CN103240036B - A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application - Google Patents
A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application Download PDFInfo
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- CN103240036B CN103240036B CN201210033806.1A CN201210033806A CN103240036B CN 103240036 B CN103240036 B CN 103240036B CN 201210033806 A CN201210033806 A CN 201210033806A CN 103240036 B CN103240036 B CN 103240036B
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Abstract
The invention discloses a kind of heat transfer reactor of Anti-temperature difference stress, including housing and heat exchanging piece, the housing unloads outlet provided with air inlet, gas outlet, manhole and catalyst, described heat exchanging piece includes some heat exchanger tubes and one or more pairs of headers with tube sheet, along around pipe shaft core, twist axially winding is set, adjacent two heat exchanger tubes of Internal and external cycle or same circle footpath are connected described heat exchanger tube by return bend or inverted U elbow.The heat transfer reactor of the present invention can more serial or parallel connections be applied in combination, reactor or horizontal water pipe reactor composition combined reactor can also be gas-cooled with air cooling reactor or around pipe to meet large-scale reaction unit needs.The heat transfer reactor of the present invention can be widely applied to various strong exothermal reactions or the endothermic reaction.The heat transfer reactor of the present invention is using return bend connection around pipe type heat transfer pipe, and retractable, structure is reliable, reduces joint leakage possibility, and Catalyst packing coefficient is high, greatlys save equipment investment, and the large-scale, ultra-large type that is particularly suitable for use in produces million tons of devices per year.
Description
Technical field
The present invention relates to the catalytic reaction device of field of chemical engineering, for fluid catalyst reaction and diabatic process, especially
It is related to a kind of suitable for synthesizing methanol, dimethyl ether, methanation, F-T reactions, H2The strongly exothermic or endothermic reactions such as S oxidations, ammonia synthesis
Heat transfer reactor of process and combinations thereof device and application.
Background technology
China's coal chemical industry is developed rapidly in recent years, and the scale of newly-built methanol device is brought up to single set and produces 100 per year by country
More than ten thousand tons, the unstripped gas of synthesizing methanol is not the former external natural gas conversion gas used mostly yet, but producing synthesis gas from coal,
C/Hratio greatly improves in synthetic raw gas, causes the reaction heat of per unit product to be up to more than 2 times, and this is large-scale to methanol device
Change and propose huge challenge.
For some strong exothermal reactions such as such as methanol-fueled CLC, in order to improve reaction efficiency, it is necessary to react while removing anti-
Should be hot, removed both at home and abroad in some big methanol devices with such as Lurgi shell-and-tubes methanol column with shell side water in reaction tube at present
Reaction heat, because the byproduct steam tower cooler area of this pipe apparatus with catalyst inside is big, shell-and-tube is one cubic metre of catalysis than huyashi-chuuka (cold chinese-style noodles)
Agent heat exchange area is up to more than 100 square metres, it is difficult to improves again (see Terry Fitzpatrich, methanol synthesis
Options as feedstocaschange, Finds number3 2007).Therefore use and improve into tower tolerance and gas line
Speed, prevent from reacting " overtemperature " and " temperature runaway " in time to take outside tower reaction heat out of, need to be more than for this using up to 5~10 times
The circulating air (i.e. recycle ratio) of unstripped gas is otherwise strong anti-caused by fast reaction come effective gas such as CO in reducing into synthetic tower gas
Heat is answered to inactivate catalyst overheating, but high recycle ratio needs to increase the equipment and pipeline investment of corresponding methanol-fueled CLC circle,
And increase power and energy consumption.It is that raw material is used made from Shell coal gasifications or Texaco coal water slurry gasifications that calculating, which shows with coal,
Synthesis gas, using low circulation than when go out the methanol content of synthetic tower up to more than 30%, and existing typical methanol-fueled CLC exhaust gas
Middle methanol content only has 5% or so, difficulty and investment of the high circulation than adding commercial plant maximization.
