CN202747831U - Spiral coil heat exchanger and reactor with heat exchanger structure - Google Patents
Spiral coil heat exchanger and reactor with heat exchanger structure Download PDFInfo
- Publication number
- CN202747831U CN202747831U CN 201220234489 CN201220234489U CN202747831U CN 202747831 U CN202747831 U CN 202747831U CN 201220234489 CN201220234489 CN 201220234489 CN 201220234489 U CN201220234489 U CN 201220234489U CN 202747831 U CN202747831 U CN 202747831U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- reactor
- tube
- heat
- 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
Images
Landscapes
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The utility model discloses a spiral coil type heat exchanger which comprises an inlet header, an outlet header and a heat exchange internal part, wherein the heat exchanger internal part comprises a spiral coil shaft core and heat exchange pipes; the heat exchange pipes are arranged spirally along the spiral coil shaft core to form a plurality of heat exchange bundles which take the spiral pipe shaft core as a circle center and have different ring diameters; and two ends of each heat exchange pipe are respectively connected with the inlet header and the outlet header. The utility model further discloses a heat exchange reactor with the spiral coil heat exchanger structure. The heat exchange reactor can be independently used, or a plurality of heat exchange reactors are connected in series or in parallel; or the heat exchanger reactor with an air-cooled reactor, a spiral coil water cooled reactor or a horizontal water pipe reactor form a combined reactor. The heat exchanger has the characteristics of large heat transfer coefficient and high volume utilization rate; and the heat exchange reactor has the advantages of high heat transfer capability, low recirculating ratio, high-carbon-ratio feed gas, high synthetic ratio and high net value.
Description
Technical field
The utility model relates to the equipment of field of chemical engineering, is used for fluid catalytic reaction and diabatic process, relates in particular to a kind of heat exchanger that is applicable to refrigerating industry, and have this heat exchanger structure be applicable to synthesizing methanol, dimethyl ether, methanation, F-T reaction, H
2The strong heat release such as S oxidation, CO conversion, ammonia synthesis or CH
4, the endothermic reaction process such as hydro carbons, methanol decomposition reactor.
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, cause the reaction heat of per unit product up to more than 2 times, this proposes huge challenge for the maximization of methanol device.
Wait some strong exothermal reactions for synthesizing such as methyl alcohol, in order to improve reaction efficiency, need to shift out simultaneously reaction heat in reaction, at present both at home and abroad remove reaction heat in the reaction tube with Lurgi shell-and-tube methanol column for example with shell side water in some large methanol devices, because the byproduct steam tower cooler area of this pipe apparatus with catalyst inside is large, 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 and (see 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 in order in time reaction heat is taken out of tower, need adopt up to 5～10 times of circulating air more than unstripped gas (being recycle ratio) for this reason and reduce in the synthetic tower gas the effectively gas such as CO, otherwise the strong reaction heat that fast reaction produces can make the catalyst overheating inactivation, but high recycle ratio need to increase the e-quipment and pipe investment of corresponding methyl alcohol circle synthesis, and increases power and energy consumption.Calculating shows that with coal be the synthesis gas that raw material uses Shell coal gasification or Texaco coal water slurry gasification to make, the methanol content that goes out synthetic tower when adopting low recycle ratio can reach more than 30%, and methanol content only has 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
Task of the present utility model is the shortcoming that overcomes prior art, provides a kind of and moves that heat energy power is high, recycle ratio is low, high-carbon is than unstripped gas, synthetic ratio is high, net value is high high efficiency energy saving heat exchanging equipment and heat transfer reaction unit.
The utility model is realized purpose by following technical proposal:
A kind of wound tube heat exchanger, comprise inlet header, outlet header and heat exchange internals, described heat exchange internals comprise around tubular axis core and heat exchanger tube, described heat exchanger tube is along twining twist layout around the tubular axis core, form a plurality of take around the tubular axis core as the center of circle, the heat-exchanging tube bundle in different circles footpath, described heat exchanger tube two ends are connected with outlet header respectively at inlet header.
As a kind of preferred, described inlet header is 1, and described outlet header has at least 2 and be even number, is symmetrically and evenly and arranges.Described outlet header is provided with when a plurality of, and described heat exchanger tube one end is connected with a plurality of outlet headers respectively take heat-exchanging tube bundle as unit.
