CN112304145A - Heat exchange tube, heat exchange device and gas-solid-liquid three-phase reactor - Google Patents
Heat exchange tube, heat exchange device and gas-solid-liquid three-phase reactor Download PDFInfo
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- CN112304145A CN112304145A CN201910712975.XA CN201910712975A CN112304145A CN 112304145 A CN112304145 A CN 112304145A CN 201910712975 A CN201910712975 A CN 201910712975A CN 112304145 A CN112304145 A CN 112304145A
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- heat exchange
- exchange tube
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
- F28F1/12—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
- F28F1/14—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element and extending longitudinally
- F28F1/20—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element and extending longitudinally the means being attachable to the element
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/10—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically
- F28D7/103—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically consisting of more than two coaxial conduits or modules of more than two coaxial conduits
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
Abstract
The invention relates to the technical field of chemical equipment, and discloses a heat exchange tube, a heat exchange device and a gas-solid-liquid three-phase reactor, wherein the heat exchange tube (1) is provided with an inlet and an outlet for respectively allowing a heat exchange medium to enter and discharge, the heat exchange tube (1) comprises a heat exchange tube body (10), and the outer wall surface of the heat exchange tube body (10) is provided with a concave-convex structure. The heat exchange tube has a large heat transfer area and can occupy a small volume in the reactor when being applied to the reactor. The heat exchange tube is applied to the heat exchange device, so that the total volume of the heat exchange device is smaller. The heat exchange tube is applied to the gas-solid-liquid three-phase reactor, so that the effective volume in the reactor can be increased.
Description
Technical Field
The invention relates to the technical field of chemical equipment, in particular to a heat exchange tube, a heat exchange device and a gas-solid-liquid three-phase reactor.
Background
Fischer-Tropsch synthesis (also called Fischer-Tropsch synthesis) is a process of synthesizing liquid hydrocarbons or hydrocarbons from synthesis gas (a mixed gas of carbon monoxide and hydrogen) as a raw material in the presence of a catalyst and under appropriate conditions. Currently, the slurry reactor of gas-liquid-solid three phases is a mainstream reactor of low-temperature Fischer-Tropsch synthesis technology.
Can emit a large amount of heats among the ft synthesis process, if can not in time shift out the reactor with these heats, very easily cause the temperature of reactor bed to rise fast for reactor bed temperature out of control and influence the going on of reaction, consequently, set up heat transfer device in the reactor usually and be used for in time removing the heat. At present, the heat exchange devices arranged in the reactor basically adopt common heat exchange tubes, coils or jacketed pipes as heat exchange elements.
In order to increase the heat transfer efficiency of the heat exchange device, the number of heat exchange tubes or the length of the heat exchange tubes is mainly increased, but the effective volume in the slurry reactor is reduced, and the fluid mechanical state of the reactor can be adversely affected.
Disclosure of Invention
The invention aims to solve the problems of low heat exchange efficiency and small effective volume in a reactor in the prior art, and provides a heat exchange tube which has a large heat transfer area and can occupy small volume in the reactor when being applied to the reactor.
In order to achieve the above object, in one aspect, the present invention provides a heat exchange tube having an inlet and an outlet for allowing a heat exchange medium to enter and discharge, respectively, the heat exchange tube including a heat exchange tube body, an outer wall surface of the heat exchange tube body being provided with a concave-convex structure.
In the technical scheme, the concave-convex structure is arranged on the outer wall surface of the heat exchange tube body, so that the heat exchange tube has a larger heat exchange area, and therefore when the heat exchange device comprising the tube bundle formed by arranging a plurality of heat exchange tubes is applied to the gas-solid-liquid three-phase reactor, the number of the heat exchange tubes can be reduced under the condition of certain heat exchange efficiency, and the effective volume of the gas-solid-liquid three-phase reactor is correspondingly increased. In addition, compared with a heat exchange tube with a smooth outer wall surface, the heat exchange tube with the concave-convex structure can effectively reduce the thickness of a retained inner layer during heat transfer, so that the heat transfer coefficient of the heat exchange tube is improved.
