaller cross-sectional diameter along the longitudinal axis at a height of the lower portion 1/5 to 4/5, such as 1/3 to 1/2, for example an inner diameter of 0.5 to 10 meters, such as 0.8 to 8 meters, or 0.9 to 7 meters, or 1 to 5 meters, or 1.2 to 3 meters, or 1.5 to 2 meters, or 1.6 to 1.8 meters; the upper part has a larger cross-sectional diameter of 0.8-15 meters, such as 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. According to one embodiment of the present invention, as shown in FIG. 1, the region between the bottom of the reactor and the liquid level in the reactor, in which the gas and the liquid or slurry are mixed with each other, is called a "gas-slurry mixing zone", and the reaction occurs during the circulation back flow. At least the heat exchange tube set and the gas distributor of the present invention are disposed in this region, and both the heat exchange tube set and the gas distributor are completely submerged below the liquid surface. According to an embodiment of the present invention, the lower end opening of the gas-liquid separator 2 also extends below the liquid level, 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 bundle. According to one embodiment of the invention, as shown in FIG. 1, the region between the upper surface of the liquid and the lower surface of the partition 12, in which the gas rises away from the liquid/slurry, and during which the two or more liquids entrained in the gas fall back down into the liquid below, is referred to as the "gas-slurry separation zone", in which the body of the gas-liquid separator 2 is disposed, preferably along the central axis of the reactor. According to one embodiment of the present invention, as shown in FIG. 1, the region from above the partition plate 12 to the top of the reactor is called "gas phase region", in which the gas is discharged from the gas outlet 11 at the top of the reactor after separating only the remaining small amount of liquid droplets, and the recovered liquid flows into the liquid phase of the gas-slurry mixing zone through the gas-liquid separator 2.

According to one embodiment of the invention, the top and bottom of the reactor shell 1 are hemispherical, or are part of a hemisphere. For example, it may be 90%, 80%, 70%, 60%, 50% or 40% of the hemisphere.

In the embodiment shown in fig. 1, the slurry inlet/outlet 13 is simply connected to a pipe, but may be further modified as necessary. For example, one or more devices selected from the group consisting of: valves, flow meters, heat exchange devices, baffles, flanges, threads, pins, fins, and any combination thereof. In addition, a plurality of slurry inlets and outlets 13 can be arranged at the bottom of the reactor, and the inlets and outlets can be arranged at the bottom of the reactor in any mode, for example, uniformly arranged at the periphery or the central position of the bottom of the reactor, and can be in the form of simple openings or nozzles. In embodiments where the reactor cross-section is square or rectangular, the access arrangements described above may also be used.

Above the inlet there is a gas distributor. According to a less preferred embodiment of the present invention, the gas distributor may be in various forms, such as an open-cell plate type gas distributor having upper and lower plates and openings in the plates, the gas raw material being introduced from a space between the two plates through a connecting pipe and mixed with the liquid phase in the form of fine bubbles through the openings in the plates; further, for example, the plurality of conduits may be in the form of an array of conduits with openings, and more specifically, the plurality of conduits may be arranged in parallel rows, intersecting grids, concentric circles or concentric squares, etc., and each conduit is connected to at least one gas inlet conduit, and each conduit may be isolated from or in fluid communication with other conduits.

According to a preferred embodiment, the gas distributor has the structure shown in fig. 2, and as shown in fig. 2, the gas distributor 4 comprises a gas distributor inlet 41, a gas distributor upper straight tube 42, a gas distributor spiral tube set 43, a gas distributor lower straight tube 44, a gas distributor annular tube 45 and a gas distributor gas distribution tube 46.

According to one embodiment of the invention, the gas distributor upper straight pipes and lower straight pipes are respectively located in two mutually parallel planes, each upper straight pipe and each lower straight pipe radially extend in a cross section perpendicular to the longitudinal axis of the slurry bed reactor, the radial extension directions of the upper straight pipes and the lower straight pipes are different, and each upper straight pipe and each lower straight pipe are communicated through a set of spiral pipe current collectors. According to a preferred embodiment of the invention, the gas distributor comprises 2 to 20 groups, for example 3 to 12 groups, or 3 to 9 groups, or 3 to 6 groups of sets of spiral tubes, preferably of the same shape and structure as one another, arranged in a centrosymmetric manner with respect to the longitudinal axis of the reactor. Each set of coils is in fluid communication with a corresponding upper straight tube 42 and a corresponding lower straight tube 44, i.e., there are as many sets 43 of coils as there are upper straight tubes 42 and lower straight tubes 44. According to an embodiment of the present invention, when viewed vertically down the longitudinal axis of the reactor, it can be seen that the upper straight tube 42 and the lower straight tube 44 associated with the same set of coils 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 (cross-section perpendicular to the longitudinal axis of the reactor) and have an angle of 1 to 40 degrees, such as 5 to 35 degrees, 8 to 30 degrees, 10 to 28 degrees, 12 to 25 degrees, 15 to 20 degrees, 16 to 18 degrees, or any combination of any two of these values. According to one embodiment of the present invention, all of the upper straight tubes 42 have the same length, which is 70 to 150% of the radius of the cross-section (the section perpendicular to the longitudinal axis of the reactor) of the reactor, or 80 to 120%, or 85 to 110%, or 90 to 105%, or 95 to 102%, or 98 to 101%, or a range of values that can be obtained by combining any two of the above values, and when the length of the upper straight tubes exceeds the radius of the cross-section of the reactor, the portion of the upper straight tubes that exceeds the length of the upper straight tubes extends to the outside of the reactor through the side wall of the reactor (as shown in FIG. 1) and is connected to a gas source disposed outside the reactor; when the length of the upper straight pipe exceeds the radius of the cross section of the reactor, a gas pipe of an external gas source is introduced into the reactor and is connected with the outer tail end of the upper straight pipe. According to one embodiment of the invention, all of the lower straight tubes 44 have the same length, which is 50 to 99%, or 60 to 95%, or 70 to 90%, or 75 to 85%, or 78 to 82%, or 70 to 80% of the radius of the reactor cross-section (cross-section perpendicular to the longitudinal axis of the reactor), or may be within a range of values obtained by combining any two of the above values.