In the described heat exchange internals, the heat exchanger tube tube wall spacing of adjacent heat-exchanging tube bundle same level face is greater than the tube wall spacing of neighbouring heat exchanger tube in the same heat-exchanging tube bundle.
As a kind of preferred, the heat exchanger tube tube wall spacing of adjacent heat exchange tubes bundle same level face is greater than 2mm.
Described heat exchanger tube and horizontal plane angle be degree preferably≤35, and the winding direction of adjacent two layers heat-exchanging tube bundle is opposite.
Neighbouring heat exchanger tube tube wall spacing is preferably 0-5mm in the described same heat-exchanging tube bundle.
Described heat exchange tube diameter is preferably 10-30mm.
Heat transferring medium in the described heat exchanger tube is water or gas.When heat transferring medium is water in the described heat exchanger tube, byproduct steam after the heat absorption; When heat transferring medium was gas in the described heat exchanger tube, gas heated up after inlet header enters the heat exchanger tube heat absorption, goes out heat exchanger from outlet header.
When being hot gas in the described heat exchanger tube, the rear vaporization of liquid heat absorption that heat exchanger tube is outer, this moment, the utility model heat exchanger was as screw and vertical tube evaporator.
When be cold air in the described heat exchanger tube, the outer part higher boiling gas cold of the heat exchanger tube liquid that congeals into, this moment, the utility model heat exchanger was used as condenser.
A kind of around the pipe type heat transfer reactor, has a reactor shell, be provided with the as mentioned above heat exchanger of structure in it, loading catalyst between heat exchanger tube, described heat exchanger tube spacing is: the heat exchanger tube tube wall spacing of adjacent heat exchange tubes bundle same level face is 2～8 times of the catalyst particle size that uses, be preferably 3～5 times, be convenient to loading catalyst and scavenging duct outer wall between heat exchanger tube.
Be respectively cold and hot medium inside and outside the described heat exchanger tube, the reversible flow heat exchange also can be all from top to bottom and flow heat exchange.
Described reactor shell top is provided with pack into the manhole of usefulness of air inlet and catalyst, and the bottom is provided with catalyst and unloads outlet and gas outlet.
As a kind of preferred, described air inlet and gas outlet are respectively equipped with gas distributor and gas collector.
The position of described outlet header and inlet header is not limited to heat exchanger top and bottom, also can be in the side of heat exchanger or heat transfer reactor housing.
Heat transfer reactor of the present utility model can be used in combination by many serial or parallel connections, can form combined reactor to satisfy large-scale reaction unit needs with the air cooling reactor and around pipe water-cooled reactor or horizontal water pipe reactor when series connection is used.When described water-cooled heat transfer reactor becomes large-scale reactor combined unit with air cooling reactor front and back series combination, the shell side air inlet of the gentle cold reactor in shell side gas outlet of described water-cooled heat transfer reactor links, and described air cooling reactor tube side gas outlet and water-cooled link around the shell side air inlet of pipe reactor.
When adopting the heat exchange of water heat absorption vaporization producing steam in the heat exchanger tube, outlet header is connected with drum, the circulating pump with pressure-regulating valve, and the bottom inlet header connects circulating pump.
A kind ofly utilize aforesaid composite set around the pipe type heat transfer reactor, formed by serial or parallel connections before and after many described heat transfer reactors.
A kind ofly utilize aforesaid composite set around the pipe type heat transfer reactor, be composed in series by described heat transfer reactor and air cooling reactor or around pipe air cooling reactor or Horizontal water cooling reactor; Described heat transfer reactor is with when pipe air cooling reactor front and back series combination becomes large-scale reactor combined unit, the shell side gas outlet of described heat transfer reactor and link around the shell side air inlet of pipe air cooling reactor, described around the tube side gas outlet of pipe air cooling reactor and the shell side air inlet binding of described heat transfer reactor; When tandem compound becomes large-scale reactor combined unit before and after described heat transfer reactor and the Horizontal water cooling reactor, be connected the shell side air inlet and connect in the shell side gas outlet of heat transfer reactor with the Horizontal water cooling reactor.