Preferably, the concave-convex structure comprises a groove arranged on the outer wall surface of the heat exchange tube body.
Preferably, the groove wall surface of the groove is arc surface-shaped; and/or
And the groove top of the groove is in arc transition connection with the outer wall surface of the heat exchange tube body.
Preferably, an included angle formed between a tangent plane passing through the groove top of the groove and a straight connecting plane connecting the lowest point of the groove bottom of the groove and the highest point of the groove top of the groove is 30-55 degrees.
Preferably, a plurality of grooves are formed in the outer wall surface of the heat exchange tube body, and the grooves are arranged along the circumferential direction of the heat exchange tube body.
Preferably, a plurality of grooves are uniformly distributed along the circumferential direction of the heat exchange tube body; and/or the number of the grooves is 15-30.
Preferably, the groove extends in an extending direction of the heat exchange tube body.
Preferably, the heat exchange tube body is a straight tube or U-shaped, wherein an inlet and an outlet for the heat exchange medium to enter and discharge are formed at two ends of the heat exchange tube body respectively.
Preferably, the heat exchange tube comprises an inner tube arranged in the heat exchange tube body, and an annular gap for flowing out of a heat exchange medium introduced from the inner tube is formed between the heat exchange tube body and the inner tube.
A second aspect of the invention provides a heat exchange apparatus comprising a tube bundle formed by an arrangement of a plurality of heat exchange tubes as provided herein. Because the heat exchange tubes provided by the invention are arranged in the heat exchange device, the number of the heat exchange tubes can be reduced under the condition of certain heat exchange efficiency, so that the total volume of the heat exchange device is smaller, and the effective volume in a reactor can be increased when the heat exchange device is applied to the reactor such as a slurry reactor.
Preferably, the tube bundle comprises a plurality of array units, and each array unit comprises four heat exchange tubes arranged in a square shape or three heat exchange tubes arranged in a regular triangle shape.
In a third aspect of the present invention, the gas-solid-liquid three-phase reactor includes a reaction shell and a heat exchange unit disposed in the reaction shell, where the heat exchange unit includes a heat exchange device located at least one of a top layer, a middle layer and a bottom layer of the gas-solid-liquid three-phase reactor, and the heat exchange device is the heat exchange device provided by the present invention. The heat exchange device provided by the invention is arranged in the gas-solid-liquid three-phase reactor, and the heat exchange device has smaller volume under the condition of certain heat exchange efficiency, so that the effective volume in the reactor can be improved.
Drawings
Fig. 1 shows a schematic perspective view of a heat exchange tube according to a preferred embodiment of the present invention;
FIG. 2 shows a schematic top view of the heat exchange tube of FIG. 1;
fig. 3 is a schematic top view showing a heat exchange tube according to a preferred embodiment of the present invention, wherein a groove is formed on an outer wall surface of a body of the heat exchange tube;
fig. 4 is a schematic perspective view showing a heat exchange tube according to another preferred embodiment of the present invention;
fig. 5 is a schematic view showing the overall structure of a heat exchange tube according to another preferred embodiment of the present invention, in which the concavo-convex structure is not shown;
fig. 6 is a schematic view showing the overall structure of a heat exchange tube according to another preferred embodiment of the present invention, in which the concavo-convex structure is not shown;
FIG. 7 is a schematic sectional view showing an applied state of a heat exchange device according to a preferred embodiment of the present invention;
FIG. 8 is a schematic sectional view showing an applied state of a heat exchange device according to another preferred embodiment of the present invention;
FIG. 9 is a schematic view showing the overall structure of a heat exchange apparatus according to a preferred embodiment of the present invention;
FIG. 10 is a schematic view showing the overall configuration of the state of use of a gas-solid-liquid three-phase reactor according to a preferred embodiment of the present invention.
