CN203916623U - Heat exchange reactor - Google Patents
Heat exchange reactor Download PDFInfo
- Publication number
- CN203916623U CN203916623U CN201290000642.6U CN201290000642U CN203916623U CN 203916623 U CN203916623 U CN 203916623U CN 201290000642 U CN201290000642 U CN 201290000642U CN 203916623 U CN203916623 U CN 203916623U
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- China
- Prior art keywords
- tube head
- transfer pipes
- fluid chamber
- fluid
- heat exchange
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000012530 fluid Substances 0.000 claims abstract description 188
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 239000003054 catalyst Substances 0.000 claims description 44
- 235000012489 doughnuts Nutrition 0.000 claims description 15
- 238000012856 packing Methods 0.000 claims description 12
- 125000006850 spacer group Chemical group 0.000 claims description 12
- 238000002955 isolation Methods 0.000 claims description 10
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 238000000034 method Methods 0.000 description 16
- 239000000919 ceramic Substances 0.000 description 9
- 239000000463 material Substances 0.000 description 9
- 239000000835 fiber Substances 0.000 description 8
- 239000011949 solid catalyst Substances 0.000 description 5
- 238000006555 catalytic reaction Methods 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- 238000009413 insulation Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000002349 favourable effect Effects 0.000 description 3
- 210000004907 gland Anatomy 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910001026 inconel Inorganic materials 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- 238000003466 welding Methods 0.000 description 3
- 238000005538 encapsulation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000006057 reforming reaction Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 206010058109 Hangnail Diseases 0.000 description 1
- 241000237983 Trochidae Species 0.000 description 1
- BGJLJGFTMKGXFG-UHFFFAOYSA-N [Ni].[W].[Cr].[Co].[Na] Chemical compound [Ni].[W].[Cr].[Co].[Na] BGJLJGFTMKGXFG-UHFFFAOYSA-N 0.000 description 1
- 238000002453 autothermal reforming Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000008393 encapsulating agent Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910001119 inconels 625 Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910001120 nichrome Inorganic materials 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Classifications
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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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
- B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
-
- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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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
- F28D7/16—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 in parallel spaced relation
- F28D7/163—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 in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing
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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
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/02—Header boxes; End plates
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/02—Header boxes; End plates
- F28F9/04—Arrangements for sealing elements into header boxes or end plates
- F28F9/06—Arrangements for sealing elements into header boxes or end plates by dismountable joints
- F28F9/10—Arrangements for sealing elements into header boxes or end plates by dismountable joints by screw-type connections, e.g. gland
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/22—Arrangements for directing heat-exchange media into successive compartments, e.g. arrangements of guide plates
-
- 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
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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
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
- B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
-
- 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
- B01J2208/00477—Controlling the temperature by thermal insulation means
- B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
-
- 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
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
-
- 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
- B01J2208/06—Details of tube reactors containing solid particles
- B01J2208/065—Heating or cooling the reactor
-
- 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
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0022—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for chemical reactors
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F2225/00—Reinforcing means
- F28F2225/08—Reinforcing means for header boxes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F2265/00—Safety or protection arrangements; Arrangements for preventing malfunction
- F28F2265/26—Safety or protection arrangements; Arrangements for preventing malfunction for allowing differential expansion between elements
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/02—Header boxes; End plates
- F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
- F28F9/0282—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by varying the geometry of conduit ends, e.g. by using inserts or attachments for modifying the pattern of flow at the conduit inlet or outlet
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Geometry (AREA)
- Fluid Mechanics (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The utility model relates to a kind of heat exchange reactor (100), it is for carrying out neither endothermic nor exothermic reaction, comprise: housing (101), described housing defined reaction wall (102), a plurality of transfer pipes (103), the first tube head (105), it is positioned at the part place, top of housing, top part for supporting hot transfer tube, the second tube head (106), it is positioned at the part place, bottom of housing, bottom part for supporting hot transfer tube, be positioned at least first fluid chamber (107) of described housing inner side, second fluid chamber (108) and San fluid chamber (109), at least four fluid openings in described housing: at least one fluid openings (110) in first fluid chamber, at least two fluid openings (111 in second fluid chamber, 112) at least one fluid openings (113) and in San fluid chamber.
Description
Technical field
The present invention relates to a kind of for carrying out the heat exchange reactor of neither endothermic nor exothermic catalytic reaction.Especially, the present invention relates to a kind of heat exchange reactor with improved Fluid Sealing for pyroreaction.Heat exchange reactor can be a part for main equipment (such as production equipment).
Background technology
For carrying out the catalytic reactor of neither endothermic nor exothermic reaction, be as known in the art, special example is for the reactor of the heat absorption steam reformation of hydrocarbon with for the heat release methyl alcohol synthetic reaction reactor of (scope of the present invention not being limited to these reactions).Reaction is typically carried out in the pipe that is loaded with applicable solid catalyst, comprises that the process air-flow of reactant passes this pipe under the pressure raising.A plurality of pipes are arranged in reactor vertically or flatly.Pipe extends in parallel along the main shaft of catalytic reactor, and heat exchange medium heating or the cooling tube in pipe outside.The solid catalyst of pipe inner side provides catalyst bed, and required chemical reaction occurs in this catalyst bed.Catalyst can be provided as solid particle or be provided as and be coated with the structure of carrying out, and for example, is provided as the thin layer on the inwall that is fixed on the pipe in steam reformer reactors.
In comprising another reactor structure of a plurality of pipes, solid catalyst particle can be arranged on the outside of described pipe (hereinafter also referred to as transfer pipes), and heat exchange medium is through inner side simultaneously.The solid catalyst in transfer pipes outside provides catalyst bed, and required chemical reaction occurs in this catalyst bed.
