CN213854448U - Spiral flow slurry bed reactor - Google Patents

Spiral flow slurry bed reactor Download PDF

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Publication number
CN213854448U
CN213854448U CN202022885290.6U CN202022885290U CN213854448U CN 213854448 U CN213854448 U CN 213854448U CN 202022885290 U CN202022885290 U CN 202022885290U CN 213854448 U CN213854448 U CN 213854448U
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heat exchange
exchange tube
spiral
tubes
tube
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王子凡
赵陆海波
唐志永
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Shanghai Ruicheng Carbon Energy Technology Co ltd
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Shanghai Ruicheng Carbon Energy Technology Co ltd
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Abstract

The utility model provides a spiral flow slurry bed reactor, slurry bed reactor includes the reactor casing, and the thick liquids that are located the casing bottom are imported and exported, are located the gas outlet at casing top, are located vapour and liquid separator, heat exchange tube set and the gas distributor in the inner space that the casing surrounds. The utility model discloses a right the structure of heat exchange tube set and/or gas distributor carries out special design, has realized showing improvement of gas-liquid mass transfer and heat transfer effect, has promoted the ft reaction efficiency from this.

Description

Spiral flow slurry bed reactor
Technical Field
The utility model belongs to the chemical industry equipment device field, concretely relates to slurry bed reactor is provided with the structure that can produce the spiral flow among this slurry bed reactor, can guide the gas-liquid fluid in the reactor to take place the efficient inner loop.
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 above-mentioned research results, realized the utility model discloses a technical purpose.
SUMMERY OF THE UTILITY MODEL
According to the utility model discloses a first aspect provides a spiral flow slurry bed reactor, slurry bed reactor includes the reactor casing, is located the thick liquids business turn over 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:
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 the utility model discloses an embodiment, water conservancy diversion cylindric heat exchange tube set totality is the cylinder, and its drum wall includes 3 to 100 water conservancy diversion section of thick bamboo heat exchange tubes, and every water conservancy diversion section of thick bamboo heat exchange tube centers on the vertical axis of water conservancy diversion cylindric heat exchange tube set distributes with the spiral.
According to the utility model discloses a further embodiment, the water conservancy diversion cylindric heat exchange tube set has top heat exchange tube ring and bottom heat exchange tube ring, every water conservancy diversion section of thick bamboo heat exchange tube respectively with top heat exchange tube ring fluid intercommunication, and with bottom heat exchange tube ring fluid intercommunication.
According to the utility model discloses a further embodiment, water conservancy diversion cylindric heat exchange tube set still has many middle part heat exchange tube rings, every water conservancy diversion section of thick bamboo heat exchange tube respectively with middle part heat exchange tube ring fluid intercommunication.
According to the utility model discloses a further embodiment, the heat exchange tube set includes 1 group to 16 groups spiral plate heat exchange tube sets, and every group spiral plate heat exchange tube set includes 2 to 20 spiral plate heat exchange tubes. According to the utility model discloses a further embodiment the bottom of heat exchange tube set, the entry of all heat exchange tubes in same spiral plate shape heat exchange tube set is in the water conservancy diversion cylindric heat exchange tube set outside along the radial distribution of water conservancy diversion cylindric heat exchange tube set. According to the utility model discloses a further embodiment the top of heat exchange tube set, the export of all heat exchange tubes in same spiral plate shape heat exchange tube set is in the water conservancy diversion cylindric heat exchange tube set outside along the radial distribution of water conservancy diversion cylindric heat exchange tube set. According to the utility model discloses a mode that according to the utility model discloses a spiral plate heat exchange tube that every group spiral plate shape heat exchange tube set was concentrated centers on with being parallel to each other the water conservancy diversion cylindric heat exchange tube set spiral rises.
According to another embodiment of the present invention, each draft tube heat exchange tube and each spiral plate heat exchange tube are in fluid communication with the coolant inlet and the coolant outlet.