Description of the reference numerals
1-heat exchange tube; 10-a heat exchange tube body; 11-a water outlet main pipe; 12-a groove; 13-a branch pipe; 14-an inner tube; 16-an annular gap; 18-a water inlet main pipe; 2-gas-solid-liquid three-phase reactor; 20-a reaction shell; 3 a-a first drum; 3 b-a second drum; 3 c-a third drum; 4-a heat exchange device; 5 a-a first circulation pump; 5 b-a second circulation pump; 5 c-third circulation pump.
Detailed Description
In the present invention, the use of directional terms such as "upper, lower, left and right" in the absence of a contrary intention, generally means that the terms "inside and outside" refer to the inside and outside of the outline of the component, both in conjunction with the orientation shown in the drawings and the orientation in actual use.
The invention provides a heat exchange tube, wherein a heat exchange tube 1 is provided with an inlet and an outlet for respectively allowing a heat exchange medium to enter and discharge, the heat exchange tube 1 comprises a heat exchange tube body 10, and the outer wall surface of the heat exchange tube body 10 is provided with a concave-convex structure. Through setting up concave-convex structure at the outer wall of heat exchange tube body 10 to make heat exchange tube 1 have bigger heat transfer area, like this, when will include the heat transfer device who arranges the tube bank that forms by a plurality of heat exchange tubes 1 and use gas-solid-liquid three-phase reactor in, under the certain circumstances of heat exchange efficiency, reducible heat exchange tube 1's quantity, corresponding improvement gas-solid-liquid three-phase reactor's effective volume from this. It can be understood that when the heat exchange tube 1 is applied to a gas-solid-liquid three-phase reactor, pressurized saturated water can be introduced into the inlet of the heat exchange tube 1, and the pressurized saturated water absorbs heat through the heat exchange tube body 10 to become a gas-liquid mixture which is discharged from the outlet. In addition, compared with a heat exchange tube with a smooth outer wall surface, the heat exchange tube 1 with the concave-convex structure can effectively reduce the thickness of a retained inner layer during heat transfer, so that the heat transfer coefficient of the heat exchange tube 1 is improved.
It should be noted that the heat exchange tube 1 may be in the form of a single tube, for example, as shown in fig. 1, the heat exchange tube body 10 may be a straight tube, or as shown in fig. 5, may be U-shaped, wherein both ends of the heat exchange tube body 10 are respectively formed to be open, wherein one end is the inlet for the heat exchange medium to enter, and the other end is the outlet for the heat exchange medium to exit.
In addition, the heat exchange tube 1 may be in the form of a sleeve, and as shown in fig. 4 and 6, the heat exchange tube 1 may include an inner tube 14 disposed inside a heat exchange tube body 10, and an annular gap 16 through which a heat exchange medium introduced from the inner tube 14 flows out is formed between the heat exchange tube body 10 and the inner tube 14, that is, an inlet port and an outlet port may be opened in the inner tube 14, and the heat exchange medium may be introduced through the inlet port of the inner tube 14 and then discharged through the outlet port of the inner tube 14, after which the heat exchange medium flows through the annular gap 16 and flows out of the heat exchange tube body. As shown in fig. 6, a plurality of branch pipes 13, for example, 2, 3, 4, 5, 6, may be provided on the heat exchange tube body 10, and the branch pipes 13 may be connected to the annular gap 16 at both ends thereof, so that the heat exchange medium discharged from the discharge port of the inner tube 14 may also flow through the branch pipes 13 and then join the annular gap 16.
The concave-convex structure may be in various forms as long as a convex surface or a concave surface is provided on the outer wall surface of the heat exchange tube body 10. Preferably, as shown in fig. 1 and 2, the concavo-convex structure may include a groove 12 opened on an outer wall surface of the heat exchange tube body 10. Wherein, the groove 12 can extend along the extending direction of the heat exchange tube body 10 to further increase the heat transfer area of the heat exchange tube 1, it can be understood that, when the heat exchange tube 1 is a single straight tube, the groove 12 extends along the axial direction of the heat exchange tube 1, and when the heat exchange tube 1 is U-shaped, the groove 12 can also be U-shaped. Further, when the projection is provided, the surface of the projection may preferably be arcuate.