The transfer pipes of other type and heat exchange reactor are known in the art.Hereinafter, with reference to heat exchange reactor and the transfer pipes with the catalyst that is arranged in pipe inner side, the present invention is described, and wherein, pipe and reactor are roughly arranged vertically.Yet scope of the present invention is not limited to pipe and the reactor of these types.Term " catalytic reactor ", " heat exchange reactor " and " reactor " are used interchangeably." catalyst bed " means to form the volume of the solid catalyst of described bed, and it is in transfer pipes inner side.Term " transfer pipes " and " pipe " are used interchangeably, and contain the pipe contacting with catalyst and heat exchange medium for the object of carrying out catalytic reaction.
Wherein process and the reactor of catalyst and heat exchange medium mediate contact are known from EP0271299.This quotes reactor and the process that discloses combined steam reformation and self-heating recapitalization.Be arranged in the pipe that steam reformation area in the lower area of reactor comprises the some with the catalyst that is arranged on inner side, and on the upper area of reactor, autothermal reforming catalyst is arranged on steam reformation pipe outside.EP-A-1106570 discloses a kind of technique for tubulose reformer (reactor) steam reformation being connected in parallel, and this reformer comprises the steam reformation pipe of some and heats by indirect heat exchange.Catalyst is arranged on the outside of steam reformation pipe in a reactor, and in another reactor, is arranged on the inner side of steam reformation pipe.
WO0156690 has described a kind of heat exchange reactor, it comprise be provided with process gas entrance and exit port shell, be bearing in a plurality of reactor tubes of their upper end, for process gas is supplied to the collector device of the upper end of reactor tube from described collector ingress port, described device comprises two or more main-inlet collectors of being arranged to across the top part of described shell, each main-inlet collector has the degree of depth that is greater than its width, thus, described pipe about shell directly or indirectly by described main-inlet manifold supports.
EP1048343A discloses a kind of reactor of heat exchanger type, it has a plurality of pipes that keep catalyst, the shell section that heat transmission medium transmits through its heat with the reacting fluid in execution and described pipe, and upper perforated plate and lower perforated plate, the upper end of described pipe is attached to described upper perforated plate via the first expansion pipe that is fixed to the upside of described upper perforated plate, the lower end of described pipe is directly fixed to relocatable lower perforated plate, relocatable space forms, this space is separated by described lower perforated plate and the inner end plate (interior head) that is attached to its downside, and there is the opening in the part of bottom, and described opening is attached to the pipe side outlet in reactor outside via the second expansion pipe.
Due to the state of catalytic reaction process, therefore heat exchange reactor must have following structure, this structure can absorption tube and housing between the differential thermal expansion that causes due to the temperature difference between them.In addition, the differential thermal expansion of this structure between must can absorption tube, this differential thermal expansion is by causing below: the temperature difference between the pipe that difference in the reaction between pipe and hot transmit mode produces, catalyst the encapsulation difference of density, the difference of catalyst activity of the difference of the difference producing due to the tolerance of the bore in reactor, the catalyst encapsulation density in each pipe, the difference producing due to the tolerance of the bore in reactor, each pipe, flow through the reacting gas of pipe uneven distribution, flow through the uneven distribution etc. of the heat transmission medium of shell section.
Have the conventional heat exchange reactor that the pipe that is fixed in tube head and tube head be fixed to reactor shell and can not meet these requirements, this is because they can not process the differential thermal expansion between housing and pipe or between pipe.In EP 1048343, thermal expansion can be absorbed by the first expansion pipe of each pipe and the second expansion pipe that is connected to unsteady lower tube head.Therefore, solution by EP 1048343 disclosed expansion issues needs the first expansion pipe and the second expansion pipe, and further, the first expansion pipe must have enough intensity, and this intensity can be born load that the weight due to pipe, catalyst and lower tube head produces and the pressure differential between tube side part and shell-side.Further, if reacting fluid or heat-exchange fluid have for example 500 ℃ or higher temperature, the second expansion pipe of EP 1048343 is desirably isolated with reacting fluid or heat-exchange fluid, and this is to be debatable because air-tightness joint is provided under this high temperature.Another solution is by providing labyrinth for example to accept the Leakage Gas slightly of expansion pipe place.Yet this is not all acceptable for all application.
Summary of the invention
One object of the present invention is to provide a kind of heat exchange reactor, and it has solved the problem of mentioning, especially expansion issues.Another object is to provide a kind of improved heat exchange reactor, and it can at high temperature operate, but still has the airtight sealing between tube and tube head.
Feature of the present invention
1. one kind for carrying out the heat exchange reactor (100) of neither endothermic nor exothermic reaction, and it comprises:
Housing (101),
Described housing defined reaction wall (102),
A plurality of transfer pipes (103), it is interior for supplying or remove the heat of the catalyst bed (104) that is arranged on described transfer pipes inner side or outside that it is arranged in described housing,
The first tube head (105), it is positioned at the part place, top of housing, for the top part of supporting hot transfer tube,
The second tube head (106), it is positioned at the part place, bottom of housing, for the bottom part of supporting hot transfer tube,
Be positioned at least first fluid chamber (107), second fluid chamber (108) and the San fluid chamber (109) of described housing inner side, described first fluid chamber is arranged in the top part of the housing of the first tube head top, in the centre portion of the housing of described second fluid chamber between the first tube head and the second tube head, and described San fluid chamber is arranged in the bottom part of the housing of the second tube head below
At least four fluid openings in described housing: at least one fluid openings (110) in first fluid chamber, at least two fluid openings (111 in second fluid chamber, 112) at least one fluid openings (113) and in San fluid chamber
The first tube head and the second tube head have the perforate for each of transfer pipes, wherein, the bottom part of each transfer pipes by the second tube head along side direction and fixed bearing upwards, and the top part sliding bearing of each transfer pipes is to the first tube head, thus, described the second tube head supports the load of a plurality of transfer pipes, and prevent that them from moving about the second tube head, and the first tube head supports a plurality of transfer pipes along lateral, allow transfer pipes to move up and down about the first tube head, and the sliding bearing of the top part of transfer pipes comprises fluid-tight seal (118).