The content of the invention
The task of the present invention is the shortcomings that overcoming prior art, passes through the structure innovation of reactor, there is provided one kind has height
Move heat energy power, realize low circulation than, high-carbon than the energy-efficient equipment under unstripped gas, the high net value of high synthetic ratio.
The present invention realizes purpose by following technical proposal：A kind of heat transfer reactor of Anti-temperature difference stress, including housing
And heat exchanging piece, described heat exchanging piece include some heat exchanger tubes, catalyst is housed between described heat exchanger tube, the housing be provided with into
Gas port, gas outlet, manhole and catalyst unload outlet, and described heat exchanging piece also includes being provided with one or more pairs of headers with tube sheet,
Described header includes inlet header and outlet header；The bottom of heat exchanger tube described in Internal and external cycle or together circle footpath are adjacent two is by U
Shape elbow connects, and the up heat exchanger tube and descending heat exchanger tube arrangement of heat transferring medium is led in composition, described up heat exchanger tube is with going out
Mouth header connection, described descending heat exchanger tube are connected with inlet header；Either：Internal and external cycle or the top with the heat exchanger tube for enclosing footpath
Connected by inverted U-shaped elbow, the up heat exchanger tube of inverted U-shaped elbow connection is connected with inlet header, descending heat exchanger tube and outlet header
Connection.Described heat transferring medium can be water or conduction oil.
Described outlet header is segmented into multiple, or inlet header and outlet header all can be in a symmetrical arrangement, such as 2
It is individual or 4 or 6 etc..
As a preferred embodiment, air inlet and gas outlet described on housing is connected to gas distributor.Described enters
The position of gas port and gas outlet can have two kinds of arrangements, when described air inlet is located at case top, described gas outlet
During positioned at housing bottom, through air inlet gas distributor, the catalyst bed outside pipe flows gas from top to bottom into axial direction；Or
Housing central section bilateral sets symmetrical air inlet and gas outlet, and gas is through the gas distribution grid in the cylinder of both sides and porous gas collection
Plate, catalyst bed radially crosses catalyst bed laminar flow outside pipe.
It is provided with as a kind of preferred scheme, in described housing around pipe shaft core, same return bend or the connection of inverted U-shaped elbow
Up heat exchanger tube and descending heat exchanger tube along around pipe shaft core respectively each by the left and axial arranged into reverse acting spiral shape to the right.Institute
For the heat exchanger tube stated to be less than 60 degree of windings with horizontal plane angle, optimal is the winding side of adjacent two layers set of heat exchange tubes less than 35 degree
To opposite.
Be additionally provided with the shell of flanged connection end socket as a kind of preferred scheme, outside described housing, described shell with
Heat transferring medium chuck is formed between housing, described inlet header passes through heat transferring medium chuck and heat transferring medium inlet communication, outlet
Header does not connect with heat transferring medium chuck, its top and the heat transferring medium outlet through shell and housing.
Outer wall spacing between the pipe of inside and outside different circle footpath heat exchanger tubes is preferably use catalyst particle size 2~8 times, optimal to be
3~5 times.
In the heat transfer reactor of the present invention, air inlet-outlet-housing is not limited to housing side, also can be on end socket or in end socket, even
The tube sheet for connecing heat exchanger tube can be flat board, ring arc, concave shaped or spirogyrate.
The present invention heat transfer reactor can more serial or parallel connections be applied in combination, can also with air cooling reactor or around
Pipe air cooling reactor or horizontal water pipe reactor form combined reactor to meet large-scale reaction unit needs.Described heat exchange is anti-
Answer device with air cooling reactor tandem be combined into large-scale reactor combined unit when, the shell side outlet of described heat transfer reactor
The shell side air inlet of the gentle cold reactor of mouth links, shell side of the air cooling reactor tube side gas outlet with water cooling around pipe reactor
Air inlet links.Described heat transfer reactor around pipe air cooling reactor tandem with being combined into large-scale reactor combined unit
When, the shell side gas outlet of described heat transfer reactor and the shell side air inlet around pipe air cooling reactor link, described to be gas-cooled around pipe
The tube side gas outlet of reactor and the shell side air inlet of described heat transfer reactor link.Described heat transfer reactor and horizontal water
When cold reactor tandem is combined into large-scale reactor combined unit, the shell side gas outlet of heat transfer reactor and Horizontal water cooling are anti-
The shell side air inlet of device is answered to connect.