In order to further increase the heat transfer area and improve the heat exchange coefficient, a plurality of grooves 12 may be formed in the outer wall surface of the heat exchange tube body 10, the plurality of grooves 12 are arranged along the circumferential direction of the heat exchange tube body 10, and preferably, the plurality of grooves 12 may be uniformly distributed along the circumferential direction of the heat exchange tube body 10.
The groove wall surface of the groove 12 may be formed in an arc surface shape, so that abrasion of materials such as a catalyst in the reactor can be reduced, and the arc surface shape also increases a turbulent motion state of a fluid flowing through the outer wall surface of the heat exchange tube body 10. In addition, the groove top of the groove 12 and the outer wall surface of the heat exchange tube body 10 can be in transition connection in a circular arc shape, so that the abrasion to materials such as a catalyst in the reactor is further reduced. It can be understood that when a plurality of grooves 12 are formed on the outer wall surface of the heat exchange tube body 10, the convex surface of the convex portion between the adjacent grooves 12 is preferably arc-shaped, so that abrasion of materials such as catalyst can be reduced.
When the plurality of grooves 12 are formed in the outer wall surface of the heat exchange tube body 10, the number of the grooves 12 is not particularly limited, and can be set according to actual requirements. Particularly, the number of the grooves 12 is preferably 15 to 30, so that the heat transfer area of the heat exchange tube 1 can be increased, and the preparation convenience can be realized, that is, the cambered surfaces of the grooves 12 can be easily prepared on the premise of ensuring the heat transfer area of the heat exchange tube 1.
As shown in fig. 3, an included angle β formed between the tangent plane passing through the groove top of the groove 12 and the straight plane connecting the lowest point of the groove bottom of the groove 12 and the highest point of the groove top of the groove 12 is 30 to 55 °, and the β angle is set within the above-mentioned angle range, not only the heat transfer area of the heat exchange tube 1 is further increased and the heat transfer system thereof is improved, but also the heat exchange tube 1 is easy to manufacture and has suitable strength.
The invention also provides a heat exchange device, and the heat exchange device 4 comprises a tube bundle formed by arranging a plurality of heat exchange tubes 1 provided by the invention. Because the heat exchange tubes 1 provided by the invention are arranged in the heat exchange device 4, the number of the heat exchange tubes 1 can be reduced under the condition of certain heat exchange efficiency, so that the total volume of the heat exchange device is smaller, and the effective volume in a reactor can be increased when the heat exchange device is applied to the reactor such as a slurry reactor. It should be noted that, as shown in fig. 9, the heat exchange device 4 may include a water inlet main pipe 18 and a water outlet main pipe 11, water inlet holes respectively communicated with inlets of the plurality of heat exchange pipes 1 may be formed in the water inlet main pipe 18 to introduce the heat exchange medium into the corresponding heat exchange pipes 1, respectively, and water outlet holes respectively communicated with outlets of the plurality of heat exchange pipes 1 may be formed in the water outlet main pipe 11 to lead the heat exchange medium out of each heat exchange pipe 1.
The heat exchange tubes 1 may be arranged in a regular manner, and as shown in connection with fig. 7 and 8, the tube bundle may comprise a plurality of arrayed cells. As shown in fig. 7, each array unit may include four heat exchange tubes 1 in a square arrangement; as shown in fig. 8, each array unit may include three heat exchange tubes 1 arranged in a regular triangle. When the heat exchange tube 1 provided by the present invention is applied to a heat exchange device, it is preferable that each array unit includes four heat exchange tubes 1 arranged in a square shape to increase the effective volume of the reactor.