According to the utility model discloses a further embodiment, the heat exchange tube set includes a plurality of coolant entry and a plurality of coolant export to and many inflow heat exchange tubes and many outflow heat exchange tubes, every coolant entry is through an inflow heat exchange tube and a set of spiral plate-shaped heat exchange tube mass flow intercommunication, and every coolant export is through an outflow heat exchange tube and a set of spiral plate-shaped heat exchange tube mass flow intercommunication.
According to another embodiment of the present invention, the spiral plate heat exchange tubes in which the spiral plate-shaped heat exchange tubes are concentrated have the same or different inner diameters. According to another embodiment of the present invention, the guide shell heat exchange tubes of the guide shell heat exchange tube set have the same or different inner diameters.
According to the utility model discloses a bottom of heat exchange tube set, the entry of all heat exchange tubes in same spiral plate shape heat exchange tube set is in the water conservancy diversion cylindric heat exchange tube set outside along the radial with the same or different interval distribution of water conservancy diversion cylindric heat exchange tube set. According to the utility model discloses a further embodiment the top of heat exchange tube set, the export of all heat exchange tubes in same spiral plate shape heat exchange tube set is in the water conservancy diversion cylindric heat exchange tube set outside along the radial interval distribution with the same or different of water conservancy diversion cylindric heat exchange tube set.
According to the utility model discloses a second aspect provides a spiral flow slurry bed reactor, slurry bed reactor includes the reactor casing, and the thick liquids that are located the casing bottom are imported and exported, are located the gas outlet at casing top, are located vapour and liquid separator, heat exchange tube set and the gas distributor in the inner space that the casing surrounded, 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 present invention, the gas distributor gas distribution pipe is at an included angle of 5 to 60 degrees with respect to the longitudinal axis of the slurry bed reactor. According to another embodiment of the present invention, the gas distributor gas distribution pipe has a component in a cross section perpendicular to the longitudinal axis of the slurry bed reactor and an included angle with the annular pipe of 3 to 45 degrees.
According to another embodiment of the present invention, each set of spiral pipes comprises 2 to 20 spiral pipes, which extend in a clockwise or counterclockwise manner from top to bottom in an equidistant or non-equidistant manner, parallel to each other, so as to fluidly communicate each upper straight pipe with each lower straight pipe.
According to another embodiment of the present invention, the spiral pipes of each set of spiral pipes are straight or curved.
According to another embodiment of the present invention, the gas distributor gas distribution pipe has an inclination angle equal to an inclination angle of the spiral pipe in which the spiral pipe is concentrated.
According to another embodiment of the present invention, the gas distributor gas distribution pipe is uniformly distributed on the lower surfaces of the plurality of annular pipes.
According to another 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.
According to the utility model discloses a further embodiment, a plurality of toroidal tubes are located same plane and set up with the form of concentric circles, and all toroidal tubes all pass through down the straight tube with the spiral pipe current collector intercommunication.
According to another embodiment of the present invention, each spiral pipe of each set of spiral pipes has the same or different inner diameter; 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.
A third aspect of the present invention provides a method for performing 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 reactor of the present invention.
According to a fourth aspect of the present invention there is provided the use of a slurry bed reactor as defined 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 figures show some designs of the invention and prior art.
Fig. 1 shows a slurry bed reactor according to an embodiment of the present invention, wherein the heat exchange tube set and the gas distributor of the present invention are included at the same time.
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, wherein the gas distributor of the heat exchange tube set and the perforated plate structure of the present invention is included.
Fig. 4 shows a slurry bed reactor according to another embodiment of the present invention, which includes a gas distributor and a guide cylinder of solid wall structure and a serpentine heat exchanger around the guide cylinder.
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 application, 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, unless otherwise specified, the term "include" used herein means open or closed. 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 application, when describing the spatial relationship of a particular component or object relative to other components or objects, the terms "inner," "outer," "over," "under," and the like are used herein to refer to the former as being inside, outside, above, or below the latter, either directly in contact with one another or separated by a distance or by a third component or object.