The heat transfer reactor of the present invention can be widely applied to close in gas-liquid hydrocarbon such as methanol-fueled CLC, methane synthesis F- T synthesis
Into, ammonia synthesis, H2S aoxidizes the strong exothermal reactions such as sulphur processed or natural gas or methane change into H2、CO、CO2Synthesis gas, methanol
Decomposition H2, the endothermic reaction such as RFCC.
The present invention has following obvious advantage than prior art：
1. linking adjacent up-downgoing pipe with return bend, being designed with header up and down than prior art reduces the leakage of half joint
Possibility, and reduce manufacturing expense.
2. between being mounted in cold pipe because of catalyst, therefore adding packing factor, reach more than 60%, and German Lurgi shell-and-tubes first
Alcohol reactor catalyst is in pipe, and packing factor is only up to 30%.
3. can be big using 10mm Diameter Walls 1mm thin-walled tubule heat transfer coefficient, it can reach bigger than huyashi-chuuka (cold chinese-style noodles) simultaneously, conduct heat by force
The high good result with capacity utilization.Therefore the reactor volume of same yield greatly reduces, and investment greatlys save, while can
With increase length, expand catalyst loading amount and ability, the large-scale, ultra-large type that is particularly suitable for use in produces million tons of devices per year.
4. gas flowing on the one hand due to catalyst be mounted in pipe between increase flow area, and be due to high heat transfer coefficient and
Heat exchange area shifting heat energy power is strong, can drop synthesis recycle ratio, improves one way combined coefficient.Reactor resistance is greatly reduced, and saves dynamic
Power consumes.
5. gas transverse flows through heat exchanger tube in beds, cross-flow improves heat transfer coefficient and efficiency, reduces the temperature difference.
6. pipe exterior catalyst is integrally formed, filling is easily uniform.
7. because using heat exchanger tube is made around pipe, retractable, Anti-temperature difference stress effect is good, and structure is reliable.
8. flanged end socket can be used, the cold pipe group of interior end socket is extracted out outside housing, clears up cold pipe and handling catalyst side
Just.
Brief description of the drawings：
Fig. 1 is that have return bend, housing upper to set the heat transfer reactor structural representation of a pair of headers in the present invention.
Fig. 1 a are the process flow diagrams of the heat transfer reactor shown in Fig. 1.
Fig. 2 is that have inverted U-shaped elbow, lower housing portion to set the heat transfer reactor structural representation of a pair of headers in the present invention.
Fig. 2 a are the process flow diagrams of the heat transfer reactor shown in Fig. 2.
Fig. 3 is the heat transfer reactor structural representation that gas transverse flows in the present invention.
Fig. 4 is chlamydate heat transfer reactor structural representation in the present invention.
Fig. 5 is the heat transfer reactor water cooling shunting means schematic diagram of the present invention
Fig. 6 is air cooling reactor A and heat transfer reactor tandem arrangement schematic diagram of the present invention.
Fig. 6 a are around pipe air cooling reactor and heat transfer reactor tandem arrangement schematic diagram of the present invention.
Fig. 7 is heat transfer reactor and transverse horizontal water cooling tandem arrangement schematic diagram of the present invention.
Fig. 8 is return bend and the schematic diagram around pipe jointing part point in heat transfer reactor of the present invention.
Inverted U-shaped elbow and the schematic diagram around pipe jointing part point in Fig. 9 heat transfer reactors of the present invention.