The invention also provides a gas-solid-liquid three-phase reactor, wherein the gas-solid-liquid three-phase reactor 2 comprises a reaction shell 20 and a heat exchange unit arranged in the reaction shell 20, the heat exchange unit comprises a heat exchange device 4 positioned on at least one of a top layer, a middle layer and a bottom layer of the gas-solid-liquid three-phase reactor 2, and the heat exchange device 4 is the heat exchange device 4 provided by the invention. Because the heat exchange device 4 provided by the invention is arranged in the gas-solid-liquid three-phase reactor 2, the heat exchange device has smaller volume under the condition of certain heat exchange efficiency, thereby being capable of improving the effective volume in the reactor. Wherein the gas-solid-liquid three-phase reactor can be a slurry reactor.
The inventor researches and discovers that when the heat exchange device comprising the tube bundle formed by arranging the plurality of heat exchange tubes with smooth outer wall surfaces is applied to a gas-solid-liquid three-phase reactor such as a slurry reactor, the lumped heat transfer coefficient is 1000W/m2K, the heat exchange tube with smooth outer wall surface is replaced by the heat exchange tube 1 with the concave-convex structure, and the lumped heat transfer coefficient can reach 1200-1600W/m2·K。
As shown in fig. 10, a steam drum may be provided outside the gas-solid-liquid three-phase reactor to separate a liquid-liquid mixture discharged from the outlet of the heat exchange tube 1, and in addition, a circulation pump may be provided outside the gas-solid-liquid three-phase reactor to pump saturated water into the inlet of the heat exchange tube 1. Specifically, when the heat exchange devices 4 are arranged on the top layer, the middle layer and the bottom layer of the gas-solid-liquid three-phase reactor, a first steam drum 3a, a second steam drum 3b and a third steam drum 3c corresponding to the three heat exchange devices 4 respectively and a first circulating pump 5a, a second circulating pump 5b and a third circulating pump 5c corresponding to the three heat exchange devices 4 respectively can be arranged.
The effects of the present invention will be further described with reference to examples.
Examples
Example 1
The heat exchange device 4 provided by the invention is applied to a slurry reactor.
The inner diameter of a reaction shell 20 of the slurry bed reactor is 5.0m, the height of the reaction shell 20 is 35m, the treatment capacity of the synthesis gas is 15 ten thousand Nm3/h, the operating pressure is 3.0MPa, the temperature is 250 ℃, the oil yield is 16 ten thousand tons/year, and the liquid level of the reactor is controlled to be 25 m.
The bottom layer and the top layer of the slurry reactor are provided with heat exchanger devices 4, wherein the array units in the tube bundle comprise four heat exchange tubes 1 which are arranged in a square shape, each heat exchange tube 1 is a single straight tube, the outer wall surface of each heat exchange tube 1 is provided with 20 grooves 12, the grooves 12 are uniformly distributed along the circumferential direction of the heat exchange tube body 10, the groove wall surface of each groove 12 is arc-surface-shaped, the groove top of each groove 12 is in arc transition connection with the outer wall surface of the heat exchange tube body 10, the included angle formed by the tangent plane passing through the groove top of each groove 12 and the connecting straight plane connecting the lowest point of the groove bottom of the groove 12 and the highest point of the groove top of the groove 12 is 30 degrees, and each groove 12 extends along the.
Two steam drums corresponding to the heat exchanger device 4 at the bottom layer and the heat exchanger device 4 at the top layer are respectively arranged outside the slurry reactor.
As can be known from thermocouple measurement axially arranged on a reaction shell of the slurry reactor, in the running process of the slurry reactor, the axial temperature difference of a slurry bed layer is within +/-2 ℃, the temperature and the pressure of a heat exchange steam drum of the whole system are stable, and the heat exchange system can meet the operation requirement of the slurry bed Fischer-Tropsch synthesis reactor.
In addition, if the heat exchange tubes 1 are replaced by ordinary heat exchange tubes in the form of single straight tubes with smooth outer wall surfaces, it is found that the number of the ordinary heat exchange tubes needs to be increased by 10% under the condition of ensuring that the heat exchange efficiency is not changed, so that the effective volume of the reactor body is reduced by 15%.