The gas-liquid hydrocarbon such as that heat transfer reactor of the present 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
2The strong exothermal reactions such as S oxidation sulphur processed or natural gas or methane conversion become H
2, CO, CO
2Synthesis gas, Methanol Decomposition H processed
2, the heat exchange in the endothermic reaction such as RFCC and the refrigerating industry.
Heat exchanger of the present utility model and heat transfer reactor have following obvious advantage than prior art:
1. can adopt thin-walled tubule (for example diameter 15mm, wall thickness 1.5mm), heat transfer coefficient is large, can reach simultaneously larger than huyashi-chuuka (cold chinese-style noodles), conduct heat by force and the high good result of capacity utilization.Therefore the heat transfer reactor volume of same output greatly reduces, and investment is saved greatly, can enlarge catalyst loading amount and equipment capacity simultaneously, is particularly useful for large-scale, ultra-large type and produces 1000000 tons of devices per year.
2. the different circles of heat exchanger footpath has the space around between the heat exchange tube tube wall, steam or the unobstructed circulation of condensate liquid as evaporimeter or condenser the time, being convenient to vaporize, and be convenient to the scavenge pipe outer wall.When being heat transfer reactor, then be convenient to load and unload catalyst.
In the heat transfer reactor because 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%.
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, improve the one way combined coefficient, the reactor resistance significantly reduces, and saves 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. manage exterior catalyst and become one, filling easily evenly.
Description of drawings:
Fig. 1 a is heat exchanger structure schematic diagram of the present utility model, and wherein outlet header and inlet header are respectively in top and the bottom of heat exchanger.
Fig. 1 b is the another kind of structural representation of heat exchanger of the present utility model, and wherein outlet header and inlet header are respectively in the both sides of heat exchanger cylindrical shell.
Fig. 2 a is heat transfer reactor structural representation of the present utility model, and wherein outlet header and inlet header are respectively in top and the bottom of heat transfer reactor device.
Fig. 2 b is the another kind of structural representation of heat transfer reactor of the present utility model, and wherein outlet header and inlet header are respectively in the both sides of heat transfer reactor housing.
Process flow diagram when Fig. 3 is heat transfer reactor use of the present utility model.
Fig. 4 is the process flow diagram that heat transfer reactor of the present utility model is connected with the air cooling reactor and used.
Fig. 5 is the association response device sketch that the heat transfer reactor of two playscript with stage directions utility models composes in parallel.
Fig. 6 is Horizontal water cooling reactor and the tandem compound reaction unit sketch around the pipe type heat transfer reactor of the present utility model.
Description of reference numerals:
1-reactor shell 2-heat exchanger tube 3-air inlet 4-gas outlet
The 5-catalyst unload the outlet 6-around tubular axis core 7-gas distributor 8-around tubular axis core positioning strip
9a-inlet header 9b-outlet header 10-heat exchanger tube positioning strip 11-drum
12-circulating pump 13-gas collector 14-manhole 15-heat exchanger cylindrical shell
The specific embodiment:
Wound tube heat exchanger as shown in Figure 1a, comprise heat exchanger cylindrical shell 15, heat exchange internals, 1 inlet header 9a, 2 outlet header 9b, described heat exchange internals comprise some heat exchanger tubes 2 and around tubular axis core 6, described around tubular axis core 6 by being positioned at the heat exchanger inside center around tubular axis core positioning strip 8, described heat exchanger tube 2 is along twining twist layout around tubular axis core 6, and the winding direction of adjacent two layers heat exchanger tube is opposite.Described inlet header 9a is positioned at the bottom of heat exchanger cylindrical shell 15, and described outlet header 9b is positioned at the top of heat exchanger cylindrical shell 15 and is arranged symmetrically with.Described heat exchanger tube 2 lower ends are communicated with inlet header 9a, and heat exchanger tube 2 upper ends are divided into two bundles and are communicated with 2 outlet header 9b respectively.The top of heat exchanger cylindrical shell 15 also is provided with the air inlet 3 with gas distributor 7, and the bottom is provided with the gas outlet 4 with gas collector 13.