According to one embodiment of the present invention, each set of coils 43 includes 2 to 20 coils, for example, the number of coils in each set of coils 43 may be 3 to 15, or 4 to 12, or 4 to 10, or 4 to 8, or 4 to 6, or 4 to 5. The helical tubes extend in a clockwise or counterclockwise manner from top to bottom in an equally spaced or unequally spaced manner, parallel to each other or unparallel, to fluidly communicate each upper straight tube with each lower straight tube. Preferably, the extension direction of the spiral tube is matched with the extension direction of a group of spiral plate-shaped heat exchange tube sets corresponding to the heat exchange tube sets above the spiral tube.

Below the gas distributor 4 there is a plurality of gas distributor loops 45, for example comprising 2 to 15 loops 45, for example comprising 3-12 loops 45, or comprising 3-10 loops 45, or comprising 3-9 loops, or comprising 3-8 loops, or comprising 3-6 loops, or comprising 3-5 loops, or comprising 3-4 loops, arranged equidistantly or non-equidistantly in a concentric circle. Each of which is in fluid communication with all of the lower straight tubes 44. The lower surface of each loop (preferably at the lowermost apex of the circular cross-section of the loop) is uniformly provided with 8 to 100 gas distributor distribution tubes 46, 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 tubes 46 are uniformly disposed on the lower surface of the loop (preferably, at the lowermost vertex of the circular cross-section of the loop), more preferably, the distance between any two adjacent gas distribution tubes 46 on each loop is the same, and more preferably, the distance between any two adjacent gas distribution tubes 46 on all loops is the same. According to a preferred embodiment of the present invention, the gas distributor gas distribution pipe is at an angle of 5 degrees to 60 degrees, such as 8 to 55 degrees, or 10 to 52 degrees, or 12 to 50 degrees, or 15 to 45 degrees, or 18 to 42 degrees, or 20 to 40 degrees, or 22 to 35 degrees, or 25 to 30 degrees, with respect to the longitudinal axis of the slurry bed reactor, or may be within a range of values where any two of the above values are combined. The component of the gas distributor gas distribution pipe in a section perpendicular to the longitudinal axis of the slurry bed reactor is at an angle of 3-45 degrees, such as 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 within a range of values obtained by combining any two of the above values, with the annular pipe. In a preferred embodiment according to the present invention, all the gas distribution pipes 46 have the same direction. According to a most preferred embodiment, all the air distribution pipes 46 are oriented in a direction matching the extension direction of the spirals in the set 43, which overall may constitute a spiral trend in the same direction. According to one embodiment of the present invention, the gas distributor gas distribution pipe is a passage formed in a wall of a lower surface of the annular pipe, or a pipe protruding from a lower surface of the annular pipe. In other words, each of the air distribution pipes 46 may be a passage formed in the annular pipe wall, not protruding from the annular pipe wall, or each of the air distribution pipes 46 may be a pipe formed on the lower surface of the annular pipe, protruding from the annular pipe wall.

According to an embodiment of the present invention, each set of coils 43 is identical to and centrosymmetric to the other sets of coils, and the upper straight pipe 42 and the lower straight pipe 44 connected to each set of coils 43 are also identical to and centrosymmetric to the other upper straight pipes and the lower straight pipes, respectively.

According to an embodiment of the present invention, the gas distributor inlet 41 is located at the outer end of the gas distributor upper straight tube 42; the gas distributor ring pipe 45 and the gas distributor lower straight pipe 44 are at the same horizontal height; a gas distributor gas distribution pipe 46 is mounted below the gas distributor collar 45. According to the embodiment of the present invention shown in FIG. 2, there are 3 sets of gas distributor helix tube sets 43, and thus there are 3 gas distributor inlets 41, gas distributor upper straight tubes 42, and gas distributor lower straight tubes 44, respectively. According to one embodiment of the invention, each set of gas distributor coils rises spirally from the lower straight tube to the upper straight tube in a clockwise or counterclockwise manner, and the number of turns of the spiral (i.e. the number of turns of the spiral completed by the spiral header starting from the lower straight tube and ending at the upper straight tube, where the number of turns represents the trajectory of the spiral viewed vertically downward along the central longitudinal axis of one spiral, and the proportion of the trajectory of the observed spiral formed at the interface perpendicular to the central longitudinal axis to one complete circle, i.e. one complete spiral of one cycle, expressed in decimal numbers) may be 0.01 to 0.3 turns, alternatively 0.05 to 0.25 turns, alternatively 0.08 to 0.20 turns, alternatively 0.09 to 0.15 turns, alternatively 0.1 to 0.12 turns. According to one embodiment of the invention, all the lower straight tubes are in the same plane, which is perpendicular to the longitudinal axis of the reactor, and all the 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 of all the lower straight tubes to the plane of all the upper straight tubes with respect to the total height in the longitudinal direction of the reactor is 0.1 to 9%, alternatively 0.5 to 8%, alternatively 1 to 7%, alternatively 2 to 6%, alternatively 3 to 5%, alternatively 4 to 5%. According to one embodiment of the invention, the ratio of the diameter of the outermost loop to the cross-sectional diameter of the reactor may be in the range of 50 to 99%, alternatively 60 to 95%, alternatively 70 to 90%, alternatively 75 to 85%, alternatively 78 to 82%, alternatively 70 to 80%, or may be within the range of any two of the above values taken in combination. According to one embodiment of the invention, the ratio of the diameter of the innermost loop to the cross-sectional diameter of the reactor may be in the range of 5 to 60%, alternatively 8 to 55%, alternatively 10 to 50%, alternatively 12 to 45%, alternatively 15 to 40%, alternatively 18 to 35%, alternatively 20 to 30%, alternatively 22 to 25%, or may be within the range of any two of the above values taken in combination. The remaining collars, if any, are disposed in an equally spaced manner between the outermost collar and the innermost collar.