Description of reference numerals：
The up descending heat exchanger tubes of heat exchanger tube 2b- of 1- housing 2- heat exchanger tubes 2a-
3- air inlet 4- manhole 5- gas outlets 6- catalyst unloads outlet
7- is around the porous gas collection plate 9a- inlet headers of pipe shaft core 81- gas distribution grids 82-
9b- outlet header 10- heat transferring medium chuck 11- shell 12- drums
13- circulating pump 14- steam outlet pipe 15- outlet pipe 16- heat transferring medium circulation pipes
17- heat transferring mediums supplement the inverted U-shaped elbow 19- longitudinal register plates of pipe 18a-U shape elbows 18b-
20- upper cover 21- heat transferring medium import 22- heat transferring mediums export 23- supporting members
Embodiment：
Embodiment 1
The heat transfer reactor of Anti-temperature difference stress as shown in Figure 1, including housing 1 and heat exchanging piece, the top of housing 1 are provided with
Air inlet 3 and manhole 4, air inlet 3 are furnished with gas distribution grid 81, and housing upper is provided with a pair of headers with tube sheet：Inlet header
9a and outlet header 9b.Described heat exchanging piece includes some heat exchanger tubes 2, Internal and external cycle or with circle footpath it is adjacent two described in heat exchanger tube
Bottom by return bend 18a connections (as shown in Figure 8), the up heat exchanger tube 2a of heat transferring medium and descending heat exchanger tube are led in composition
2b arranges that descending heat exchanger tube 2b connects with inlet header 9a, up heat exchanger tube 2a connects with outlet header 9b.Each layer heat exchanger tube by
Longitudinal register plate 19 positions.The inside center of housing 1 is additionally provided with around pipe shaft core 7, and the up heat exchanger tube of same return bend connection is with
Row heat exchanger tube along around pipe shaft core 7 respectively each counterclockwise or clockwise direction spirality arrangement, around the bottom of pipe shaft core 7
A bottom is supported on by supporting member 23, around the top retractable of pipe shaft core 7.The up heat exchanger tube of same return bend connection
It is opposite with the winding direction of descending heat exchanger tube.Housing bottom is provided with gas outlet 5 and catalyst unloads outlet 6, and gas outlet 5 is equipped with porous
Gas collection plate 82.Heat transferring medium uses water.
Above-mentioned heat transfer reactor in use, Catalyst packing between pipe, as shown in Figure 1a, outlet header 9b is gone out by steam
Mouth pipe 14 connects drum 12, and drum 12 connects circulating pump 13 by outlet pipe 15, and circulating pump 13 is also connected with supplementing water pipe 17, import
Header 9a connects circulating pump 13 by heat transferring medium circulation pipe 16.Reaction gas enters from air inlet 3, and heat transferring medium is from inlet header
9a is entered in each heat exchanger tube 2, descending with spiral shape along descending heat exchanger tube, then up heat exchanger tube is transferred to through return bend, with
The spiral shape direction opposite with down direction is up, is during which exchanged heat with the reaction gas axially across catalyst layer, part water in pipe
Steam is vaporizated into, the separate vapour of drum 12 with regulating valve, remaining water and the benefit from supplement water pipe 17 are gone through outlet header 9b
Water-filling is again introduced into inlet header 9a through the boosting of circulating pump 13 after converging and recycled.
Embodiment 2
The heat transfer reactor of Anti-temperature difference stress as shown in Figure 2, structure composition is same as Example 1, and difference is：Import
Header 9a and outlet header 9b is located at lower housing portion, and the top of adjacent two heat exchanger tubes 2 of Internal and external cycle or same circle footpath is by inverted U-shaped elbow
18b connections (as shown in Figure 9), up heat exchanger tube 2a and descending heat exchanger tube the 2b arrangement of heat transferring medium are led in composition, i.e., it is up to change
Heat pipe 2a is connected with inlet header 9a, descending heat exchanger tube 2b is connected with outlet header 9b.Work when above-mentioned heat transfer reactor uses
As shown in Figure 2 a, heat transferring medium cyclic process is same as Example 1 for skill flow.