2. according to the heat exchange reactor described in feature 1, it is characterized in that, the described bottom part of transfer pipes comprises bottleneck (114), thus, the area of section of each perforate in the area of section of the lower end of transfer pipes and the second tube head is less than the area of section of the transfer pipes of bottleneck top.
3. according to the heat exchange reactor described in feature 2, it is characterized in that, catalyst bed is positioned at transfer pipes inner side, and described transfer pipes includes each the supporting member (115) of bottom part of the transfer pipes that is arranged in bottleneck top, with supporting catalyst bed.
4. according to the heat exchange reactor described in feature 3, it is characterized in that, also comprise the separator (116) between bottleneck and supporting member, to adapt to the height of supporting member.
5. according to the heat exchange reactor described in feature 4, it is characterized in that, described supporting member and described separator are an integrated unit.
6. according to the heat exchange reactor described in any one in aforementioned feature, it is characterized in that, at least one in the first tube head and the second tube head has concave shape.
7. according to the heat exchange reactor described in any one in aforementioned feature, it is characterized in that, the second tube head has elliptical shape, and thus, the edge of described the second tube head is distributed in the load of transfer pipes.
8. according to the heat exchange reactor described in any one in aforementioned feature, it is characterized in that, at least one in the first tube head and the second tube head is isolated thing (117) isolation at least one side of tube head.
9. according to the heat exchange reactor described in feature 8, it is characterized in that, described spacer (117) is arranged on the sidepiece in the face of at least one of the first tube head of second fluid chamber and the second tube head, and the thickness of spacer is suitable for so that spacer has the surface of general plane on the face of spacer that faces second fluid chamber.
10. according to the heat exchange reactor described in any one in feature 8 to 9, it is characterized in that, a part and the spacer of each in the transfer pipes in the second fluid chamber between the first tube head and the second tube head have length about equally.
11. according to the heat exchange reactor described in any one in aforementioned feature, it is characterized in that, for each transfer pipes, described seal comprises the have wire packing stuffing-box (119) of (120), this wire packing (120) around transfer pipes by compressing device (121) compression.
12. according to the heat exchange reactor described in any one in aforementioned feature, it is characterized in that, at least one in transfer pipes is provided with in the attachment means at part place, top (122,130), thereby realizes all heat-exchange tubes of at least lifting and the second tube head.
13. according to the heat exchange reactor described in any one in aforementioned feature, it is characterized in that, described reactor wall at least forms the first tubular section (124) of being arranged by top, second fluid chamber part, the second tubular section (125) of being arranged by second fluid chamber mid portion, and the 3rd tubular section (126) of being arranged by bottom, second fluid chamber part, described the first tubular section and described the 3rd tubular section have the diameter that is greater than the second tubular section, with allow at least two doughnuts equably distributing fluids travel to and fro between at least two fluid openings in second fluid chamber and travel to and fro between bottom surface section and the upper surface portion of transfer pipes.
14. according to the heat exchange reactor described in any one in aforementioned feature, it is characterized in that, also comprise around transfer pipes and be arranged in the indoor liner of second fluid (127), described liner has bottom surface section and the upper surface portion that perforation (129) is travelled to and fro between at least two fluid openings of second fluid chamber for distributing fluids equably and travelled to and fro between transfer pipes.
15. according to the heat exchange reactor described in feature 14, it is characterized in that, in the face of at least one at least a portion in region of described liner at least two fluid openings in second fluid chamber does not have described perforation, described region can be used as fluid impact plate thus.
In an embodiment of the present invention, for carrying out the heat exchange reactor of neither endothermic nor exothermic reaction, comprise housing, transfer pipes, tube head, fluid chamber and the fluid openings with reactor wall.Housing and transfer pipes are arranged in roughly vertical position, and this is conducive to the structural strength of the member under the especially operation under the temperature and pressure raising.Reactor is divided at least San Ge fluid chamber by tube head.In the first fluid chamber that is arranged in the top part of the housing above the first tube head, first fluid is put into through fluid openings, and is dispensed to transfer pipes.First fluid flows downstream into the San fluid chamber of the bottom part that is arranged in the housing below the second tube head in pipe inner side, wherein, in the adfluxion from each pipe, and emit from fluid openings.In the second fluid chamber that is arranged in the centre portion of reactor shell, second fluid is put into via a fluid openings that is arranged in the bottom part of centre portion.Second fluid upwards flows in centre portion, simultaneously its heat exchange with first fluid by the execution of transfer pipes wall.In the part of the top of centre portion, second fluid is emitted by another fluid openings.Catalyst bed can be arranged in the inner side of the pipe in second fluid chamber or the outside of pipe.Transfer pipes is supported by two tube heads.Pipe sliding bearing is on first in the perforate in tube head, and the movement of therefore resisting along continuous straight runs when the top of each pipe part is supported and fixedly time, they are independent of each other and vertically move freely.For the present invention, pipe is fixed in second time tube head especially, and they can not move along any direction about the second tube head.The position of the corresponding perforate of the bottom part of each pipe in described tube head is fixed to the second tube head; It can be fixed together with the lower end of each pipe directly over corresponding perforate, be fixed together with the end of the pipe of perforate inner side, or is fixed together with the end sections of pipe and the tube end of tube head below in perforate.Pipe is fixed to the second tube head can be completed with any known way, as for example, welds, and it is preferred, and this is because it is bubble-tight.Importantly, fixing means can tolerate operating temperature.Understand, because pipe only vertically slides and is fixed to the first tube head, therefore the second tube head supports the load of a plurality of transfer pipes.