In the present invention, "inner diameter of the tube" means an inner diameter (in the case of a tube having a circular cross section) or an inner equivalent diameter (in the case of a tube having a cross section of other shape such as a square, rectangle, ellipse, etc.) after removing the wall thickness in a cross section perpendicular to the central longitudinal axis of the tube. "equivalent diameter" means the diameter of a circle having the same area as a certain non-circular shape, for example, assuming a square cross section with a side length of 1 mm and an area of 1 mm square, the equivalent diameter is the diameter of a circle with an area of 1 mm square [ e.g., equivalent diameter d ═ 2/pi%²)]. Equivalent diameters for other geometries can also be calculated in the same manner.

According to an embodiment of the present invention, the aspect ratio (ratio of length to inner diameter) of the upper straight tube 42 is 50 to 4, alternatively 40 to 4.5, alternatively 30 to 4.8, alternatively 20 to 5, alternatively 15 to 5.2, alternatively 12 to 5.5, alternatively 10 to 6, alternatively 9 to 6, alternatively 8 to 6, alternatively 7 to 6, or may be within a range where any two of the above values are combined.

According to one embodiment of the present invention, each of the coils in the coil assembly 43 has the same inner diameter as each other. According to one embodiment of the present invention, the ratio of the inner diameter of each of the coils in the coil assembly 43 to the inner diameter of the upper straight tube 42 is 0.1 to 0.8, alternatively 0.2 to 0.7, alternatively 0.3 to 0.6, alternatively 0.4 to 0.5, or may be within a range of values where any two of the above values are combined. According to one embodiment of the present invention, each of the lower straight tubes 44 has the same inner diameter as each other. 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, alternatively 0.4 to 0.8, alternatively 0.5 to 0.7, alternatively 0.45 to 0.6, or may be within a range of values where any two of the above values are combined. According to one embodiment of the invention, each collar 45 has the same inner diameter as each other. According to one embodiment of the present invention, the ratio of the inner diameter of the loop pipe 45 to the inner diameter of the upper straight pipe 42 is 0.1 to 0.8, alternatively 0.2 to 0.7, alternatively 0.3 to 0.6, alternatively 0.4 to 0.5, or may be within a range where any two of the above values are combined. According to one embodiment of the present invention, each of the tubes 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 gas distribution pipe 46 to the inner diameter of the upper straight pipe 42 is 0.01 to 0.3, alternatively 0.02 to 0.25, alternatively 0.05 to 0.2, alternatively 0.08 to 0.1, or may be within a range of values where any two of the above values are combined.

In accordance with a preferred embodiment of the present invention, each of the plurality of coils is positioned in alignment with each of the plurality of collars.

For example, in the embodiment shown in fig. 2, the number of the gas distributor collars 45 is 4, and the cylindrical surfaces where the circular lines of the 4 gas distributor collars 45 are located are respectively overlapped with the cylindrical surfaces where the 4 spiral gas pipes of the gas distributor spiral pipe set 43 are located from inside to outside, that is, each gas distributor collar 45 is located right below each spiral gas pipe.

In this embodiment, the axis of the gas distributor gas distribution pipe 46 is tangent to the cylindrical surface where the circular 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 of the helical gas pipe directly above it.

In the interior space above the gas distributor 4, in particular below the level of the slurry bed, the gas-liquid two-phase material and optionally also the solid-phase material come into contact with one another and undergo a reaction, for example a Fischer-Tropsch reaction.

According to a less preferred embodiment of the invention, a draft tube, which may be formed by a non-porous wall, may be provided above the gas distributor 4, so that the gas-liquid mixture flows substantially upwards outside the draft tube and substantially downwards inside the draft tube during the reaction, thereby establishing a material circulation flow in the reactor. According to a less preferred embodiment of the invention, one or more heat exchangers surrounding the guide shell may be arranged in the space between the outer surface of the guide shell and the inner surface of the reactor shell, and the heat exchangers may be of any configuration, such as one or more spiral, serpentine, circular or linear heat exchange tubes.

But according to a preferred embodiment of the invention, a specially designed heat exchanger tube set 3 according to the invention is arranged above the gas distributor. According to a preferred embodiment of the present invention, the heat exchange tube bank 3 comprises a flow guide cylindrical heat exchange tube bank 34 and one or more sets of spiral plate-shaped heat exchange tubes 33, the flow guide cylindrical heat exchange tube bank 34 and the spiral plate-shaped heat exchange tubes 33 being in fluid communication. According to a preferred embodiment of the present invention, the heat exchange tube set 3 is disposed above the gas distributor 4 in the gas-slurry mixing zone, and the top end of the heat exchange tube set is not below the liquid level or slurry level, for example, is not below the liquid level or slurry level by 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, or any two of the above values are combined to obtain a value range.

According to a preferred embodiment of the present invention, the heat exchange tube set 3 comprises a spiral plate-shaped heat exchange tube set 33, a guide cylindrical heat exchange tube set 34, an upper heat exchange straight tube 35, an upper heat exchange circular tube 36, a lower heat exchange straight tube 38, a lower heat exchange circular tube 37, a coolant inlet 32 and a coolant outlet 31, or the heat exchange tube set 3 is composed of a spiral plate-shaped heat exchange tube set 33, a guide cylindrical heat exchange tube set 34, an upper heat exchange straight tube 35, an upper heat exchange circular tube 36, a lower heat exchange straight tube 38, a lower heat exchange circular tube 37, a coolant inlet 32 and a coolant outlet 31.