Example 2
The heat exchange device 4 provided by the invention is applied to a slurry reactor.
The inner diameter of a reaction shell 20 of the slurry bed reactor is 10m, the height of the reaction shell 20 is 60m, the treatment capacity of the synthetic gas is 40 ten thousand Nm3/h, the operating pressure is 3.0MPa, the temperature is 270 ℃, and the oil yield is 65 ten thousand tons per year.
The bottom layer, the middle layer and the top layer of the slurry reactor are respectively provided with a heat exchanger device 4, the array units in the tube bundle comprise four heat exchange tubes 1 which are arranged in a square shape, the heat exchange tubes 1 are U-shaped tubes, the outer wall surfaces of the heat exchange tubes 1 are provided with 30 grooves 12, the grooves 12 are uniformly distributed along the circumferential direction of the heat exchange tube body 10, the groove wall surface of each groove 12 is arc-surface-shaped, the groove top of each groove 12 is in arc transition connection with the outer wall surface of the heat exchange tube body 10, the included angle formed by the tangent plane passing through the groove top of each groove 12 and the connecting straight plane connecting the lowest point of the groove bottom of each groove 12 and the highest point of the groove top of each groove 12 is 40 degrees, and each groove 12 extends.
Three steam drums corresponding to the heat exchanger device 4 at the bottom layer, the heat exchanger device 4 at the middle layer and the heat exchanger device 4 at the top layer are respectively arranged outside the slurry reactor.
Relevant tests show that in the operation process of the slurry reactor, the axial temperature difference of a slurry bed layer is within +/-3 ℃, the axial temperature difference of the reactor is controlled within 3 ℃, the temperature and the pressure of a steam drum of the whole system are stable, and the heat exchange system can meet the operation requirements of the slurry bed Fischer-Tropsch synthesis reactor.
In addition, if the heat exchange tubes 1 are replaced by U-shaped common heat exchange tubes with smooth outer wall surfaces, it is found that the number of the common heat exchange tubes needs to be increased by 15% under the condition of ensuring that the heat exchange efficiency is not changed, and meanwhile, the increased heat exchange tubes need to be matched with supporting pieces, collecting tubes and the like, so that the effective volume of the reactor body is reduced by 20%.
The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, numerous simple modifications can be made to the technical solution of the invention, including combinations of the individual specific technical features in any suitable way. The invention is not described in detail in order to avoid unnecessary repetition. Such simple modifications and combinations should be considered within the scope of the present disclosure as well.
Claims (12)
1. The heat exchange tube is characterized in that the heat exchange tube (1) is provided with an inlet and an outlet for respectively allowing a heat exchange medium to enter and discharge, the heat exchange tube (1) comprises a heat exchange tube body (10), and the outer wall surface of the heat exchange tube body (10) is provided with a concave-convex structure.
2. A heat exchange tube according to claim 1, wherein the concavo-convex structure comprises a groove (12) opened in an outer wall surface of the tube body (10).
3. The heat exchange tube according to claim 2, characterized in that the groove wall surface of the groove (12) is arc surface shaped; and/or
The groove top of the groove (12) is in arc transition connection with the outer wall surface of the heat exchange tube body (10).
4. A heat exchange tube according to claim 3, characterized in that the angle formed between a tangent plane passing through the groove top of the groove (12) and a straight connecting plane connecting the lowest point of the groove bottom of the groove (12) and the highest point of the groove top of the groove (12) is 30-55 °.
5. A heat exchange tube according to claim 2, wherein the outer wall surface of the tube body (10) is provided with a plurality of grooves (12), and the plurality of grooves (12) are arranged along the circumferential direction of the tube body (10).
6. A heat exchange tube according to claim 5, wherein a plurality of the grooves (12) are uniformly distributed along the circumferential direction of the tube body (10); and/or the number of the grooves (12) is 15-30.
7. A heat exchange tube according to claim 2, wherein the groove (12) extends in the extending direction of the tube body (10).
