CN202460592U - Temperature stress resistant heat transfer reactor and composite device thereof - Google Patents
Temperature stress resistant heat transfer reactor and composite device thereof Download PDFInfo
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- CN202460592U CN202460592U CN2012200487540U CN201220048754U CN202460592U CN 202460592 U CN202460592 U CN 202460592U CN 2012200487540 U CN2012200487540 U CN 2012200487540U CN 201220048754 U CN201220048754 U CN 201220048754U CN 202460592 U CN202460592 U CN 202460592U
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Abstract
The utility model discloses a temperature stress resistant heat transfer reactor, which comprises a shell and a heat exchange piece, wherein the shell is provided with an air inlet, an air outlet, a manhole and a catalyst discharge hole; the heat exchange piece comprises a plurality of heat exchange pipes and one pair or multiple pairs of headers with pipe plates, wherein the heat exchange pipes are spirally and axially wound along a wound pipe central spindle; and two adjacent heat exchange pipes on an inner ring and outer ring or with the same ring diameter are connected by a U-shaped bend or an inverse U-shaped bend. Multiple heat transfer reactors disclosed by the utility model can be combined by being connected in series or in parallel, or the heat transfer reactor and an air-cooled reactor, or a wound pipe air-cooled reactor or a horizontal water pipe reactor form a joint reactor so as to satisfy the requirement of a large reaction device. The heat transfer reactor disclosed by the utility model can be widely applied to various types of strong heat release reaction or heat adsorption reaction. The heat transfer reactor disclosed by the utility model adopts a wound pipe type heat exchange pipe connected by the U-shaped bend, can be freely flexible, has a reliable structure and is especially suitable for large and ultra-large devices of million tons of annual output, the joint leakage possibility is lowered, a catalyst filling coefficient is high, and the equipment investment is greatly saved.
Description
Technical field
The utility model relates to the catalytic reaction device of field of chemical engineering, is used for fluid catalytic reaction and diabatic process, relates in particular to a kind of synthesizing methanol, dimethyl ether, methanation, F-T reaction, H of being applicable to
2The heat transfer reactor and the composite set thereof of strong heat release such as S oxidation, ammonia synthesis or endothermic reaction process.
Background technology
China's Coal Chemical Industry develops rapidly in recent years; Country brings up to single cover to the scale of newly-built methanol device and produces per year more than 1,000,000 tons; The conversion of natural gas gas that the unstripped gas of synthesizing methanol abroad adopts before also scarcely being, but producing synthesis gas from coal, C/Hratio significantly improves in the synthetic raw gas; The reaction heat that causes the per unit product is up to more than 2 times, and this proposes huge challenge for the maximization of methanol device.
Wait some strong exothermal reactions for synthesizing like methyl alcohol; In order to improve reaction efficiency; Need shift out reaction heat simultaneously in reaction, remove the reaction heat in the reaction tube with for example Lurgi shell-and-tube methanol column with shell side water in some big methanol devices both at home and abroad at present, because the byproduct steam tower cooler area of this pipe apparatus with catalyst inside is big; Shell-and-tube is that one cubic metre of catalyst heat exchange area is up to more than 100 square metres than huyashi-chuuka (cold chinese-style noodles); Be difficult to improve again (seeing Terry Fitzpatrich, methanol synthesis options as feedstocas change, Finds number3 2007).Therefore adopt and improve tower tolerance and gas linear velocity; Prevent reaction " overtemperature " and " temperature runaway " outward so that in time take reaction heat out of tower; Need adopt up to 5～10 times of circulating air (being recycle ratio) for this reason and reduce in the synthetic tower gas effectively gas such as CO more than unstripped gas; Otherwise the strong reaction heat that fast reaction produces can make the catalyst overheating inactivation, but high recycle ratio need increase the equipment and the pipeline investment of corresponding methyl alcohol circle synthesis, and increases power and energy consumption.Calculating shows the synthesis gas that uses coal to use Shell coal gasification or Texaco coal water slurry gasification to make as raw material; Adopt the methanol content that goes out synthetic tower when hanging down recycle ratio can reach more than 30%; And methanol content has only about 5% in the synthetic exhaust gas of existing typical methyl alcohol, and high recycle ratio has increased difficulty and investment that commercial plant maximizes.