According to a preferred embodiment of the present invention, the central axis of the heat exchange tube set 3 overlaps with the central axis of the reactor. According to a preferred embodiment of the present invention, the guide shell type heat exchange tube set 34 is composed of a plurality of spiral heat exchange tubes (hereinafter also referred to as "guide shell type heat exchange tubes") located in the same cylindrical surface. According to one embodiment of the present invention, the number of the guide shell heat exchange tubes in the guide shell heat exchange tube set 34 may be 3 to 100, such as 6 to 90, or 12 to 80, or 15 to 70, or 16 to 60, or 18 to 50, or 20 to 40, or 25 to 35, or 30 to 32, or any two of the above values may be combined to obtain a value range. According to a preferred embodiment of the present invention, all of the "draft tube heat exchange tubes" spiral up in a uniform manner along a common cylindrical profile, thereby collectively forming a cylindrical structure resembling a conventional draft tube, and thus the overall combination of the draft tube heat exchange tubes is referred to as a draft tube heat exchange manifold 34. However, the guide shell type heat exchange tube set 34 is different from the conventional guide shell in that the periphery of the tube set is composed of a plurality of heat exchange tubes, the heat exchange tubes are not closed, and slurry can enter and exit from gaps among the heat exchange tubes to a certain extent. In accordance with a preferred embodiment of the present invention, all of the "draft tube heat exchange tubes" within the draft tube bank 34 spiral up in a clockwise or counterclockwise manner along the cylindrical contour of the outer periphery of the bank 34 in a parallel manner to one another, the number of turns of the helix (i.e., the number of turns of the helix completed by a draft tube heat exchanger tube starting from the lower annular tube 37 and ending at the upper annular tube 36, where the number of turns represents the trajectory of the helix viewed vertically down the central longitudinal axis of a helix, and the fraction of the trajectory of the observed helix formed at the interface perpendicular to the central longitudinal axis to a complete circle, i.e., a complete helix of one period, expressed in decimal numbers) may be 0.5 to 3 turns, or 0.8 to 2.5 turns, or 0.9 to 2, or 1 to 1.8, or 1 to 1.5, or a combination of any two of the foregoing. According to the preferred embodiment of the present invention shown in fig. 1, each draft tube heat exchange tube extends spirally upward in a counterclockwise manner with a spiral period of 1. According to a preferred embodiment of the present invention, the upper and lower ends of all the draft tube heat exchange tubes are connected to an upper heat exchange loop 36 (also referred to as a top heat exchange tube ring, herein, the upper heat exchange loop and the top heat exchange tube ring are used interchangeably) and a lower heat exchange loop 37 (also referred to as a bottom heat exchange tube ring, herein, the lower heat exchange loop and the bottom heat exchange tube ring are used interchangeably), which are in fluid communication with the upper heat exchange loop 36 and the lower heat exchange loop 37, respectively. According to one embodiment of the present invention, in addition to the top and bottom heat exchange tube rings described above, one or more middle heat exchange tube rings may optionally be provided at different heights of the collection of draft tube heat exchange tubes, each draft tube heat exchange tube being in fluid communication with the middle heat exchange tube ring, respectively. For example, the number of middle heat exchange tube rings may be in the range of 1-10, or 2-6, or 3-5, or any combination of the two. These intermediate heat exchange tubes may be disposed at uniform intervals at different elevations in the collection of draft tube heat exchange tubes 34, each in fluid communication with each of the draft tube heat exchange tubes in the collection of draft tube heat exchange tubes 34, and may optionally have a coolant inlet and/or a coolant outlet for additional introduction/withdrawal of coolant at different elevations.

According to a preferred embodiment of the present invention, 1 to 16, e.g., 2 to 15, or 3 to 12, or 3 to 9, or 3 to 6, sets of spiral plate-shaped heat exchange tubes, each set comprising 2 to 20, e.g., 3 to 18, or 3 to 15, or 3 to 12, or 3 to 9, or 4 to 6, spiral plate heat exchange tubes, are arranged in a centrosymmetric manner around the middle guide shell-shaped heat exchange tube set. According to one embodiment of the invention, at the bottom of the heat exchange tube set, the inlets of all the heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed along the radial direction of the guide cylindrical heat exchange tube set outside the guide cylindrical heat exchange tube set and are respectively in fluid communication with the same heat exchange lower straight tube 38; at the top of the heat exchange tube set, outlets of all heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed on the outer side of the guide flow cylindrical heat exchange tube set along the radial direction of the guide flow cylindrical heat exchange tube set and are respectively communicated with the same heat exchange upper straight tube 35 in a fluid mode; the spiral plate heat exchange tubes in each group of spiral plate-shaped heat exchange tube sets are uniformly spaced from each other and spirally ascend around the flow guide cylindrical heat exchange tube set in a mutually parallel mode. Therefore, all the spiral plate heat exchange tubes in each group of spiral plate heat exchange tubes are in fluid communication with the upper heat exchange straight tube 35 and the lower heat exchange straight tube 38, and the number of the groups of spiral plate heat exchange tubes is correspondingly the number of the upper heat exchange straight tubes and the lower heat exchange straight tubes. According to a preferred embodiment of the present invention, the outer end of each heat exchanging upper straight tube 35 has a coolant outlet 31, and the outer end of each heat exchanging lower straight tube 38 has a coolant inlet 32. In accordance with a preferred embodiment of the present invention, all of the sets of spiral plate shaped heat exchange tubes are identical in size and shape to each other. In accordance with a preferred embodiment of the present invention each of the sets of spiral plate heat exchange tubes is of the same size and shape as the other. All the spiral plate heat exchange tubes in the heat exchange tube set can spirally extend from the lower heat exchange straight tube 38 at the lower part to the upper heat exchange straight tube 35 at the upper part in a clockwise or anticlockwise mode. In a preferred embodiment according to the present invention, the number of turns of the helix of each of the plurality of sets of spiral plate heat exchange tubes (i.e., the number of turns of the helix completed by one of the spiral plate heat exchange tubes starting from the lower straight tube 38 and ending at the upper straight tube 35, where the number of turns represents the fraction of the trajectory of the helix viewed vertically downward along the central longitudinal axis of one helix, the fraction of the trajectory of the observed helix at the interface perpendicular to the central longitudinal axis forming one complete circle, i.e., one complete helix of one cycle, expressed in decimal numbers) can be in the range of 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 a combination of any two of the above. According to the preferred embodiment of the present invention as shown in fig. 1, each of the spiral plate heat exchange tubes extends spirally upward in a counterclockwise manner with a spiral period of 1.