First fluid can flow along downward direction: via the fluid openings in first fluid chamber, it flows and flow out to San fluid chamber and from fluid openings through transfer pipes from first fluid chamber; Or in other embodiments, it can flow in opposite direction.In an embodiment, the fluid openings of second fluid can the bottom part along upward direction from second fluid chamber flows, and is upward through second fluid chamber, and flows out from second fluid chamber via the fluid openings in the top part of second fluid chamber around pipe.First fluid flows downward therein, and second fluid upwards flows, and catalyst bed is placed in transfer pipes inner side, and in the embodiment of endothermic heat of reaction, second fluid must transfer heat to first fluid.Therefore, advantageously, in the situation that temperature is the highest, pipe for example fixes by being welded to the second tube head.
In an embodiment of the present invention, transfer pipes has the bottleneck at their part place, bottom, and the external diameter of pipe and internal diameter reduce thus.Therefore, the end portion that is fixed to the pipe of the second tube head needs the corresponding perforate in the second tube head, and it is only even as big as the pipe diameter corresponding to reducing, this tube head than the perforate perforation by larger diameter and then increased the intensity of the second tube head.
Catalyst bed is arranged in another embodiment of the present invention of transfer pipes inner side therein, is positioned at the pipe inner side of bottom part of the pipe of bottleneck top for the supporting member of catalyst bed.Supporting member can have any applicable structure, for example, and the silk screen on the top of the supporting grid being held by support ring.Bottleneck serves as the lower support stop part of catalyst supports part, and separator can be placed between bottleneck and catalyst supports part, to adjust the height of the catalyst bed in each pipe.Supporting member and separator also can be integrated into single unit, and the height of this unit then can change to adjust the height of the catalyst bed in each pipe as mentioned.
In yet another embodiment of the present invention, at least one in the first tube head and the second tube head has concave shape.Especially for the second tube head of the load of supporting hot transfer tube and catalyst bed, concave shape (for example, elliptical shape) is favourable, this be because its by the load transfer on the core of tube head the periphery to tube head, wherein, tube head can be supported by reactor wall.The separator of adjusting the height of the catalyst supports part in each pipe can be suitable for compensating the concave shape of the second tube head, makes the bottom of the catalyst bed in each pipe have the equal height in reactor.This is favourable in expectation during the even catalyst activity in all pipes.
In an embodiment, at least one in the first tube head and the second tube head is isolated on the sidepiece of the tube head in the face of second fluid chamber.In the situation of temperature in second fluid chamber higher than the temperature in first fluid chamber and San fluid chamber and in pipe, the tube head of spacer protective separation is avoided high temperature, and therefore the thickness of tube head can reduce for given requirement of strength therein.This is especially favourable for the second load-carrying tube head.In addition, isolation thickness can be similar to the height of the catalyst supports part of the given concave shape that is suitable for compensating the first tube head and/or the second tube head, insulation surfaces is roughly plane thus, and the length of the pipe between relative insulation surfaces or between insulation surfaces and relative tube head can be for all pipes all about equally.In yet another embodiment, the top of the catalyst bed in each transfer pipes is positioned at the At The Height identical or almost identical with insulation surfaces with bottom.
In an embodiment of the present invention, the top part of each transfer pipes tube head sealing upward.Seal provides lateral-supporting and the roughly fluid-tight connection of the pipe in the perforate of tube head, but allowed pipe described slippage about the first tube head in perforate.In an embodiment, seal comprises the stuffing-box for each pipe.Stuffing-box can be fixed around each perforate (for example,, by welding or other known means) to the first tube head.Seal can be ceramic packing rope, its between stuffing-box and the outer wall of each pipe around pipe by means of compressor (such as, nut or any other known compression device) compress.Stuffing-box also can comprise locked plug-in unit (such as, lock(ing) bolt), to prevent the dismounting of compressor reducer part.
Special advantage of the present invention is, relatively hot fluid enters second fluid chamber via the fluid openings in the bottom part of second fluid chamber and relatively cold fluid (by relatively hot fluid heating) flows through in the embodiment of transfer pipes therein, and the seal that is arranged in the stuffing-box of first fluid chamber is exposed to significantly lower than the temperature of the maximum temperature of hot fluid relatively.This means the process that is even significantly higher than the maximum permissible dose of given encapsulant for wherein the hottest inlet gas, also can realize roughly fluid-tight seal.
In yet another embodiment of the present invention, at least one in transfer pipes is provided with the attachment means at part place, the top of pipe.This allows the installation of Mechanical stops (for example, in being fixed to the hanger of the first tube head), and this Mechanical stops prevents that transfer pipes from skidding off from the first tube head when its lifting.Attachment means can be any known technology, such as, screw thread, the perforate through pipe, springlock, hangnail, connector, united piece, connector etc.; And they can be arranged on outside, inner side or outside and the inner side of pipe.Attachment means provides transfer pipes in reactor and the simple installation of tube head: the Mechanical stops of some that is enough to the gross weight of carrying pipe and tube head is arranged on the attachment means place on the top of pipe of respective amount, afterwards all pipes and the first tube head and the second tube head liftable.After in tube head and pipe are arranged on to reactor, remove Mechanical stops.