8. A heat exchange tube according to any one of claims 1 to 7, wherein the heat exchange tube body (10) is a straight tube or a U-shaped tube, wherein both ends of the heat exchange tube body (10) form an inlet and an outlet for the inlet and the outlet of a heat exchange medium, respectively.
9. A heat exchange tube according to any one of claims 1 to 7, characterised in that the heat exchange tube (1) comprises an inner tube (14) disposed inside the tube body (10), an annular gap (16) being formed between the tube body (10) and the inner tube (14) for the outflow of a heat exchange medium introduced by the inner tube (14).
10. A heat exchange device, characterized in that the heat exchange device (4) comprises a tube bundle formed by an arrangement of a plurality of heat exchange tubes (1) according to any one of claims 1 to 9.
11. The heat exchange device according to claim 10, wherein the tube bundle comprises a plurality of array units, each array unit comprising four heat exchange tubes (1) in a square arrangement or three heat exchange tubes (1) in a regular triangular arrangement.
12. A gas-solid-liquid three-phase reactor, characterized in that the gas-solid-liquid three-phase reactor (2) comprises a reaction shell (20) and a heat exchange unit arranged in the reaction shell (20), the heat exchange unit comprises a heat exchange device (4) positioned at least one of a top layer, a middle layer and a bottom layer of the gas-solid-liquid three-phase reactor (2), wherein the heat exchange device (4) is the heat exchange device (4) of claim 10 or 11.
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| CN201910712975.XA CN112304145A (en) | 2019-08-02 | 2019-08-02 | Heat exchange tube, heat exchange device and gas-solid-liquid three-phase reactor |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB878916A (en) * | 1958-04-25 | 1961-10-04 | Andre Huet | Improvements in heat exchanger tubes |
| GB2083603A (en) * | 1980-09-12 | 1982-03-24 | Feist Artus | A pipe made from flexible or rigid plastics material, for conveying heat transfer fluids |
| CN201053840Y (en) * | 2007-06-28 | 2008-04-30 | 北京广厦新源石化设备开发有限公司 | Vertical flute reinforced heat-exchanging pipe |
| JP2015094502A (en) * | 2013-11-11 | 2015-05-18 | 株式会社 テスク資材販売 | Radiator and air conditioning system using the same |
| CN205279833U (en) * | 2015-12-22 | 2016-06-01 | 上海交通大学 | Condensation heat exchange tube |
| CN107790072A (en) * | 2016-09-05 | 2018-03-13 | 神华集团有限责任公司 | The method of Fischer-Tropsch slurry reactor system and Fischer-Tropsch synthesis |
| CN108854867A (en) * | 2018-09-19 | 2018-11-23 | 上海兖矿能源科技研发有限公司 | A kind of heat transfer system for Fischer-Tropsch synthesis device |
-
2019
- 2019-08-02 CN CN201910712975.XA patent/CN112304145A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB878916A (en) * | 1958-04-25 | 1961-10-04 | Andre Huet | Improvements in heat exchanger tubes |
| GB2083603A (en) * | 1980-09-12 | 1982-03-24 | Feist Artus | A pipe made from flexible or rigid plastics material, for conveying heat transfer fluids |
| CN201053840Y (en) * | 2007-06-28 | 2008-04-30 | 北京广厦新源石化设备开发有限公司 | Vertical flute reinforced heat-exchanging pipe |
| JP2015094502A (en) * | 2013-11-11 | 2015-05-18 | 株式会社 テスク資材販売 | Radiator and air conditioning system using the same |
| CN205279833U (en) * | 2015-12-22 | 2016-06-01 | 上海交通大学 | Condensation heat exchange tube |
| CN107790072A (en) * | 2016-09-05 | 2018-03-13 | 神华集团有限责任公司 | The method of Fischer-Tropsch slurry reactor system and Fischer-Tropsch synthesis |
| CN108854867A (en) * | 2018-09-19 | 2018-11-23 | 上海兖矿能源科技研发有限公司 | A kind of heat transfer system for Fischer-Tropsch synthesis device |
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