It is emphasized that the embodiments shown in the drawings and described below are merely exemplary embodiments of the invention, which is not intended to limit the scope of the invention. The scope of the present invention is defined by the claims and may include any technical solutions within the scope of the claims, including but not limited to further modifications and substitutions of these specific embodiments.
The uniformity of mass and heat transfer of some preferred slurry bed reactors is characterized hereinafter primarily based on the fischer-tropsch reaction, but it is emphasized here that the utility of the slurry bed reactor of the present invention is not limited to these reactions only, but can be used in any other process that can be implemented in a gas-liquid-solid three-phase system or a gas-liquid two-phase system, and also allows these other processes to gain technological improvements and gains due to 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 includes a reactor housing 1, and sequentially includes a slurry inlet and outlet 13 at the bottom, a gas distributor 4, a heat exchange tube set 3, a separator 2, a partition plate 12, and a gas outlet 11 in the order from the bottom to the top.
According to an 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, in the above reaction process, the liquid materials (e.g. liquid reaction product, liquid solvent, liquid by-product, residual liquid raw material, etc.) in the slurry bed reactor are extracted continuously or intermittently through the slurry inlet and outlet 13 at the bottom of the reactor and optionally one or more openings arranged 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 part, lower part or bottom), and these extracted materials can be subjected to subsequent product recovery and purification, and the by-product 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 present invention, the reactor housing 1 of the slurry bed reactor is used to enclose an inner space surrounding the reactor for carrying out the reaction, and may be a stainless steel housing, for example. In the reactor shown in fig. 1, the shell cross-sectional diameter is substantially constant, but the scope of the invention is not limited thereto, 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 present invention, the reactor has a longitudinal (axial) height of 5-100 meters, such as 10-80 meters, preferably 20-50 meters, more preferably 20-35 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 0.5-10 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 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 from the bottom of the reactor to the liquid level in the reactor is called "gas-slurry mixing zone", in which gas and liquid or slurry are mixed with each other, and the reaction occurs during the circulation back flow. At least the heat exchange tube set and the gas distributor of the utility model are arranged in the area, and the heat exchange tube set and the gas distributor are not arranged below the liquid level completely. 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 flow guide cylindrical heat exchange tube assembly. According to one embodiment of the present invention, as shown in fig. 1, the region between the upper surface of the liquid and the lower surface of the partition 12 is called the "gas-slurry separation zone", in which the gas leaves the liquid/slurry to rise, and during this rise, at least two liquids carried in the gas will fall back into the liquid below, and the main body of the gas-liquid separator 2 is disposed in this region, 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", and 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 in this region, 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 a gas distributor of various types, for example, a perforated plate type gas distributor, which has an upper and a lower two-layer plate, and a hole in the plate, and the gas raw material is introduced from a space between the two-layer plates through a connecting pipe and mixed with the liquid phase in the form of fine bubbles through the hole in the plate; 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 the utility model discloses an embodiment, the straight tube is located within two planes that are parallel to each other respectively with lower straight tube on the gas distributor, and every is gone up the straight tube and every down the straight tube is at the perpendicular to along radial extension in the cross-section of slurry bed reactor axis of ordinates, and go up the straight tube and the radial extending direction of straight tube is different down, and every goes up the straight tube and every down the straight tube via a set of spiral pipe mass flow body intercommunication. 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 coils, preferably of the same shape and structure as each other and 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 looking 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 set 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 section perpendicular to the longitudinal axis of the reactor) and have an included angle of 1 degree to 40 degrees, such as 5 degrees to 35 degrees, 8 degrees to 30 degrees, 10 degrees to 28 degrees, 12 degrees to 25 degrees, 15 degrees to 20 degrees, 16 degrees to 18 degrees, or the included angle may be within a range of values obtained by combining any two of the above values. According to one embodiment of the present invention, all the upper straight tubes 42 have the same length, which is 70-150% of the radius of the cross section (the section perpendicular to the longitudinal axis of the reactor) of the reactor, or 80-120%, or 85-110%, or 90-105%, or 95-102%, or 98-101%, or can be within the range of the numerical value obtained by combining any two of the above numerical values, and when the length of the upper straight tube exceeds the radius of the cross section of the reactor, the portion of the upper straight tube beyond the length of the upper straight tube 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. In accordance with one embodiment of the present 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 (the section perpendicular to the longitudinal axis of the reactor), or can be within the range of any two of the above values combined.