The utility model content
The task of the utility model is the shortcoming that overcomes prior art, through the structure innovation of reactor, provides a kind of and has height and move heat energy power, realize that low recycle ratio, high-carbon are than the energy-efficient equipment under unstripped gas, the high net value of high synthetic ratio.
The utility model is realized purpose through following technical proposal: a kind of heat transfer reactor of temperature resistance difference stress; Comprise housing and heat exchanging piece; Described heat exchanging piece comprises some heat exchanger tubes, between described heat exchanger tube catalyst is housed, and said housing is provided with air inlet, gas outlet, manhole and catalyst and unloads outlet; Described heat exchanging piece also comprises the one or more pairs of headers that are provided with the band tube sheet, and described header comprises inlet header and outlet header; The bottom of the adjacent two described heat exchanger tubes of Internal and external cycle or same circle footpath is connected by return bend; The up heat exchanger tube of logical heat transferring medium and descending heat exchanger tube are arranged in constituting; Described up heat exchanger tube is connected with outlet header, and described descending heat exchanger tube is connected with inlet header; Or: the top of the heat exchanger tube in Internal and external cycle or same circle footpath 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 is connected with outlet header.Described heat transferring medium can be water or conduction oil.
Described outlet header can be divided into a plurality of, and perhaps inlet header and outlet header all can be in a symmetrical arrangement, for example 2 or 4 or 6 etc.
As a kind of preferred, the above air inlet and gas outlet of housing is connected with gas distributor respectively.Can there be two kinds of arrangements the position of described air inlet and gas outlet, when described air inlet be positioned at case top, when described gas outlet is positioned at housing bottom, gas becomes axially mobile through the air inlet gas distributor from top to bottom at the outer catalyst bed of pipe; Perhaps bilateral is provided with the air inlet and the gas outlet of symmetry at housing middle part, gas distribution grid and the porous gas collection plate of gas in the cylindrical shell of both sides, and it is mobile radially to cross beds at the outer catalyst bed one-tenth of pipe.
As a kind of preferred version, be provided with in the described housing around the tubular axis core, the up heat exchanger tube that same return bend or inverted U-shaped elbow connect and descending heat exchanger tube along around the tubular axis core respectively separately by left with become the reverse acting spiral oblique crank Z to layout to the right.Described heat exchanger tube is to twine less than 60 degree with horizontal plane angle, and optimum is that the winding direction of adjacent two layers set of heat exchange tubes is opposite less than 35 degree.
As a kind of preferred version; Described housing also is provided with the shell of flanged connection end socket outward; Constitute the heat transferring medium chuck between described shell and housing; Described inlet header is communicated with the heat transferring medium import through the heat transferring medium chuck, and outlet header is not communicated with the heat transferring medium chuck, and its top is communicated with the heat transferring medium outlet of passing shell and housing.
Outer wall spacing between the pipe of inside and outside different circles footpath heat exchanger tube is preferably 2～8 times that use catalyst particle size, and optimum is 3～5 times.
In the heat transfer reactor of the utility model, air inlet-outlet-housing is not limited to side, also can be on end socket or in the end socket, and the tube sheet that connects heat exchanger tube can be dull and stereotyped, ring arc, concave shaped or spirogyrate.
The utility model heat transfer reactor can many serial or parallel connections combination use, also can form combined reactor to satisfy large-scale reaction unit needs with the air cooling reactor or around pipe air cooling reactor or horizontal water pipe reactor.When series combination becomes large-scale reactor combined unit before and after described heat transfer reactor and the air cooling reactor; The shell side air inlet of the gentle cold reactor in shell side gas outlet of described heat transfer reactor links, and said air cooling reactor tube side gas outlet and water-cooled link around the shell side air inlet of pipe reactor.When described heat transfer reactor becomes large-scale reactor combined unit with series combination before and after pipe air cooling reactor; The shell side gas outlet of described heat transfer reactor and link around the shell side air inlet of pipe air cooling reactor, said around the tube side gas outlet of pipe air cooling reactor and the shell side air inlet binding of described heat transfer reactor.During the synthetic large-scale reactor combined unit of series, the shell side gas outlet of heat transfer reactor and the shell side air inlet of horizontal water-cooled reactor are connected before and after described heat transfer reactor and the horizontal water-cooled reactor.