According to one embodiment of the invention, the ratio of the vertical height from the plane of the heat exchange lower loop 37 to the plane of the heat exchange upper loop 36 relative to the total height in the longitudinal direction of the reactor is in the range of 10 to 90%, alternatively 15 to 80%, alternatively 20 to 70%, alternatively 30 to 60%, alternatively 40 to 55%, alternatively 45 to 50%, or a combination of any two of the above. According to one embodiment of the invention, the lower heat exchange loop 37 and the upper heat exchange loop 36 are aligned with each other and have the same dimensions, and the ratio of the diameter of the lower heat exchange loop 37 and the upper heat exchange loop 36 (i.e. the diameter of the cross-section of the flow guide tube-shaped heat exchange tube bundle 34) to the diameter of the cross-section of the reactor may be 10 to 70%, or 15 to 65%, or 20 to 60%, or 25 to 55%, or 30 to 50%, or 35 to 40%, or may be within the range of any two of the above values taken in combination.

According to an embodiment of the present invention, the aspect ratio (ratio of length to inner diameter) of the heat exchange upper straight tube 35 and the heat exchange lower straight 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 may be within a range obtained by combining any two of the above values. According to an embodiment of the present invention, the inner diameter of the heat exchange upper straight pipe 35 and the heat exchange lower straight pipe 37 may be 1 to 30mm, for example, 2 to 25 mm, or 3 to 22 mm, or 5 to 20 mm, or 8 to 18 mm, or 10 to 15 mm, or 12 to 14 mm, or may be within a range obtained by combining any two of the above values.

According to one embodiment of the invention, the heat exchange upper loop 36 and the heat exchange lower loop 37 have exactly the same size and shape. According to one embodiment of the invention, the ratio of the inner diameter of the heat exchange upper straight pipe 35 to the inner diameter of the heat exchange upper loop 36 and the heat exchange lower loop 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 may be within a range of values where any two of the above values are combined.

According to one embodiment of the present invention, each of the spiral tubes in the flow-guiding cylindrical heat exchange tube set 34 has the same inner diameter as each other. According to one embodiment of the present invention, the ratio of the inside diameter of each spiral tube in the flow-guiding cylindrical heat exchange tube set 34 to the inside diameter of the heat exchange upper loop 36 is 0.1 to 0.8, alternatively 0.2 to 0.7, alternatively 0.3 to 0.6, alternatively 0.4 to 0.5, or may be within a range of values 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 tube in the collection of spiral plate shaped heat exchange tubes 33 to the inner diameter of the heat exchange upper loop 36 is from 0.1 to 0.8, alternatively from 0.2 to 0.7, alternatively from 0.3 to 0.6, alternatively from 0.4 to 0.5, or alternatively can be within the range of any combination of the two values.

According to a preferred embodiment, the heat exchange tube may be made of a material selected from the group consisting of: stainless steel, plexiglass, copper, iron, ceramic, glass, aluminum, and the like. During the reaction, a heat exchange fluid (e.g., water, heat exchange oil, carbon dioxide, etc.) flows through the heat exchange tubes, providing fine adjustments to the temperature in the reactor.

Without wishing to be bound by any particular theory, the inventors surprisingly found that the arrangement of the heat exchange tube not only can improve the heat transfer efficiency, but also effectively combines the mixing and flow guiding functions of the flow guiding cylinder and the heat transfer function of the heat exchange tube due to the specific structural design, thereby reducing the influence of adverse factors such as adverse back mixing, dead zones, vortexes, large bubbles and the like in the reaction system, and finally showing the further improvement of the catalytic reaction effect in the reactor.

The upper part of the inner space of the reactor may be optionally provided with a separator as required. After the reaction (e.g. fischer-tropsch reaction) has been carried out, the gaseous stream, in which a portion of the liquids and solids are entrained, rises to the separator. The separator may be any separator known in the art that can be used to perform three phase separation of gas, liquid and solid, preferably a cyclone separator 2. According to a preferred embodiment, the cyclone 2 is arranged coaxially with the reactor housing 1; the cyclone separator 2 comprises, from top to bottom, a cyclone gas phase outlet 21 in the gas phase zone, a cyclone inlet 22 in the gas slurry separation zone, and a cyclone slurry outlet 23 in the gas slurry mixing zone. According to a preferred embodiment the direction of rotation of the fluid in the cyclone 2 is clockwise in plan view. According to a preferred embodiment, the separator further comprises downstream thereof a baffle, a demister or the like. After separation of the liquid and solids in the separator, the gaseous material rises from the separator through the partition and is then discharged from the reactor top outlet 11. While the liquid and solid components separated in the separator flow back down into the slurry. According to a preferred embodiment, the separator is a cyclone 2 comprising a dipleg, the lower end of which extends below the liquid level in the reactor. In a preferred embodiment of the invention, the reactor according to the invention comprises 1 to 20, preferably 1 to 10, separation devices which are distributed uniformly around the inner wall below the partition.