Embodiment 3
The heat transfer reactor of Anti-temperature difference stress as shown in Figure 3, the structure composition for the internals that exchange heat is same as Example 1, enters
Also with embodiment 1, difference is for mouth header 9a and outlet header 9b position：Air inlet 3 and gas outlet 5 are located at housing central section pair
Claim arrangement, air inlet 3 connects housing 1 and gas distribution grid 81, the connected porous gas collection plate 82 in gas outlet 5 and housing 1, reaction gas from
Air inlet 3 is uniformly distributed into catalyst layer through gas distribution grid 81, and reaction gas flows laterally through catalyst layer to opposite side
Porous gas collection plate 82, then gone out from gas outlet 5.Above-mentioned heat transfer reactor is in use, its heat transferring medium cyclic process and implementation
Example 1 is identical.
Above-mentioned Fig. 1 to Fig. 3 can use bolt by removable cover plate and connection without the header of the heat transfer reactor of the present invention of shell
Box body activity fit sealing, cover plate need to be only pulled down during to overhaul.
Embodiment 4
The heat transfer reactor of Anti-temperature difference stress as shown in Figure 4, heat exchanging piece is same as Example 1, and distinctive points are：Described
The shell 11 with upper cover 20 is additionally provided with outside housing, described upper cover 20 is fixedly connected with shell 11 with flange.Described is outer
Heat transferring medium chuck 10 is formed between shell 11 and housing 1, the heat transferring medium flowed in heat transferring medium chuck, which equally rises, to be removed in internals
Reaction heat, and housing is kept lower temperature.Inlet header 9a and outlet header 9b is located at housing upper, wherein inlet header 9a
Connected by heat transferring medium chuck 10 with heat transferring medium import 21, outlet header 9b does not connect with heat transferring medium chuck 10, thereon
Portion connects with through the heat transferring medium outlet 22 of shell 11, housing 1.
Upper cover 20 is provided with air inlet 3, and gas outlet 5 is arranged at the bottom of housing 1 and catalyst unloads outlet 6, and heat transferring medium is from changing
Thermal medium inlet 21 enters, and arrives inlet header 9a through heat transferring medium chuck 10, distribution enters each heat exchanger tube 2.Outlet header 9b goes out
The heat transferring medium containing vapour come removes drum.Heat exchanger tube 2 arranged along around pipe shaft core 7 and straight at angle α with spiral wound, under
Capable heat exchanger tube is up to being turned to through return bend behind bottom, and up heat exchanger tube winding direction is opposite with descending heat exchanger tube.Each layer changes
Heat pipe is positioned by longitudinal register plate 19, and ectonexine is equipped with catalyst between pipe, can also be left in heat exchanger tube top dress 200mm again
Right appropriate high catalytic agent, can sink after catalyst reduction, reduce catalyst layer height.Air inlet 3 on upper cover 20 doubles as
Manhole, flange is taken apart during maintenance, repaired available for dress catalyst or enter for worker in tower, air inlet 3 and gas outlet 5 are equipped with
Gas distributor.Supporting member 23 is provided between shell 11 and housing 1.
Inlet header 9a and outlet header 9b can be set multigroup, such as 2~8 groups, be provided to load and unload the catalyst between pipe
It is convenient, manufacture is turned into feasible around the reactor that pipe number is more, diameter is big, housing side cloth bobbin carriage has been also convenient for maintenance.
There is flange to link housing and upper cover in Fig. 4, but flange can also not had to, and end socket is directly welded with casing cylinder
Connect.
The reactor of structure shown in the present embodiment is especially suitable for ammonia synthesis project and existing shell improvement cost invention knot
The reconstruction project of structure.