Gas-liquid hydrocarbon such as that the heat transfer reactor of the utility model can be widely used in is synthetic in methyl alcohol, the synthetic Fischer-Tropsch of methane is synthetic are synthetic, ammonia synthesis, H
2Strong exothermal reactions such as S oxidation system sulphur or natural gas or methane conversion become H
2, CO, CO
2Synthesis gas, Methanol Decomposition system H
2, the endothermic reaction such as RFCC.
The utility model has following obvious advantage than prior art:
1. link adjacent administration-management up and down with return bend, all be provided with header up and down than prior art and reduce half joint leakage possibility, and reduce manufacturing expense.
2. because of catalyst is contained between cold pipe, so increased packing factor, reach more than 60%, and German Lurgi shell-and-tube methanol reactor catalyst is contained in the pipe, packing factor only reaches 30%.
3. can adopt the thin-walled tubule heat transfer coefficient of 10mm diameter wall thickness 1mm big, can reach bigger simultaneously, conduct heat by force and the high good result of capacity utilization than huyashi-chuuka (cold chinese-style noodles).Therefore the reactor volume of same output greatly reduces, and investment is saved greatly, simultaneously available increase length, enlarge catalyst loading amount and ability, be particularly useful for large-scale, ultra-large type and produce 1000000 tons of devices per year.
Gas flow on the one hand since catalyst be contained in and increase flow area between pipe, and be since high heat transfer coefficient and heat exchange area to move heat energy power strong, synthetic recycle ratio can be fallen, raising one way combined coefficient.The reactor resistance significantly reduces, and practices thrift power consumption.
5. gas transverse flows through heat exchanger tube in the beds, and cross-flow improves heat transfer coefficient and efficient, reduces the temperature difference.
6. the outer dress of pipe catalyst becomes one, and filling is prone to evenly.
7. make heat exchanger tube owing to adopting around pipe, retractable, temperature resistance difference stress effect is good, reliable in structure.
8. can adopt flanged end socket, the cold pipe group of interior end socket is extracted out outside the housing, clear up cold pipe and loading and unloading convenient catalyst.
Description of drawings:
Fig. 1 has return bend, housing top that the heat transfer reactor structural representation of a pair of header is set in the utility model.
Fig. 1 a is the process flow diagram of heat transfer reactor shown in Figure 1.
Fig. 2 has inverted U-shaped elbow, lower housing portion that the heat transfer reactor structural representation of a pair of header is set in the utility model.
Fig. 2 a is the process flow diagram of heat transfer reactor shown in Figure 2.
Fig. 3 is the heat transfer reactor structural representation that gas transverse flows in the utility model.
Fig. 4 is a chlamydate heat transfer reactor structural representation in the utility model.
Fig. 5 is the heat transfer reactor water-cooled shunting means sketch map of the utility model
Fig. 6 is air cooling reactor A and the utility model heat transfer reactor tandem arrangement sketch map.
Fig. 6 a is around pipe air cooling reactor and the utility model heat transfer reactor tandem arrangement sketch map.
Fig. 7 is the utility model heat transfer reactor and horizontal horizontal water-cooled tandem arrangement sketch map.
Fig. 8 is a return bend and the sketch map that divides around pipe jointing part in the utility model heat transfer reactor.
Inverted U-shaped elbow and the sketch map that divides around pipe jointing part in Fig. 9 the utility model heat transfer reactor.
Description of reference numerals:
The descending heat exchanger tube of the up heat exchanger tube 2b-of 1-housing 2-heat exchanger tube 2a-
3-air inlet 4-manhole 5-gas outlet 6-catalyst unloads outlet
7-is around tubular axis core 81-gas distribution grid 82-porous gas collection plate 9a-inlet header
9b-outlet header 10-heat transferring medium chuck 11-shell 12-drum
13-circulating pump 14-steam outlet pipe 15-outlet pipe 16-heat transferring medium circulation pipe
The 17-heat transferring medium replenishes the inverted U-shaped elbow 19-of pipe 18a-U shape elbow 18b-longitudinal register plate
20-upper cover 21-heat transferring medium import 22-heat transferring medium outlet 23-supporting member.