In an embodiment of the present invention, two fluids distribution doughnuts are provided as with two fluid openings in second fluid chamber and are connected.Doughnut provides homogeneous (uniform) fluid from fluid intake opening to the region around all transfer pipes nearest from one end to distribute, and distributes from the homogeneous (uniform) fluid from the nearest region around all transfer pipes of the other end to fluid issuing opening.Described doughnut is configured to around the section of reactor wall of second fluid chamber with the diameter of expansion, and this allows fluid to flow around tube bank.The section of these enlarged diameter of reactor wall is arranged in top part and the bottom part of second fluid chamber.The mid portion of fluid chamber has the reactor wall diameter that is only slightly greater than tube bank external diameter, with minimum material consumption.In one embodiment of the invention, the fluid intake of second fluid chamber is at part place, the bottom of second fluid chamber, and the indoor fluid issuing of second fluid is at part place, the top of second fluid chamber.Around the fluid in the second fluid chamber of all transfer pipes be uniformly distributed and as previously mentioned the even heat of all having guaranteed between uniform reaction level and transfer pipes inner side and the fluid in outside that is uniformly distributed of the catalyst bed in the even length of transfer pipes transmit.
In an embodiment of the present invention, by the liner that is arranged in the reactor wall inner side of second fluid chamber and holds all transfer pipes (tube bank), further guaranteed the homogeneous (uniform) fluid distribution around all transfer pipes.At least in the part in the region of doughnut, be lined with the opening distributing around liner in described, itself otherwise form the sheet that surrounds tube bank.Opening in the liner in the region by the doughnut for fluid intake, the fluid in second fluid chamber flow to corresponding doughnut from fluid intake, and enters from the nearest space around transfer pipes, one end of pipe.Similarly, opening in the liner in the region by the doughnut for fluid issuing, fluid in second fluid chamber is from the nearest spatial flow around transfer pipes of the other end from pipe, through the opening in the liner in the region for the doughnut of fluid issuing, to corresponding doughnut, and leave by the fluid issuing of second fluid chamber.Liner can be the seal that is closely fixed to reactor wall, and to guarantee there is no bypass of fluid between tube bank and reactor wall, this is because will reduce heat transference efficiency through the fluid exporting from second fluid chamber inlet to second fluid chamber between reactor wall and tube bank.
In yet another embodiment of the present invention, the opening in described liner around the even circumferential of each end of liner distribute, except directly in the face of the region of the liner of the fluid openings of second fluid chamber.In these regions, at least a portion of liner does not have opening, and thus, this part of liner is as fluid impact plate, and this fluid impact plate further provides around the homogeneous (uniform) fluid of transfer pipes and distributes.
As known in the art, tube bank can be provided with baffle plate, and for example, the baffle plate of dish and baked donut type, with the heat transmission between the fluid in further reinforced pipe outside and the fluid of pipe inner side.
Accompanying drawing explanation
Some embodiments of the present invention with reference to the accompanying drawings discuss the present invention in more detail, in this accompanying drawing:
Fig. 1 is the side cross-sectional view of an embodiment of heat exchange reactor,
Fig. 2 is the fluid intake of second fluid chamber and the sectional top view of outlet,
Fig. 3 is the side cross-sectional view of the heat exchange reactor before assembling,
Fig. 4 is the detailed view of the first tube head of isolation,
Fig. 5 is the detailed view of the second tube head of isolation,
Fig. 6 a and Fig. 6 b are liner and the detailed view with the first tube head of baffle plate and connecting rod,
Fig. 7 is the detailed view of the bottom part of transfer pipes,
Fig. 8 is the detailed view of embodiment of stuffing-box at the part place, top of transfer pipes,
Fig. 9 is the detailed view of top part that comprises the pipe of attachment means,
Figure 10 is the second tube head of isolation and the detailed view of San fluid chamber,
Figure 11 is the detailed view of the section of transfer pipes,
Figure 12 is the detailed view of the embodiment of stuffing-box.
List of parts
100. heat exchange reactor
101. housing
102. reactor wall
103. transfer pipes
104. catalyst bed
105. first tube heads
106. second tube heads
107. first fluid chambers
108. second fluid chambers
109. San fluid chamber
110. fluid openings, first fluid chamber
111. fluid openings, top, second fluid chamber part
112. fluid openings, bottom, second fluid chamber part
113. fluid openings, San fluid chamber
114. bottleneck
115. supporting grids
116. separator
117. spacer
118. seal
119. stuffing-box
120. wire packing
121. compression devices
121a. locked plug-in unit
122. attachment means (screw thread)
123. hanger
124. reactor walls first on tubular section
The second intermediate tubular section of 125. reactor walls
The 3rd time tubular section of 126. reactor walls
127. liner
128. baffle plate
129. liner perforation
130. lock nut.
The specific embodiment
Will be appreciated that to be only below specific embodiments more of the present invention.An advantage of the present invention is that it is telescopic, so other size is scope of the present invention with pipe quantity.
HTER is tubulose heat-exchange reformer as shown in Figure 1.It is heat exchange reactor 100, and it comprises housing 101, and housing 101 has the catalyst 104 of reactor wall 102 and transfer pipes 103 inner sides.It has two strands of streams that separate; At pipe side (pipe inner side) upper mobile process gas (PG) with at the upper mobile Exhaust Gas (EG) of shell-side (pipe outside).There are 1300 pipes.In this embodiment, catalytic reaction is the endothermic reaction.Therefore, from Exhaust Gas, the shell-side at pipe transmits the process gas needs heat of pipe inner side.
Process gas stream
Relatively cold process gas (Exhaust Gas is colder relatively) enters first fluid chamber 107 at the place, just top of reactor by the fluid openings 110 in first fluid chamber, and is dispensed to transfer pipes via the first tube head 105.PG flows through the pipe that is filled with catalyst, and reforming reaction occurs receiving from shell-side in hot.PG leaves pipe via the second tube head 106, flow to San fluid chamber 109, and flows out by fluid openings 113.