Embodiment 5
Fig. 5 is the combined reactor sketch that composes in parallel of heat transfer reactor of two playscripts with stage directions invention, the reaction of left and right two in figure
Device respectively comes with the drum and circulating pump of adjustable pressure for vaporization, such as 100m is respectively housed for methanol-fueled CLC, every reactor3
Catalyst, using water as heat transferring medium, by house steward L Lai pressure about 8MPa, temperature entering about 200 DEG C more tower gas be bisected into two tunnels difference
Reacted into the tower of left and right two, reaction heat is absorbed by the water in pipe produces steam, and Methanol Molar content reaches in reaction gas
10% is convergeed to house steward by outlet at bottom again goes heat exchange, refrigerated separation methanol product.Two reactors in the present embodiment also may be used
To fully enter left tower or right tower with tandem compound, the i.e. inlet gas from house steward, outlet at bottom reaction gas send the right side again after reaction
Tower or the reaction of left tower, then reactor outlet goes the cold separation that exchanges heat.It is that synthetic tower resistance is low using the advantages of the former two tower parallel connection
Saving energy, but two tower catalyst-assemblies highly need to be equal, and otherwise gas distribution is uneven, and the big tower of a tower is small, influences combined coefficient.
It is big using tower pressure drop during the latter's cascade towers, but the distribution of two tower gases can be avoided uneven, and the tower of the latter two respectively has independent regulation
The drum of temperature, can be according to the activity of two tower catalyst, and section temperature is in the hope of realizing optimum response before and after separately adjustable course of reaction
Lower reaction.
Embodiment 6
As shown in fig. 6, air cooling heat transfer reactor B and the combination unit figure around pipe-type water-cooling heat transfer reactor A of the present invention,
Be gas-cooled heat transfer reactor B the visible the applicant of detailed construction the patent of invention of mandate " internal heat catalytic reaction method and
Fig. 2 or Fig. 3 in equipment (ZL200310121904.1) ", about 100 DEG C of reaction gases enter heat exchange from air cooling heat transfer reactor B bottoms
Tube bank sucting reaction heat is heated to more than 200 DEG C, then is entered from the present invention around pipe-type water-cooling heat transfer reactor A imports and occurred instead
Should, reaction heat by pipe water absorb produce steam, reaction gas (such as carry out synthesizing methanol reaction, Methanol Molar content of about
10%, temperature is more than 230 DEG C) go out enter to be gas-cooled heat transfer reactor B shell side air inlets around pipe-type water-cooling heat transfer reactor A again, it is being gas-cooled
For heat transfer reactor B catalyst layer further after reaction, Methanol Molar content about 13%, reaction gas goes out air cooling heat exchange reaction again
Device B.
By taking the methanol synthesis reaction of strong exothermal reaction as an example, using water as heat transferring medium, 1,600,000 tons big methanol dress is produced per year
Put and use combinations thereof device, synthesis pressure 8.2MPa, 4 meters of air cooling heat transfer reactor B internal diameters, dress domestic catalyst 110m3, around
4 meters of pipe-type water-cooling heat transfer reactor A internal diameters, dress domestic catalyst 100m3, material gas quantity 476000Nm3/ h, with circulating air
724000Nm3/ h converges rear 1200000Nm3/ h tolerance, about 100 DEG C of temperature are entered to be gas-cooled absorbing reaction heat in the cold pipes of heat transfer reactor B
About 220 DEG C of heating goes out tower, enters and is reacted around pipe-type water-cooling heat transfer reactor A, around pipe-type water-cooling heat transfer reactor A catalyst focus temperature
Degree is raised to 249 DEG C, and reaction heat heating water in pipe produces steam, and reaction gas is to around pipe-type water-cooling heat transfer reactor A bottom temps
235 DEG C, Methanol Molar content 11.5% in reaction gas, go out and enter around pipe-type water-cooling heat transfer reactor A on air cooling heat transfer reactor B
The further synthesizing methanol of tower is entered in portion, reaction heat heat adverse current inlet tower gas in cold pipe make in cold pipe temperature of about 220 DEG C of outlets go around
Pipe-type water-cooling heat transfer reactor A, air cooling heat transfer reactor B manage outer reaction gas temperature and drop to 205 DEG C, and methanol is raised in reaction gas
16.16%, tolerance 905564Nm3/ h, the heat transfer reactor B that goes out to be gas-cooled send to refrigerated separation methanol, the smart yield of alcohol 210 in product
Ton/when, material balance see the table below.