The specific embodiment:
Embodiment 1
The heat transfer reactor of temperature resistance difference stress as shown in Figure 1; Comprise housing 1 and heat exchanging piece; Said housing 1 top is provided with air inlet 3 and manhole 4, and air inlet 3 is furnished with gas distribution grid 81, and housing top is provided with the header of a pair of band tube sheet: inlet header 9a and outlet header 9b.Described heat exchanging piece comprises some heat exchanger tubes 2; The bottom of the adjacent two described heat exchanger tubes of Internal and external cycle or same circle footpath connects (as shown in Figure 8) by return bend 18a; The up heat exchanger tube 2a of logical heat transferring medium and descending heat exchanger tube 2b arrange in constituting, and descending heat exchanger tube 2b is communicated with inlet header 9a, up heat exchanger tube 2a is communicated with outlet header 9b.Each layer heat exchanger tube is by longitudinal register plate 19 location.Housing 1 inside center also is provided with around tubular axis core 7; Up heat exchanger tube that same return bend connects and descending heat exchanger tube are along arranging by counter clockwise direction or clockwise direction spirality separately respectively around tubular axis core 7; At the bottom of tubular axis core 7 bottoms are bearing in through supporting member 23 tin, the retractable around the top of tubular axis core 7.The up heat exchanger tube that same return bend connects is opposite with the winding direction of descending heat exchanger tube.Housing bottom is provided with gas outlet 5 and unloads outlet 6 with catalyst, and gas outlet 5 is furnished with porous gas collection plate 82.Heat transferring medium adopts water.
When above-mentioned heat transfer reactor uses; Catalyst is seated between pipe; Shown in Fig. 1 a, outlet header 9b connects drum 12 through steam outlet pipe 14, and drum 12 connects circulating pump 13 through outlet pipe 15; Circulating pump 13 also connects additional water pipe 17, and inlet header 9a connects circulating pumps 13 through heat transferring medium circulation pipe 16.Reaction gas gets into from air inlet 3; Heat transferring medium enters into each heat exchanger tube 2 from inlet header 9a; Heat exchanger tube along descending is descending with spirality, changes up heat exchanger tube over to through return bend again, and is up with the spirality direction opposite with down direction; During this time with the reaction gas heat exchange of axially passing catalyst layer; The part water vapor is a steam in the pipe, removes drum 12 separate vapours with control valve through outlet header 9b, and all the other water get into inlet header 9a recycle once more with converging after circulating pump 13 boosts from the supplementing water of replenishing water pipe 17.
The heat transfer reactor of temperature resistance difference stress as shown in Figure 2; Structure is formed identical with embodiment 1; Difference is: inlet header 9a and outlet header 9b are positioned at lower housing portion; Internal and external cycle or connects (as shown in Figure 9) by inverted U-shaped elbow 18b with the top of adjacent two heat exchanger tubes 2 in circle footpath, the up heat exchanger tube 2a of logical heat transferring medium and descending heat exchanger tube 2b layout in constituting, promptly up heat exchanger tube 2a is connected with inlet header 9a, descending heat exchanger tube 2b is connected with outlet header 9b.Technological process when above-mentioned heat transfer reactor uses is shown in Fig. 2 a, and the heat transferring medium cyclic process is identical with embodiment 1.
The heat transfer reactor of temperature resistance difference stress as shown in Figure 3; The structure of heat exchange internals is formed identical with embodiment 1; Also with embodiment 1, difference is in the position of inlet header 9a and outlet header 9b: air inlet 3 is positioned at housing middle part symmetric arrangement with gas outlet 5, and air inlet 3 is communicated with housing 1 and gas distribution grid 81; Gas outlet 5 connected porous gas collection plates 82 and housing 1; Reaction gas evenly distributes through gas distribution grid 81 from air inlet 3 and gets into catalyst layers, and the reaction gas lateral flow is passed the porous gas collection plate 82 of catalyst layer to opposite side, 5 goes out from the gas outlet again.When above-mentioned heat transfer reactor used, its heat transferring medium cyclic process was identical with embodiment 1.
Above-mentioned Fig. 1 can not adopt bolt with removable cover plate and the movable fit sealing of header casing with the header of the utility model heat transfer reactor of shell to Fig. 3, gets final product so that only need pull down cover plate during maintenance.