Exhaust Gas stream
Relatively hot EG (relatively process gas hotter) enters the second fluid chamber 108 on the shell-side of pipe by the fluid openings 112 in the part of bottom, second fluid chamber.Stream, through being the pipe of shutter configuration, is delivered to heat the reaction of pipe inner side.EG flows out by the fluid openings 111 in the part of top, second fluid chamber.Baffle plate 128 has dish and baked donut structure, and causes the cross-current largely through pipe.By EG flow point be assigned to tube bank/from tube bank distribute EG flow through by reactor wall 124 first doughnut and liner 127 in the 3rd time tubular section of tubular section neutralization reaction wall 126 complete, provided tube bank as shown in Figure 2 expectation radially entrance and radially export.When EG enters reactor, it is distributed on circumference in the doughnut around liner.Then, EG flows through the perforation 129 of making in liner.At nozzle location place, there is less perforation.With which, liner is as shock plate.When EG flows out shutter configuration, also at top, middle punch obtains radial flow from the bottom of reactor, to be stretched over the liner at top.Liner is welded to reactor wall 102, to avoid the bypass of EG.In the second intermediate tubular section of reactor wall 125, when not having fluid to be intended in this section bypass, liner is near tube bank.
In Fig. 3, show individually the shell of the reactor that comprises liner and tube bank before bundle is arranged on reactor inner side as can be seen.Oval pipe head from the load of 1300 pipes in the bottom of reactor is received.Tube head is isolated above tube head, causes the temperature of tube head of the process gas of effuser.The top shell flange place that loads on of upper oval pipe head, baffle plate and connecting rod is accepted.Upper tube head is isolated in lower head, has given its PG inlet temperature.The circular cone connecting portion place that loads on from liner is received by shell joint.
Thermal expansion
Pipe is fixed on lower tube head place.The thermal stretching of pipe is received by the Yi Ge mechanism (stuffing-box 119 of pipe) of each pipe at upper tube head place.The individual difference that this has allowed pipe as seen in Figure 4 to extend.Shutter configuration utilizes connecting rod to hang from head tube head, and moves down when being heated.Liner is welded to shell.To expand respectively up and down from this point in the two ends of liner.
Upper tube head assembly
Upper tube head has the ear 123 for the some of the installation activity lifting at bundle.Head utilizes fiber ceramics material and lower isolation, and this fiber ceramics material is held in place by interior lining panel.The tube head perforation of 1300 pipes.In each perforation place, there is the packing box assembly of above-head.
Lower tube head assembly
Head utilizes fiber ceramics material and upper isolation, and fiber ceramics material is held in place by metal inner lining plate, sees Fig. 5.
Liner and baffle plate assembly
Liner is welded to the circular cone on shell.It is in top and the perforation of place, bottom.
Baffle plate is held in place by connecting rod.As seen in Figure 6 b, connecting rod is connected to tube head.
Pipe assembly
Pipe is the vicissitudinous length of tool due to oval-shaped tube head.
There is attachment means 122, such as, the threaded sections in the top of the pipe in a part for pipe.This attachment means when carrying out lifting bundle by hanger for lock nut 130 is installed.
Silk screen
With reference to Fig. 7, catalyst relies on supporting grid 115.Separator 116 remains on correct height such as thin walled cylindrical pipe by catalyst supports grid.Pipe diameter diminishes in the base section of pipe is in bottleneck 114.This is done, to obtain larger toughness, and so thinner tube head.Different embodiment has been shown in Figure 11, the needs that it has omitted separator by the part that changes the diameter of the below that changes transfer pipes into and reduce and alternative bottleneck, the diameter of the bottom part of pipe reduces by means of edge.
Packing box assembly
1300 stuffing-boxes 119 comprise the residing stuffing-box of seal 118 comprising wire packing 120.As visible on Fig. 8, there is compression device 121 (such as gland ring), it is as hollow bolt work, and when rope is compressed, this hollow bolt is around pipe rotation.Between rope and gland ring, there is driven torus, it protects wire packing to avoid frictional force when letter tensioning.Packing box assembly is welded to tube head from inner side.On Figure 12, seen another embodiment of stuffing-box.Here, compression gland ring is locked by another ring 121a.
Assembling
For tube bank is assembled in shell, the hanger lifting at your above tube head place.Lower tube head is elevated to top portion by the pipe being held in place by lock nut.Fig. 9: packing box assembly is shown with lock nut 130 (left side top).Lock nut is as wherein connecting the upper tube head of crane and the connector between pipe and lower tube head.When bundle is in place, between lower tube head and shell connector, complete seal welding.
Figure 10: the final number of assembling steps of the base section of reactor.Bundle declines, and oval pipe head and the sealed welding of shell connector.
Example
The cold process gas of ~ 410 ℃ enters at the place, just top of reactor, and is dispensed to pipe.PG flows through the pipe that is filled with catalyst, and reforming reaction occurs receiving from shell-side in hot.PG leaves pipe at ~ 750 ℃, and flows out by outlet at bottom.
The hot EG of ~ 1005 ℃ enters by lower nozzle on shell-side.Stream, through being the pipe of shutter configuration, is delivered to heat the reaction of pipe inner side.EG flows out by upper casing side nozzle at the temperature of ~ 600 ℃.
Top portion has the internal diameter of 4250mm, and 85mm is thick, and is made by SA-387 gr22 cl2.Head utilizes fiber ceramics material and lower isolation, and this fiber ceramics material is held in place by thick nichrome 693 interior lining panels of 3mm.