Above-mentioned air cooling heat transfer reactor B can also use air cooling as shown in Figure 6 a instead around pipe reactor C, and described air cooling is around pipe
The housing upper of reactor is provided with one or more outlet header 9b, and lower housing portion is provided with one or more inlet header 9a, its
Remaining structure is passed through low-temp reaction gas with embodiment 1 in inlet header 9a, through heat exchanger tube 2 with managing the reaction gas in outer catalyst layer
Reverse heat-exchange, go out reactor from outlet header 9b after gas converting heat and remove the shell side air inlet around pipe-type water-cooling heat transfer reactor A, go out
Reaction gas around pipe-type water-cooling heat transfer reactor A shell side gas outlet enters shell side air inlet of the air cooling around pipe reactor C.
Embodiment 7
Fig. 7 is Horizontal water cooling reactor D with the present invention around pipe type heat transfer reactor A tandem compound reactor sketch, instead
Should gas advanced heat transfer reactor A reactions, heat transfer reactor of the invention used around pipe, and heat exchange area is big, and it is strong to move heat energy power, can be with
Meet that reaction reaction heat early stage is big, fully remove reaction heat, avoid catalyst overheating from inactivating, connected after pipe type heat transfer reactor
Horizontal tower, Horizontal water cooling reactor D and visible the applicant of structure authorized entitled " transverse pipe type heat transfer equipment " are (specially
Profit number is ZL200410103104) patent of invention.Horizontal water cooling reactor D gas transverse flowing catalytic bed circulating face
Greatly, catalyst bed height is vertical around pipe tower is low, resistance is small, is combined with before and after pipe water-cooling tower, can reach good reaction
Effect, resistance is reduced again, reduces energy consumption.
The heat transfer reactor of the present invention used in the embodiment of the present invention 5,6,7 is with chlamydate structure, can also use such as
The heat transfer reactor of the present invention without shell shown in Fig. 1,2,3.
Subject of the present invention is fully described above by each embodiment of numerous legends, but is not limited to these contents,
Such as air inlet-outlet-housing is not limited to housing side, heat exchanger tube on end socket or in end socket, also can be connected tube sheet can be flat board,
Ring arc, concave shaped or spirogyrate.With multiple tops, the small tube sheet in bottom heat-transfer pipe can also be connected with interior end socket；Heat exchange reaction
During device loading catalyst, can the heat insulation layer of certain altitude be also set around pipe top or bottom.
Claims (7)
1. a kind of heat transfer reactor of Anti-temperature difference stress, including housing and heat exchanging piece, described heat exchanging piece includes some heat exchanger tubes,
Catalyst is housed, the housing unloads outlet provided with air inlet, gas outlet, manhole and catalyst, and it is special between described heat exchanger tube
Sign is：Described heat exchanging piece also includes being provided with one or more pairs of headers with tube sheet, described header include inlet header with
Outlet header；Internal and external cycle or with circle footpath it is adjacent two described in the bottom of heat exchanger tube connected by return bend, heat exchange is led in composition and is situated between
The up heat exchanger tube of matter and descending heat exchanger tube arrangement, described up heat exchanger tube are connected with outlet header, described descending heat exchange
Pipe is connected with inlet header, and heat transferring medium is entered in each heat exchanger tube from inlet header, along descending heat exchanger tube with spiral shape
OK, then through return bend up heat exchanger tube is transferred to from bottom to top；Internal and external cycle or with circle footpath it is adjacent two described in heat exchanger tube top
Portion is connected by inverted U-shaped elbow, and the up heat exchanger tube that inverted U-shaped elbow connects is connected with inlet header, descending heat exchanger tube joins with outlet
Case connects；It is provided with described housing around pipe shaft core, the up heat exchanger tube and descending heat exchanger tube of same return bend connection are along around pipe
Shaft core is respectively each by axial arranged into reverse acting spiral shape to the left or to the right；Described heat exchanger tube with horizontal plane angle be less than 60
Degree winding, the winding direction of adjacent two layers set of heat exchange tubes are opposite；
Described air inlet and gas outlet is connected with gas distributor, and described air inlet is located at case top, described outlet
Mouth is located at housing bottom.