In the embodiment shown in fig. 1, the gas phase outlet 11 is simply connected to one pipe, but may be further modified as needed. For example, one or more devices selected from the group consisting of: valves, flow meters, heat exchange devices, baffles, flanges, threads, pins, fins, and any combination thereof.

In addition to the apparatus shown in FIG. 1, the reactor of the present invention may also include other apparatuses as needed, for example: a settling tube, which may be a ratio pipe having an inner diameter smaller than the diameter of the cross-section of the reactor, disposed in the inner space of the reactor in a direction parallel to the longitudinal axis of the reactor for guiding the material to settle down in the tube; a material circulation system comprising a circulation inlet located on a wall of the shell in the middle of the reactor, a circulation pipe located outside or inside the reactor shell, and a circulation outlet located at the bottom of the reactor (but above the inlet at the bottom of the shell), the circulation system being adapted to draw a portion of the material in the reactor from the circulation inlet during the course of the reaction and transport it via the circulation pipe to the circulation outlet at the bottom, thereby establishing an additional circulation of the material in the reactor to promote mass and heat transfer; a heating/cooling device; temperature/pressure/flow rate sensors; flow control members such as baffles, flow directing plates, fins, stirring blades, and the like. One or more of the above-mentioned means may be additionally added to the slurry bed reactor as needed, but according to a preferred embodiment of the present invention, the desired superior properties of mass and heat transfer are achieved without the use of the above-mentioned other means by the preferred design of the distribution plate.

According to a preferred embodiment of the invention, the reactor of the invention is shown in figures 1 and 2 and it operates in the following manner: before the reactor starts to operate, liquid materials or solid-liquid mixed slurry is filled from the slurry inlet and outlet 13, the liquid level of the slurry is higher than the highest position of the heat exchange tube set 3, and then the reactor is under a proper reaction condition. After the reactor starts to operate, the gas-phase reactant is introduced from the gas distributor inlet 41, is sprayed out from the gas distributor gas distribution pipe 46, and transmits the kinetic energy thereof 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, the slurry below the gas distributor gas distribution pipe 46 starts to flow spirally clockwise under the combined action of all the gas distributor gas distribution pipes 46. After the gas phase is sprayed out from the gas distribution pipe 46 of the gas distributor, bubbles are formed in the slurry, the vertical speed of the bubbles is changed from downward to upward under the driving of buoyancy, and the slurry around the bubbles is driven to flow upward. Due to the existence of the guide flow cylindrical heat exchange tube set 34, the slurry flows upwards outside the guide flow cylindrical heat exchange tube set 34 and downwards inside the guide flow cylindrical heat exchange tube set 34, so that a better circulation effect is generated in the whole reactor. Outside guide shell shape heat exchange tube set 34, because the existence of gas distributor spiral tube set 43 and spiral heat exchange tube set 33, and the effect of blocking of spiral tube set to thick liquids is bigger, and the effect of blocking to the bubble is littleer, and most bubbles can pass in the gap of spiral tube set at the in-process that rises, and most thick liquids can rise along spiral tube set spiral to the speed difference of bubble and thick liquids has been increased, has strengthened mass transfer effect. When slurry outside the guide pipe-shaped heat exchange tube set 34 flows above the heat exchange tube set 3, the slurry can be turned into the guide pipe-shaped heat exchange tube set 34 in a vortex mode, the speed difference between the gas phase and the slurry at the vortex position is great, and the mass transfer effect is excellent.

The cyclone separator 2 is positioned at the top of the reactor, a gas phase outlet 21 of the cyclone separator extends to the upper part of the partition plate 12, and a liquid phase outlet 23 of the cyclone separator is submerged below the liquid level of the slurry bed and extends into a cylindrical surface where the guide flow cylindrical heat exchange tube set 34 is positioned. The technical scheme can ensure that the slurry separated by the cyclone separator 2 is directly poured into the guide flow cylindrical heat exchange tube set 34 with higher density, and promote the fluid circulation inside and outside the guide flow cylindrical heat exchange tube set 34.

Due to the action of centrifugal force, part of bubbles can be discharged into the guide cylindrical heat exchange tube set 34 by slurry which rises spirally outside the guide cylindrical heat exchange tube set 34, and the bubbles which are driven to move upwards by buoyancy and the slurry which flows downwards in the guide cylindrical heat exchange tube set 34 flow reversely, so that the mass transfer effect is enhanced.

As the Fischer-Tropsch synthesis reaction is strongly exothermic, heat needs to be timely removed through the heat exchange tube set 3, the temperature of the slurry is maintained within the range of 250-300 ℃, and the typical preferred temperature is 255-265 ℃. The purpose of heat removal can be achieved by controlling the flow and temperature of the introduced cooling water.

Any two or more of the above-described embodiments of the present invention may be combined with each other arbitrarily, and such combinations are also included in the present general inventive concept.

Examples

Preferred embodiments of the present invention are specifically exemplified in the following examples, but it should be understood that the scope of the present invention is not limited thereto.

In the following examples and comparative examples, a number of reaction systems were constructed, the effect of which on the fischer-tropsch reaction was examined by designing the reactor configuration, distribution plates and heat exchangers therein.

Examples 1 to 3 and comparative example 1

In the following examples 1 to 3, the slurry bed reactors shown in FIGS. 1, 3 and 4 were used, respectively, in which the reactor shell was made of stainless steel, the height of the "slurry mixing zone" for receiving the slurry therebelow from the bottom to the liquid surface of the reactor was 9 m, the reactor shell was formed into a uniform cylindrical shape from the top to the bottom, the inner diameter was 2m, the total axial height of the reactor was 11.5 m, 1 gas-liquid/solid cyclone separating device was disposed at the top of the reactor, and the slurry mixing zone in the reactor was charged with 36 tons of liquid paraffin and 1.8 tons of cobalt-based catalyst (chemical formula of Co-based catalyst was Co) in advance before the reaction started₂C, according to DOI: 10.1038/nature 19786), the catalyst being present in the slurry in an amount of 5 wt%.