Head portion is that 50mm is thick, and has the internal diameter of 3600mm.Head is made by inconel 625 or extra large sodium cobalt chromium tungsten nickel (Haynes) 230.Head utilizes fiber ceramics material and upper isolation, and this fiber ceramics material is held in place by thin inconel 693 interior lining panels of 3mm.Liner, baffle plate and connecting rod are made by inconel 693.
Pipe is about 11 meters long, and wherein, internal diameter is that 50mm and external diameter are 60mm.All parts of pipe assembly are made by inconel 693.
Claims (15)
1. one kind for carrying out the heat exchange reactor (100) of neither endothermic nor exothermic reaction, and it comprises:
Housing (101),
Described housing defined reaction wall (102),
A plurality of transfer pipes (103), it is interior for supplying or remove the heat of the catalyst bed (104) that is arranged on described transfer pipes inner side or outside that it is arranged in described housing,
The first tube head (105), it is positioned at the part place, top of described housing, for supporting the top part of described transfer pipes,
The second tube head (106), it is positioned at the part place, bottom of described housing, for supporting the bottom part of described transfer pipes,
Be positioned at least first fluid chamber (107), second fluid chamber (108) and the San fluid chamber (109) of described housing inner side, described first fluid chamber is arranged in the top part of the described housing of described the first tube head top, in the centre portion of the described housing of described second fluid chamber between described the first tube head and described the second tube head, and described San fluid chamber is arranged in the bottom part of the described housing of described the second tube head below
At least four fluid openings in described housing: at least two fluid openings (111 at least one fluid openings (110) in described first fluid chamber, described second fluid chamber, 112) at least one fluid openings (113) and in described San fluid chamber
Described the first tube head and described the second tube head have the perforate for each of described transfer pipes, wherein, the described bottom part of each transfer pipes by described the second tube head along side direction and fixed bearing upwards, and the top part sliding bearing of each transfer pipes is to described the first tube head, thus, the load of the described a plurality of transfer pipes of described the second tube head supporting, and prevent that them from moving about described the second tube head, and described the first tube head is along the described a plurality of transfer pipes of lateral supporting, allow described transfer pipes to move up and down about described the first tube head, and the sliding bearing of the top part of described transfer pipes comprises fluid-tight seal (118).
2. heat exchange reactor according to claim 1, it is characterized in that, the described bottom part of described transfer pipes comprises bottleneck (114), thus, the area of section of each perforate in the area of section of the lower end of described transfer pipes and described the second tube head is less than the area of section of the transfer pipes of described bottleneck top.
3. heat exchange reactor according to claim 2, it is characterized in that, described catalyst bed is positioned at described transfer pipes inner side, and described transfer pipes includes each the supporting member (115) of bottom part of the described transfer pipes that is arranged in described bottleneck top, to support described catalyst bed.
4. heat exchange reactor according to claim 3, is characterized in that, also comprises the separator (116) between described bottleneck and described supporting member, to adapt to the height of described supporting member.
5. heat exchange reactor according to claim 4, is characterized in that, described supporting member and described separator are an integrated unit.
6. according to heat exchange reactor in any one of the preceding claims wherein, it is characterized in that, at least one in described the first tube head and described the second tube head has concave shape.
7. according to the heat exchange reactor described in any one in claim 1-5, it is characterized in that, described the second tube head has elliptical shape, and thus, the edge of described the second tube head is distributed in the load of described transfer pipes.
8. according to the heat exchange reactor described in any one in claim 1-5, it is characterized in that, at least one in described the first tube head and described the second tube head is isolated thing (117) isolation at least one side of described tube head.
9. heat exchange reactor according to claim 8, it is characterized in that, described spacer (117) is arranged on the sidepiece in the face of at least one of described first tube head of described second fluid chamber and described the second tube head, and the thickness of described spacer is suitable for so that described spacer has the surface of general plane on the face of described spacer that faces described second fluid chamber.
10. heat exchange reactor according to claim 8, it is characterized in that, a part and the described spacer of each in the described transfer pipes in the described second fluid chamber between described the first tube head and described the second tube head have length about equally.
11. according to the heat exchange reactor described in any one in claim 1-5, it is characterized in that, for each transfer pipes, described seal comprises the have wire packing stuffing-box (119) of (120), described wire packing (120) around described transfer pipes by compressing device (121) compression.
12. according to the heat exchange reactor described in any one in claim 1-5, it is characterized in that, at least one in described transfer pipes is provided with the attachment means (122,130) at part place, described top, thereby realizes all described heat-exchange tubes of at least lifting and described the second tube head.
13. according to the heat exchange reactor described in any one in claim 1-5, it is characterized in that, described reactor wall at least forms the first tubular section (124) of being arranged by top, described second fluid chamber part, the second tubular section (125) of being arranged by described second fluid chamber mid portion, and the 3rd tubular section (126) of being arranged by bottom, described second fluid chamber part, described the first tubular section and described the 3rd tubular section have the diameter that is greater than described the second tubular section, with allow at least two doughnuts equably distributing fluids travel to and fro between at least two fluid openings in described second fluid chamber and travel to and fro between bottom surface section and the upper surface portion of described transfer pipes.
14. according to the heat exchange reactor described in any one in claim 1-5, it is characterized in that, also comprise around described transfer pipes and be arranged in the indoor liner of described second fluid (127), described liner has bottom surface section and the upper surface portion that perforation (129) is travelled to and fro between at least two fluid openings of described second fluid chamber for distributing fluids equably and travelled to and fro between described transfer pipes.