The heat transfer reactor of temperature resistance difference stress as shown in Figure 4, heat exchanging piece is identical with embodiment 1, and distinctive points is: described housing also is provided with the shell 11 of band upper cover 20 outward, and described upper cover 20 is fixedly connected with shell 11 usefulness flanges.1 of described shell 11 and housing constitute heat transferring medium chuck 10, and the heat transferring medium that flows in the heat transferring medium chuck rises equally and removes reaction heat in the internals, and make housing keep lower temperature.Inlet header 9a and outlet header 9b are positioned at housing top; Wherein inlet header 9a is communicated with heat transferring medium import 21 through heat transferring medium chuck 10; Outlet header 9b is not communicated with heat transferring medium chuck 10, and its top is communicated with the heat transferring medium outlet 22 of passing shell 11, housing 1.
There is flange to link housing and upper cover among Fig. 4, but also can be without flange, and end socket and casing cylinder are directly welded.
The reactor of structure shown in the present embodiment is specially adapted to the reconstruction project of ammonia synthesis project and existing shell improvement cost utility model structure.
Fig. 5 is the combined reactor sketch that the heat transfer reactor of two playscript with stage directions utility models composes in parallel; Two reactors respectively carry the drum and the circulating pump of scalable pressure for vaporization about among the figure; It is synthetic for example to be used for methyl alcohol, and every reactor is equipped with the 100m3 catalyst, is heat transferring medium with water; By the next about 8MPa of pressure of house steward L; Temperature is about advancing 200 ℃ more tower gas divide equally be two the tunnel get into respectively about two towers react, reaction heat is absorbed generation steam by the water in pipe, the methyl alcohol molar content reaches 10% and converges to house steward again by outlet at bottom and go heat exchange, refrigerated separation methanol product in the reaction gas.Two reactors in the present embodiment also can be used tandem compound, and promptly the inlet gas from house steward all gets into left tower or right tower, and reaction back outlet at bottom reaction gas send right tower or the reaction of left tower again, and reactor outlet goes the cold separation of heat exchange then.The advantage that adopts the parallel connection of the former two towers is that the low energy consumption of synthetic tower resistance economizes, but two tower catalyst-assembly height need equate, otherwise that gas distributes is uneven, and the big tower of a tower is little, influences combined coefficient.The tower pressure drop is big when adopting the series connection of the latter's two towers; But can avoid two tower gas maldistributions; And the latter's two towers respectively have the drum of independent adjusting temperature, can be according to two tower activity of such catalysts, and the section temperature is reacted under the optimum response in the hope of realizing before and after the independent regulation course of reaction.
As shown in Figure 6; The composite set figure around tubular type water-cooled heat transfer reactor A of air cooling heat transfer reactor B and the utility model; Fig. 2 or Fig. 3 in the visible the applicant's of the detailed structure of air cooling heat transfer reactor B the mandate patent of invention " inner heat-exchange catalytic reaction method and apparatus (ZL200310121904.1) "; About 100 ℃ of reaction gases get into heat-exchanging tube bundle sucting reaction heat from air cooling heat transfer reactor B bottom and are heated to more than 200 ℃, react from getting into around tubular type water-cooled heat transfer reactor A import of the utility model again, and reaction heat is absorbed by water in pipe and produces steam; Reaction gas (for example carries out the synthesizing methanol reaction; It is about 10% that the methyl alcohol molar content reaches, and temperature is more than 230 ℃) go out again around the cold heat transfer reactor B of tubular type water-cooled heat transfer reactor A air inlet shell side air inlet, at the catalyst layer of air cooling heat transfer reactor B further after the reaction; The methyl alcohol molar content reaches 13% approximately, and reaction gas goes out air cooling heat transfer reactor B again.