At the start of the reaction, the raw material gas was supplied at 0.18 m.s^-1Is fed into the reactor from an inlet at the bottom of the reactor so that a 503 standard square is fed into the reactor per hourA feed gas comprising 49% by volume of hydrogen, 49% by volume of CO and 2% by volume of nitrogen. The pressure in the reactor during the reaction was maintained at 1.0MPa, and the target temperature was set at 260 ℃. The raw material gas input from the gas distributor is subjected to gas distribution through the distribution plate, and then rises in a slurry bed layer in a dispersed manner, bubbles drive slurry in the bed layer and a catalyst to flow upwards together to reach the surface of the slurry, in the process, the raw material gas, liquid paraffin and the catalyst are contacted with each other, the raw material gas is subjected to Fischer-Tropsch synthesis reaction under the action of the catalyst to generate wax and hydrocarbon oil, and meanwhile, part of byproduct light hydrocarbons are generated. The gaseous material detached from the surface of the slurry, lifted with a portion of the droplets and fine solids, and after separation by means of a cyclone, the mixture of product and by-product was removed from the outlet, and the product was characterized and analyzed by means of a gas chromatograph, model GC-14C, manufactured by shimadzu corporation, the results of which are summarized in table 1. The majority of the liquid and solid material moves laterally at the slurry surface towards the reactor shell, descends along the shell back to the distributor plate, repeats the slurry bed reaction process described above, and the liquid and solids recovered at the cyclone return to the level of the slurry bed via the blanking leg of the cyclone, also moves laterally towards the reactor shell, descends along the shell back to the distributor plate, repeats the slurry bed reaction process described above.

The different designs of the comparative examples and examples of the invention are as follows:

example 1

The slurry bed reactor of example 1 was designed in the manner described above, wherein the gas distributor 4 shown in FIG. 2 was used, and the axial length of the upper straight pipe 42 in the gas distributor 4 was 1000mm and the inner diameter was 132 mm; the axial length of the lower straight pipe 44 is 800mm, and the inner diameter is 112 mm; when viewed downwards 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 cross section of the reactor respectively, and the included angle between the upper straight tube 42 and the lower straight tube 44 is 30 degrees; all the upper straight pipes 42 are in the same plane, all the lower straight pipes 44 are in the same plane, and the vertical height between the plane of the upper straight pipes 42 and the plane of the lower straight pipes 44 is 600 mm; the gas distributor comprises three groups of gas distributor spiral tube sets 44, each group comprises four spiral tubes, the spiral degree of each spiral tube is 0.1 circle, and the inner diameter of each spiral tube is 92 mm; the heat exchanger comprises four annular tubes 45, the diameter of the outermost annular tube 45 is 1600mm, the diameter of the innermost annular tube 45 is 400mm, the rest two annular tubes are arranged between the outermost annular tube and the innermost annular tube at equal intervals, the number of the air distribution tubes 46 arranged from the outermost annular tube to the lower surface of the innermost annular tube is 120, 90, 60 and 30 respectively, the inclination angle of each air distribution tube 46 is the same as the inclination direction of the guide cylinder heat exchange tube at the bottom of the guide cylinder heat exchange tube set opposite to the inclination angle of the guide cylinder heat exchange tube set, and the inner diameter of each air distribution tube 46 is 3 mm.

The heat exchange tube set 3 is characterized in that the inner diameters of the heat exchange upper straight tubes 36 and the heat exchange lower straight tubes 37 are 60mm, the heat exchange upper straight tubes and the heat exchange lower straight tubes are totally three, all the heat exchange upper straight tubes 36 are in the same plane, all the heat exchange lower straight tubes 37 are in the same plane, and the vertical height between the plane of the upper straight tubes 36 and the plane of the lower straight tubes 37 is 6000 mm; the diameter of the heat exchange upper ring pipe 36 and the heat exchange lower ring pipe 37 is 800mm, the inner diameter is 60mm, 24 heat exchange pipes are arranged in the guide cylinder type heat exchange pipes in a centralized mode, the spiral degree of each heat exchange pipe is 1 circle, and the inner diameter is 60 mm. Three groups of spiral plate-shaped heat exchange tube sets 33 are arranged in total, four spiral heat exchange tubes are arranged in each group, the spiral degree of the four heat exchange tubes is 1 circle, and the inner diameter is 60 mm. The vertical distance between the upper end of the heat exchange tube set 3 and the liquid level is 400 mm. Condensed water at normal temperature was supplied into the heat exchange tube at a flow rate of 3.23 m/sec.

Example 2

The slurry bed reactor of example 2 was designed in the same manner as in example 1 except that the gas distributor 4 shown in FIG. 2 was not used in the reactor, but a porous plate gas distributor 5 consisting of a gas phase inlet 51, a gas chamber 52 and a porous plate 53, respectively, from the bottom up, which were constituent parts of the reactor shell 1 instead of separate parts like the gas distributor 4 in example 1 was used. The slurry inlet and outlet 13 in example 1 was changed to a gas phase inlet 51 in example 2, and the inner diameter thereof was 80 mm. Above the gas phase inlet 51 is a gas chamber 52 having 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 perforated plate 53. The diameter of the porous plate 53 is equal to the inner diameter of the reactor shell 1, four circles of holes are distributed on the porous plate, the circle diameter and the number of the holes of each circle correspond to the diameter of the annular pipe 45 of the gas distributor 4 and the number of the gas distribution pipes arranged on the lower surface of each annular pipe one by one, and 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 of example 1 was moved to the cylindrical side of the reactor shell 1 in example 2, above the perforated plate 53, and the inner cylindrical surface of the slurry inlet and outlet 13 was tangent to the upper surface of the perforated plate 53, and the inner diameter of the slurry inlet and outlet 13 was 100 mm.