According to one embodiment of the present invention, each set 43 of coils comprises 2 to 20 coils, for example, the number of coils in each set 43 of coils 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 of 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 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 any two of the above values. 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 an 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 spiral pipe 43 is identical to and symmetrical with the other sets of spiral pipe, and the upper straight pipe 42 and the lower straight pipe 44 connected to each set of spiral pipe 43 are also identical to and symmetrical with the other sets of upper straight pipe and lower straight pipe, 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 the gas distributor coil assembly 43, and thus there are 3 gas distributor inlets 41, 3 gas distributor upper straight tubes 42, and 3 gas distributor lower straight tubes 44, respectively. According to an embodiment of the present invention, each set of the gas distributor helix tube sets spirally rises from the lower straight tube to the upper straight tube in a clockwise or counterclockwise manner, and the number of turns of the helix (i.e. the number of turns of the helix completed by the helix header starting from the lower straight tube to the end of the upper straight tube, where the number of turns represents the trajectory of observing the helix vertically downward along the central longitudinal axis of one helix, and the proportion of the trajectory of the observed helix formed on the interface perpendicular to the central longitudinal axis to a complete circle, i.e. a complete helix of one period, expressed in decimal number) may 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 an embodiment of the invention, all lower straight tubes are in the same plane, which is perpendicular to the reactor longitudinal axis, and all upper straight tubes are in the same plane, which is perpendicular to the reactor longitudinal axis. According to an 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 to the total height of the reactor in the longitudinal direction 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 an embodiment of the invention, the ratio of the diameter of the outermost loop to the cross-sectional diameter of the reactor may be 50-99%, alternatively 60-95%, alternatively 70-90%, alternatively 75-85%, alternatively 78-82%, alternatively 70-80%, or may be within the range of any two of the above values taken in combination. According to an 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 5-60%, alternatively 8-55%, alternatively 10-50%, alternatively 12-45%, alternatively 15-40%, alternatively 18-35%, alternatively 20-30%, alternatively 22-25%, or may be within the range of any two of the above values combined. 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 circular tube cross section) or an inner equivalent diameter (in the case of a square, rectangle, oval, or the like tube cross section) after removing 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, 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 of any two of the above values.
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 an embodiment of the present invention, the ratio of the inner diameter of each spiral pipe in the spiral pipe set 43 to the inner diameter of the upper straight pipe 42 is 0.1 to 0.8, or 0.2 to 0.7, or 0.3 to 0.6, or 0.4 to 0.5, or can be within a range of values obtained by combining any two of the above values. 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, or 0.4 to 0.8, or 0.5 to 0.7, or 0.45 to 0.6, 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 of the collars 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 ring pipe 45 to the inner diameter of the upper straight pipe 42 is 0.1 to 0.8, or 0.2 to 0.7, or 0.3 to 0.6, or 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, each of the gas distribution 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, or 0.02 to 0.25, or 0.05 to 0.2, or 0.08 to 0.1, or may be within a range of values obtained by combining any two of the above values.
In a preferred embodiment of the present invention, the positions of each of the coils of the coil set and each of the loops are aligned with each other.
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 present invention, a draft tube may be provided above the gas distributor 4, which draft tube may be formed by a non-porous wall, so that the gas-liquid mixture flows substantially upward outside the draft tube and substantially downward inside the draft tube during the reaction, 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 shell may be disposed 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.