Methyl alcohol synthetic reaction with strong exothermal reaction is an example, adopts water as heat transferring medium, produces 1600000 tons big methanol devices per year and adopts the combinations thereof device, synthesis pressure 8.2MPa, 4 meters of air cooling heat transfer reactor B internal diameters, dress domestic catalyst 110m
3, around 4 meters of tubular type water-cooled heat transfer reactor A internal diameters, dress domestic catalyst 100m
3, material gas quantity 476000Nm
3/ h is with circulating air 724000Nm
3/ h converges back 1200000Nm
3/ h tolerance; Absorption reaction heat heats up about 220 ℃ and goes out tower in the cold pipe of the temperature cold heat transfer reactor B of about 100 ℃ of air inlets, advances the reaction around tubular type water-cooled heat transfer reactor A, is raised to 249 ℃ around tubular type water-cooled heat transfer reactor A catalyst hot(test)-spot temperature; Reaction heat heating water generates steam in pipe; Reaction gas arrives around 235 ℃ of tubular type water-cooled heat transfer reactor A bottom temps, and methyl alcohol molar content 11.5% in the reaction gas goes out around tubular type water-cooled heat transfer reactor A entering air cooling heat transfer reactor B top and advances the further synthesizing methanol of tower; The interior adverse current inlet tower gas of reaction heat heats cold pipe makes the interior temperature of cold pipe reach about 220 ℃ of outlets and goes around tubular type water-cooled heat transfer reactor A; The outer reaction gas temperature of air cooling heat transfer reactor B pipe drops to 205 ℃, and methyl alcohol is raised to 16.16% in the reaction gas, tolerance 905564Nm
3/ h goes out air cooling heat transfer reactor B and sends to refrigerated separation methyl alcohol, and in smart pure 210 output ton/times in the product, material balance sees the following form.
Above-mentioned air cooling heat transfer reactor B also can use air cooling shown in Fig. 6 a instead around pipe reactor C; Described air cooling is provided with one or more outlet header 9b around the housing top of pipe reactor; Lower housing portion is provided with one or more inlet header 9a; All the other structures feed low-temp reaction gas with embodiment 1 in the inlet header 9a, the reaction gas reverse heat-exchange outside heat exchanger tube 2 and pipe in the catalyst layer; Go out reactor from outlet header 9b behind the gas converting heat and remove shell side air inlet, go out the cold shell side air inlet of reaction gas air inlet around pipe reactor C around the shell side gas outlet of tubular type water-cooled heat transfer reactor A around tubular type water-cooled heat transfer reactor A.
Fig. 7 be horizontal water-cooled reactor D and the utility model around pipe type heat transfer reactor A tandem compound reactor sketch; The advanced heat transfer reactor A reaction of reaction gas; The heat transfer reactor of the utility model adopts around pipe, and heat exchange area is big, and it is strong to move heat energy power; It is big to satisfy reaction reaction heat in early stage; Fully remove reaction heat, avoid the catalyst overheating inactivation, the horizontal tower of series connection behind the pipe type heat transfer reactor, the authorized name of the visible the applicant of horizontal water-cooled reactor D and structure is called the patent of invention of " transverse pipe type heat transfer equipment " (patent No. is ZL200410103104).The gas transverse of the horizontal water-cooled reactor D catalytic bed circulating face that flows is big, catalyst bed height vertical low around the pipe tower, resistance is little, with combination before and after the pipe water-cooling tower, can reach good reaction effect, reduce resistance again, cut down the consumption of energy.
The utility model heat transfer reactor that adopts among the utility model embodiment 5,6,7 is the structure that has shell, also can adopt as Fig. 1,2, shown in 3 not with the utility model heat transfer reactor of shell.
More than through each embodiment of numerous legends abundant description done in the theme of the utility model; But be not limited to these contents; For example air inlet-outlet-housing is not limited to side, also can be on end socket or in the end socket, and the tube sheet that connects heat exchanger tube can be dull and stereotyped, ring arc, concave shaped or spirogyrate.Can also use a plurality of tops, the little tube sheet in bottom and interior end socket to be communicated with heat-transfer pipe; During the heat transfer reactor loading catalyst, also can be at the heat insulation layer that certain altitude is set around pipe top or bottom.
Claims (7)
1. the heat transfer reactor of a temperature resistance difference stress; Comprise housing and heat exchanging piece; Described heat exchanging piece comprises some heat exchanger tubes, between described heat exchanger tube catalyst is housed, and said housing is provided with air inlet, gas outlet, manhole and catalyst and unloads outlet; It is characterized in that: described heat exchanging piece also comprises the one or more pairs of headers that are provided with the band tube sheet, and described header comprises inlet header and outlet header; The bottom of the adjacent two described heat exchanger tubes of Internal and external cycle or same circle footpath is connected by return bend; The up heat exchanger tube of logical heat transferring medium and descending heat exchanger tube are arranged in constituting; Described up heat exchanger tube is connected with outlet header, and described descending heat exchanger tube is connected with inlet header; Or Internal and external cycle or connects by inverted U-shaped elbow with the top of the adjacent two described heat exchanger tubes in circle footpath, the up heat exchanger tube of inverted U-shaped elbow connection is connected with inlet header, descending heat exchanger tube is connected with outlet header.