Example 3

The slurry bed reactor of example 3 was designed in the same manner as in example 1 except that the heat exchange tube set 3 shown in fig. 1 was not used in the reactor, but a conventional guide shell 7 and serpentine heat exchange tubes 6 were used. The position, diameter and height of the guide shell 7 are the same as those of the guide shell-shaped heat exchange tube set 34 in embodiment 1. The number of the serpentine heat exchange tubes 6 is 1, the height of the serpentine heat exchange tubes is the same as that of the guide cylinder 7, the number of turns is 40.25, and the inner diameter of the serpentine heat exchange tubes is 30 mm.

Comparative example 1

The slurry bed reactor of comparative example 1 was designed in the same manner as in example 1 except that the perforated plate gas distributor 5 described in example 2 above and the conventional guide shell 7 and the serpentine heat exchange tubes 6 described in example 3 above were used.

The applicant characterized the products of all the inventive and comparative examples described above and characterized and analyzed the composition of the product drawn off at the outlet of the reactor using a gas chromatograph model GC-14C, manufactured by shimadzu corporation. In addition, in order to monitor the temperature distribution in the reactor, from the distribution plate, a temperature sensor is arranged in the slurry bed layer in the reactor at intervals of 6 m height adherence, after the reaction is stable, the reading of each temperature sensor is read, and the average value T of all the temperature sensors is taken_{Are all made of}And then obtaining the value of T in the readings of the temperature sensors_{Are all made of}The mean Δ T of the absolute values of all differences was taken as the "mean temperature float absolute value" to rate the heat transfer efficiency within the system.

TABLE 1

As can be seen from the experimental results shown in the above table, the present invention achieved significant improvements in catalytic reaction results and temperature uniformity, respectively, over the existing conventional design by using a specially designed heat exchange tube set and a gas distributor (example 2 and example 3, respectively, compared to comparative example 1); in addition, example 1 of the present invention compared to example 2/example 3 shows that a significant improvement in catalytic reaction results and temperature uniformity can be further achieved if the specially designed heat exchange tube set of the present invention is used together with a gas distributor in a slurry bed reactor.

Claims

1. A helical flow slurry bed reactor, the slurry bed reactor includes the reactor shell, is located the thick liquids import and export of casing bottom, is located the gas outlet at casing top, is located vapour and liquid separator, heat exchange tube set and the gas distributor in the inner space that the casing surrounds, wherein:

2. The spiral flow slurry bed reactor of claim 1 wherein the collection of draft tube heat exchange tubes is generally cylindrical with a cylindrical wall comprising from 3 to 100 draft tube heat exchange tubes, each draft tube heat exchange tube being spirally distributed about a longitudinal central axis of the collection of draft tube heat exchange tubes.

3. The spiral flow slurry bed reactor of claim 1 wherein the collection of draft tube heat exchange tubes has a top heat exchange tube annulus and a bottom heat exchange tube annulus, each draft tube heat exchange tube being in fluid communication with the top heat exchange tube annulus and with the bottom heat exchange tube annulus, respectively.

4. The spiral flow slurry bed reactor of claim 3 wherein the collection of draft tube heat exchange tubes further comprises a plurality of middle heat exchange tube rings, each draft tube heat exchange tube being in fluid communication with a respective one of the middle heat exchange tube rings.

5. The spiral flow slurry bed reactor of claim 1 wherein the collection of heat exchange tubes comprises from 1 to 16 sets of spiral plate shaped heat exchange tubes, each set of spiral plate shaped heat exchange tubes comprising from 2 to 20 spiral plate heat exchange tubes;

at the bottom of the heat exchange tube set, inlets of all heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed on the outer side of the flow guide cylindrical heat exchange tube set along the radial direction of the flow guide cylindrical heat exchange tube set;

at the top of the heat exchange tube set, outlets of all heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed on the outer side of the flow guide cylindrical heat exchange tube set along the radial direction of the flow guide cylindrical heat exchange tube set;

the spiral plate heat exchange tubes in each set of spiral plate-shaped heat exchange tubes spirally rise around the flow guide cylindrical heat exchange tube set in a mutually parallel manner.

6. The spiral flow slurry bed reactor of any one of claims 1 to 5 wherein each draft tube heat exchange tube and each spiral plate heat exchange tube is in fluid communication with the coolant inlet and coolant outlet.

7. The spiral flow slurry bed reactor according to any one of claims 1 to 5, wherein the heat exchange tube set comprises a plurality of coolant inlets and a plurality of coolant outlets, and a plurality of inflow heat exchange tubes and a plurality of outflow heat exchange tubes, each coolant inlet being in communication with a set of spiral plate-shaped heat exchange tube current collectors via one inflow heat exchange tube, and each coolant outlet being in communication with a set of spiral plate-shaped heat exchange tube current collectors via one outflow heat exchange tube.

8. The spiral flow slurry bed reactor according to any one of claims 1 to 5, wherein the spiral plate heat exchange tubes of the set of spiral plate heat exchange tubes have the same or different inner diameters;

the guide shell heat exchange tubes in the guide shell heat exchange tube set have the same or different inner diameters.

9. The spiral flow slurry bed reactor of claim 5,

at the bottom of the heat exchange tube set, inlets of all heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed at the same or different intervals along the radial direction of the flow guide cylindrical heat exchange tube set outside the flow guide cylindrical heat exchange tube set;

and at the top of the heat exchange tube set, outlets of all heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed at the same or different intervals along the radial direction of the flow guide cylindrical heat exchange tube set outside the flow guide cylindrical heat exchange tube set.

10. A method of performing a catalytic reaction, which is a gas-liquid phase reaction or a gas-liquid-solid phase reaction, in a spiral flow slurry bed reactor as claimed in any one of claims 1 to 9.