However, according to a preferred embodiment of the present invention, a specially designed heat exchanger tube set 3 of the present invention is provided above the gas distributor. According to a preferred embodiment of the present invention, the heat exchange tube assembly 3 comprises a guide cylindrical heat exchange tube assembly 34 and one or more spiral plate-shaped heat exchange tube assemblies 33, wherein the guide cylindrical heat exchange tube assembly 34 is in fluid communication with the spiral plate-shaped heat exchange tube assembly 33. According to a preferred embodiment of the present invention, the heat exchange tube set 3 is disposed above the gas distributor 4, and is located 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 the utility model discloses a preferred embodiment, heat exchange tube set 3 includes spiral plate-shaped heat exchange tube set 33, water conservancy diversion cylindric heat exchange tube set 34, straight tube 35 on the heat transfer, ring canal 36 on the heat transfer, straight tube 38 under the heat transfer, ring canal 37 under the heat transfer, coolant liquid entry 32 and coolant liquid export 31, perhaps heat exchange tube set 3 comprises spiral plate-shaped heat exchange tube set 33, water conservancy diversion cylindric heat exchange tube set 34, straight tube 35 on the heat transfer, ring canal 36 on the heat transfer, straight tube 38 under the heat transfer, ring canal 37 under the heat transfer, coolant water entry 32 and coolant water export 31.
According to a preferred embodiment of the present invention, the center axis of the heat exchange tube set 3 overlaps with the center 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 an 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 together to obtain a value range. According to a preferred embodiment of the present invention, all of these "draft tube heat exchange tubes" spiral up in a uniform manner along a common cylindrical contour, thereby collectively constituting a cylindrical structure, which resembles a conventional draft tube, and thus the overall combination of these 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 in parallel with one another along the cylindrical contour of the outer periphery of the bank 34, 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 shown in fig. 1 of the present invention, each draft tube heat exchange tube extends spirally in a counterclockwise manner, and the spiral period of each draft tube heat exchange tube is 1. According to a preferred embodiment of the present invention, the upper and lower ends of all draft tube heat exchange tubes are connected to the heat exchange upper loop 36 (also referred to as top heat exchange tube ring, herein, the heat exchange upper loop and the top heat exchange tube ring can be used interchangeably) and the heat exchange lower loop 37 (also referred to as bottom heat exchange tube ring, herein, the heat exchange lower loop and the bottom heat exchange tube ring can be used interchangeably), and are respectively in fluid communication with the heat exchange upper loop 36 and the heat exchange lower loop 37. According to the utility model discloses an embodiment, except above-mentioned top and bottom heat transfer pipe ring, can optionally be in the not co-altitude department of water conservancy diversion cylindric heat exchange tube set sets up one or more middle part heat transfer pipe rings, every water conservancy diversion section of thick bamboo heat exchange tube respectively with middle part heat transfer pipe ring fluid intercommunication. 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 groups, for example, 2 to 15 groups, or 3 to 12 groups, or 3 to 9 groups, or 3 to 6 groups of spiral plate-shaped heat exchange tube sets are arranged in a centrosymmetric manner around the middle guide cylindrical heat exchange tube set, and each group of spiral plate-shaped heat exchange tube sets comprises 2 to 20, for example, 3 to 18, or 3 to 15, or 3 to 12, or 3 to 9, or 4 to 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 the heat exchange tubes in the same spiral plate-shaped heat exchange tube set are distributed along the radial direction of the guide flow cylindrical heat exchange tube set outside the guide flow 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 the upper straight tube 35 of each heat exchange has a coolant outlet 31, and the outer end of the lower straight tube 38 of each heat exchange has a coolant inlet 32. In 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 plurality of sets of spiral plate heat exchange tubes is 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 of the present invention, the number of turns of the spiral of each spiral plate heat exchange tube in each set of spiral plate heat exchange tubes (i.e. the number of turns of the spiral completed from the lower straight tube 38 to the end of the upper straight tube 35, where the number of turns represents the trace of the spiral observed vertically downward along the central longitudinal axis of the spiral, and the ratio of the trace of the observed spiral formed on the interface perpendicular to the central longitudinal axis to the complete circle, i.e. the complete spiral of one period, is expressed by a decimal number) may 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 a numerical range obtained by combining any two of the above end values. According to the preferred embodiment of the present invention as shown in fig. 1, each spiral plate heat exchange tube extends spirally upward in a counterclockwise manner with a spiral period of 1.