15. heat exchange reactors according to claim 14, it is characterized in that, in the face of at least one at least a portion in region of described liner at least two fluid openings in described second fluid chamber does not have described perforation, described region can be used as fluid impact plate thus.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EPPCT/EP2011/003283 | 2011-07-01 | ||
| PCT/EP2011/003283 WO2013004254A1 (en) | 2011-07-01 | 2011-07-01 | Heat exchange reactor |
| PCT/EP2012/060854 WO2013004448A1 (en) | 2011-07-01 | 2012-06-08 | Heat exchange reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203916623U true CN203916623U (en) | 2014-11-05 |
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ID=44628755
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201290000642.6U Expired - Lifetime CN203916623U (en) | 2011-07-01 | 2012-06-08 | Heat exchange reactor |
Country Status (7)
| Country | Link |
|---|---|
| KR (1) | KR20140001590U (en) |
| CN (1) | CN203916623U (en) |
| BR (2) | BR212013033842U2 (en) |
| DE (1) | DE212012000120U1 (en) |
| ES (1) | ES1103681Y (en) |
| RU (1) | RU148799U1 (en) |
| WO (2) | WO2013004254A1 (en) |
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| CN106582468A (en) * | 2015-10-14 | 2017-04-26 | 中国石化工程建设有限公司 | Axial micro-channel coupling reactor and applications thereof |
| CN106693849A (en) * | 2015-08-04 | 2017-05-24 | 中国石化工程建设有限公司 | Methanation reactor and methanation technology |
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| CN103983131A (en) * | 2014-05-29 | 2014-08-13 | 南通航海机械集团有限公司 | Marine light-duty efficient heater |
| US9816767B2 (en) * | 2016-01-12 | 2017-11-14 | Hamilton Sundstrand Corporation | Tubes and manifolds for heat exchangers |
| KR101983667B1 (en) * | 2016-09-29 | 2019-05-29 | 디앤이에스 주식회사 | Cooling and heating energy saving type automatic control system with low flux refrigerator and low flux controlling of cool and heating fluid |
| DE102017203058A1 (en) * | 2017-02-24 | 2018-08-30 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. | Heat exchanger and reactor |
| CN109289749B (en) * | 2017-07-24 | 2024-05-07 | 北京燕东兆阳新能源科技有限公司 | Flameless oxidation heating reactor |
| WO2021217330A1 (en) * | 2020-04-27 | 2021-11-04 | 北京燕东兆阳新能源科技有限公司 | Methanol vaporizing and mixing device, methanol heating reactor, methanol non-flame heating device, and control method |
| WO2022162051A1 (en) * | 2021-01-28 | 2022-08-04 | Topsoe A/S | Catalytic heat exchange reactor with helical flow |
| EP4309780A1 (en) * | 2022-07-20 | 2024-01-24 | Linde GmbH | Tube base for a tubular reactor and reactor comprising such a tube base |
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| GB1316886A (en) * | 1970-12-24 | 1973-05-16 | Semenov V P | Apparatus for use in reforming hydrocarbons under pressure |
| BE790200A (en) * | 1971-10-27 | 1973-04-17 | Babcock & Wilcox Co | IMPROVEMENTS RELATING TO EXCHANGERS OF |
| US4871014A (en) * | 1983-03-28 | 1989-10-03 | Tui Industries | Shell and tube heat exchanger |
| ATE69559T1 (en) * | 1985-06-27 | 1991-12-15 | Stone & Webster Eng Corp | PRODUCTION OF SYNTHETIC GAS BY CONVECTION REFORMING. |
| GB8629497D0 (en) | 1986-12-10 | 1987-01-21 | British Petroleum Co Plc | Apparatus |
| US6153152A (en) * | 1990-04-03 | 2000-11-28 | The Standard Oil Company | Endothermic reaction apparatus and method |
| GB9516125D0 (en) * | 1995-08-07 | 1995-10-04 | Ici Plc | Heat exchange apparatus and process |
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2011
- 2011-07-01 WO PCT/EP2011/003283 patent/WO2013004254A1/en not_active Application Discontinuation
-
2012
- 2012-06-08 DE DE212012000120.4U patent/DE212012000120U1/en not_active Expired - Lifetime
- 2012-06-08 ES ES201450003U patent/ES1103681Y/en not_active Expired - Fee Related
- 2012-06-08 BR BR212013033842U patent/BR212013033842U2/en active IP Right Grant
- 2012-06-08 BR BR112013033842-3A patent/BR112013033842B1/en not_active IP Right Cessation
- 2012-06-08 RU RU2014103299/05U patent/RU148799U1/en active
- 2012-06-08 KR KR2020137000082U patent/KR20140001590U/en not_active Application Discontinuation
- 2012-06-08 WO PCT/EP2012/060854 patent/WO2013004448A1/en active Application Filing
- 2012-06-08 CN CN201290000642.6U patent/CN203916623U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106693849A (en) * | 2015-08-04 | 2017-05-24 | 中国石化工程建设有限公司 | Methanation reactor and methanation technology |
| CN106582468A (en) * | 2015-10-14 | 2017-04-26 | 中国石化工程建设有限公司 | Axial micro-channel coupling reactor and applications thereof |
| CN106582468B (en) * | 2015-10-14 | 2019-04-26 | 中国石化工程建设有限公司 | A kind of axial direction microchannel coupled reactor and application |
Also Published As
| Publication number | Publication date |
|---|---|
| DE212012000120U1 (en) | 2014-02-14 |
| ES1103681Y (en) | 2014-06-10 |
| BR112013033842B1 (en) | 2019-09-24 |
| ES1103681U (en) | 2014-03-19 |
| WO2013004448A8 (en) | 2014-02-06 |
| BR212013033842U2 (en) | 2015-11-03 |
| WO2013004254A1 (en) | 2013-01-10 |
| RU148799U1 (en) | 2014-12-20 |
| KR20140001590U (en) | 2014-03-17 |
| WO2013004448A1 (en) | 2013-01-10 |
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