2. the heat transfer reactor of temperature resistance difference stress as claimed in claim 1 is characterized in that: described air inlet and gas outlet are connected with gas distributor, and described air inlet is positioned at case top, and described gas outlet is positioned at housing bottom.
3. the heat transfer reactor of temperature resistance difference stress as claimed in claim 1 is characterized in that: described air inlet and gas outlet are positioned at housing middle part bilateral and are symmetrical set, and described air inlet and gas outlet are connected with gas distributor.
4. the heat transfer reactor of temperature resistance difference stress as claimed in claim 1; It is characterized in that: be provided with in the described housing around the tubular axis core, the up heat exchanger tube that same return bend connects and descending heat exchanger tube along around the tubular axis core respectively separately by becoming the reverse acting spiral oblique crank Z to the left or to the right to layout.
5. like the heat transfer reactor of the arbitrary described temperature resistance difference stress of claim 1-4; It is characterized in that: described housing also is provided with the shell of band end socket outward; Constitute the heat transferring medium chuck between described shell and housing; Described inlet header is communicated with the heat transferring medium chuck, and described outlet header is communicated with the heat transferring medium outlet.
6. a composite set that utilizes the heat transfer reactor of temperature resistance difference stress as claimed in claim 1 is characterized in that: be made up of serial or parallel connection before and after many that respectively the carry drum described heat transfer reactors.
7. composite set that utilizes the heat transfer reactor of temperature resistance difference stress as claimed in claim 1 is characterized in that: be composed in series by described heat transfer reactor and air cooling reactor or around pipe air cooling reactor or horizontal water-cooled reactor; When described heat transfer reactor becomes large-scale reactor combined unit with series combination before and after pipe air cooling reactor; The shell side gas outlet of described heat transfer reactor and link around the shell side air inlet of pipe air cooling reactor, said around the tube side gas outlet of pipe air cooling reactor and the shell side air inlet binding of described heat transfer reactor; During the synthetic large-scale reactor combined unit of series, the shell side gas outlet of heat transfer reactor and the shell side air inlet of horizontal water-cooled reactor are connected before and after described heat transfer reactor and the horizontal water-cooled reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200487540U CN202460592U (en) | 2012-02-14 | 2012-02-14 | Temperature stress resistant heat transfer reactor and composite device thereof |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200487540U CN202460592U (en) | 2012-02-14 | 2012-02-14 | Temperature stress resistant heat transfer reactor and composite device thereof |
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| CN202460592U true CN202460592U (en) | 2012-10-03 |
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|---|---|---|---|
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103240036A (en) * | 2012-02-14 | 2013-08-14 | 杭州林达化工技术工程有限公司 | Temperature stress resistant heat transfer reactor and composite device and application thereof |
| CN107774201A (en) * | 2016-08-31 | 2018-03-09 | 楼韧 | A kind of reactor for optimizing temperature and its reaction process and application |
| EP3199231A4 (en) * | 2014-09-24 | 2018-08-01 | Ren Lou | Large reactor and device and process thereof |
| CN112691614A (en) * | 2019-10-22 | 2021-04-23 | 中石化广州工程有限公司 | Integral type reaction indirect heating equipment |
-
2012
- 2012-02-14 CN CN2012200487540U patent/CN202460592U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103240036A (en) * | 2012-02-14 | 2013-08-14 | 杭州林达化工技术工程有限公司 | Temperature stress resistant heat transfer reactor and composite device and application thereof |
| CN103240036B (en) * | 2012-02-14 | 2018-02-16 | 杭州林达化工技术工程有限公司 | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application |
| EP3199231A4 (en) * | 2014-09-24 | 2018-08-01 | Ren Lou | Large reactor and device and process thereof |
| CN107774201A (en) * | 2016-08-31 | 2018-03-09 | 楼韧 | A kind of reactor for optimizing temperature and its reaction process and application |
| CN112691614A (en) * | 2019-10-22 | 2021-04-23 | 中石化广州工程有限公司 | Integral type reaction indirect heating equipment |
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