2. the heat transfer reactor of Anti-temperature difference stress as claimed in claim 1, it is characterised in that：Described air inlet and gas outlet
Set positioned at housing central section Bilateral Symmetry, described air inlet and gas outlet are connected with gas distributor.
3. the heat transfer reactor of the Anti-temperature difference stress as described in claim 1-2 is any, it is characterised in that：Outside described housing also
Provided with the shell with end socket, heat transferring medium chuck, described inlet header and heat transferring medium are formed between described shell and housing
Chuck connects, described outlet header and heat transferring medium outlet.
A kind of 4. combination unit of heat transfer reactor using Anti-temperature difference stress as claimed in claim 1, it is characterised in that：By
Respectively come with the heat transfer reactor tandem described in more of drum or compose in parallel.
A kind of 5. combination unit of heat transfer reactor using Anti-temperature difference stress as claimed in claim 1, it is characterised in that：By
Described heat transfer reactor is composed in series with air cooling reactor or around pipe air cooling reactor or Horizontal water cooling reactor；Described changes
Thermal reactor with around pipe air cooling reactor tandem be combined into large-scale reactor combined unit when, described heat transfer reactor
Shell side gas outlet and the shell side air inlet link around pipe air cooling reactor, it is described around the tube side gas outlet of pipe air cooling reactor and institute
The shell side air inlet for the heat transfer reactor stated links；Described heat transfer reactor is combined into Horizontal water cooling reactor tandem
During large-scale reactor combined unit, the shell side gas outlet of heat transfer reactor connects with the shell side air inlet of Horizontal water cooling reactor.
A kind of 6. heat transfer reactor the answering in strong exothermal reaction or the endothermic reaction of Anti-temperature difference stress as claimed in claim 1
With.
7. application of the heat transfer reactor of Anti-temperature difference stress as claimed in claim 6 in strong exothermal reaction or the endothermic reaction,
It is characterized in that：Described strong exothermal reaction is methanol-fueled CLC, methane synthesis, F- T synthesis or H2S aoxidizes sulfur reaction processed, institute
The endothermic reaction stated is that natural gas or methane change into H2、CO、CO2Synthesis gas, Methanol Decomposition H2Or RFCC is anti-
Should.
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| CN201210033806.1A CN103240036B (en) | 2012-02-14 | 2012-02-14 | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application |
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| CN103752225B (en) * | 2014-01-04 | 2015-06-10 | 衢州昀睿工业设计有限公司 | Self-circulating synthesis reactor with double rising kinetic energy |
| CN105642197A (en) * | 2014-09-24 | 2016-06-08 | 楼韧 | Large-sized reactor, and device and process thereof |
| CN105462640B (en) * | 2015-12-03 | 2018-06-29 | 合肥通用机械研究院 | A kind of deep cooling hydrocarbon material denitrogenation tower top condensing unit |
| US11260357B2 (en) | 2017-12-21 | 2022-03-01 | Uop Llc | Process and apparatus for fluidizing a catalyst bed |
| CN108954360A (en) * | 2018-06-08 | 2018-12-07 | 浙江涌原新能科技股份有限公司 | A kind of novel energy-saving environment-friendly device |
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| CN1600412A (en) * | 2003-09-22 | 2005-03-30 | 上海兖矿能源科技研发有限公司 | Contiuous industrial reactor of slurry state bed in gas, liquid and solid three phases |
| CN202460592U (en) * | 2012-02-14 | 2012-10-03 | 杭州林达化工技术工程有限公司 | Temperature stress resistant heat transfer reactor and composite device thereof |
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