According to an embodiment of the present 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 to the total height of the reactor in the longitudinal direction is 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 values. According to an embodiment of the present invention, the heat exchange lower loop 37 and the heat exchange upper loop 36 are aligned with each other and have the same size, and the ratio of the diameter of the heat exchange lower loop 37 and the heat exchange upper loop 36 (i.e. the diameter of the cross section of the flow guide tube-shaped heat exchange tube set 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 a range of values obtained by combining any two of the above values.
According to an embodiment of the present invention, the aspect ratio (length to inner diameter) of the heat exchange upper straight pipe 35 and the heat exchange lower straight pipe 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 of 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 1-30 mm, such as 2-25 mm, or 3-22 mm, or 5-20 mm, or 8-18 mm, or 10-15 mm, or 12-14 mm, or may be within a range of any two of the above values.
According to one embodiment of the present invention, the heat exchange upper loop 36 and the heat exchange lower loop 37 have identical dimensions and shapes. According to an embodiment of the present 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 obtained by combining any two of the above values.
According to one embodiment of the present invention, each of the spiral tubes in the flow guide cylindrical heat exchange tube assembly 34 has the same inner diameter as each other. According to an embodiment of the present invention, the ratio of the inner diameter of each spiral tube in the flow guiding cylindrical heat exchange tube set 34 to the inner diameter of the heat exchange upper ring tube 36 is 0.1 to 0.8, or 0.2 to 0.7, or 0.3 to 0.6, or 0.4 to 0.5, or can be within a range of values obtained by combining any two of the above values. According to an embodiment of the present invention, the ratio of the inner diameter of each heat exchange tube in the spiral plate-shaped heat exchange tube set 33 to the inner diameter of the heat exchange upper ring tube 36 is 0.1 to 0.8, or 0.2 to 0.7, or 0.3 to 0.6, or 0.4 to 0.5, or can be within a range of values obtained by combining any two of the above 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 of the invention comprises 1-20, preferably 1-10, separation devices, which are evenly distributed 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 devices may be additionally added to the slurry bed reactor as required, 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 devices by the preferred design of the distribution plate.
According to a preferred embodiment of the present invention, the reactor of the present invention is shown in fig. 1 and 2 and 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 at will, and such combinations are also included in the present general inventive concept.
Examples
The preferred embodiments of the present invention are specifically illustrated 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 503 standard feed gases comprising 49% by volume of hydrogen, 49% by volume of CO and 2% by volume of nitrogen are fed into the reactor per hour. 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 is directed towards the reactor shell at the slurry surfaceThe body moves laterally and descends along the housing back to the distributor plate to repeat the slurry bed reaction process described above, and the liquid and solids recovered at the cyclone are returned to the level of the slurry bed via the feed leg of the cyclone, also moving laterally towards the reactor housing, and descend along the housing back to the distributor plate to repeat the slurry bed reaction process described above.
The different designs of the comparative examples and embodiments of the present 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 above practical examples and comparative examples, and characterized and analyzed the composition of the product drawn out of the reactor outlet by means of 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 takenAre all made ofAnd then obtaining the value of T in the readings of the temperature sensorsAre all made ofThe 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
Figure BDA0002818899690000231
As can be seen from the experimental results shown in the above table, the present invention, by using the specially designed heat exchange tube set and the gas distributor, respectively achieves significant improvements in catalytic reaction results and temperature uniformity, compared to the conventional design (example 2 and example 3 are respectively compared to comparative example 1); additionally, embodiment 1 of the utility model compares with embodiment 2/embodiment 3 and shows, if adopt simultaneously among the slurry bed reactor the utility model discloses specially designed's heat exchange tube set and gas distributor, catalytic reaction result and temperature homogeneity can further realize showing the improvement.

Claims (9)

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:
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.
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.
CN202022885290.6U 2020-12-04 2020-12-04 Spiral flow slurry bed reactor Active CN213854448U (en)

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