According to the difference of actual use occasion, the heat transferring medium in the heat exchanger tube is water or gas.Heat transferring medium heats up after inlet header enters the heat exchanger tube heat absorption in the heat exchanger tube, go out heat exchanger from outlet header, the outer heat transferring medium of heat exchanger tube enters from the air inlet 3 at heat exchanger top, goes out heat exchanger from gas outlet, bottom 4 after passing the interior heat transferring medium heat-shift of heat exchanger tube space outerpace and heat exchanger tube.。
Heat exchanger shown in Fig. 1 b comprises heat exchanger cylindrical shell 15, heat exchange internals, 1 inlet header 9a, 2 outlet header 9b, and in the both sides, top of heat exchanger cylindrical shell 15, all the other structures are with embodiment 1 respectively for outlet header 9b and inlet header 9a.
Shown in Fig. 2 a around the pipe type heat transfer reactor, comprise reactor shell 1, heat exchange internals, 1 inlet header 9a, 2 outlet header 9b, described reactor shell 1 top is provided with the manhole (not showing among Fig. 2 a) that outlet header 9b, air inlet 3 and the catalyst of packing into are used, air inlet 3 is furnished with gas distributor 7, and inlet header 9a is positioned at lower housing portion.Described heat exchange internals comprise some heat exchanger tubes 2 and around tubular axis core 6, described heat exchanger tube is along twining twist layout around tubular axis core 6, and by heat exchanger tube positioning strip 10 location, described heat exchanger tube 2 lower ends are communicated with inlet header 9a, and described heat exchanger tube 2 upper ends are communicated with outlet header 9b.Around tubular axis core 6 by being positioned at the enclosure interior center around tubular axis core positioning strip 8.The winding direction of adjacent two layers heat exchanger tube is opposite.Reactor shell 1 bottom is provided with also that catalyst unloads outlet 6 and with the gas outlet 4 of gas collector 13.The tube wall spacings of inside and outside different circle footpath heat exchanger tube are for using 5 times of catalyst particle size, and Catalyst packing is between pipe, and the heat transferring medium in the heat exchanger tube is water.
Process flow diagram when above-mentioned heat transfer reactor uses as shown in Figure 3, outlet header 9b connects the import of drum 11 and circulating pump 12 successively, inlet header 9a connects the outlet of circulating pump 12.Reaction gas enters from air inlet 3, enter catalyst layer through gas distributor 7, heat transferring medium distributes from inlet header 9a and enters into each heat exchanger tube, up with spirality along heat exchanger tube, during this time with the reaction gas heat exchange of axially passing catalyst layer, the part water vapor is steam in the heat exchanger tube, goes drum 11 separate vapours with control valve, all the other water and supplementing water to converge to boost by circulating pump 12 that again to enter inlet header 9a recycling through outlet header 9b.
Be depicted as the another kind of structural representation of heat transfer reactor of the present utility model such as Fig. 2 b, comprise manhole 14 that reactor shell 1, heat exchange internals, 1 inlet header 9a, 2 outlet header 9b, the catalyst of packing into use, with the air inlet 3 of gas distributor 7 with the gas outlet 4 of gas collector 13, its outlet header 9b and inlet header 9a are positioned at the both sides of heat transfer reactor housing, and all the other are with embodiment 3.
As shown in Figure 4, composite set figure around pipe type heat transfer reactor A and air cooling heat transfer reactor B of the present utility model, wherein around the structure of pipe type heat transfer reactor with embodiment 2, heat transferring medium in the heat exchanger tube is water, the detailed construction of air cooling heat transfer reactor B is identical with A, about 100 ℃ of reaction gases enter around heat exchange tube bundle sucting reaction heat around pipe heat transfer reactor B bottom from air cooling and are heated to more than 200 ℃, enter catalyst layer around pipe type heat transfer reactor A air inlet and react from of the present utility model again, reaction heat is absorbed by the water in the heat exchanger tube and produces steam, reaction gas (for example carries out the synthesizing methanol reaction, the methyl alcohol molar content reaches about 10%, temperature is more than 230 ℃) go out again around the cold heat transfer reactor B of pipe type heat transfer reactor A air inlet shell side air inlet, after the catalyst layer of air cooling heat transfer reactor B further reacts, the methyl alcohol molar content reaches 13% approximately, and reaction gas goes out air cooling heat transfer reactor B again.
Fig. 5 is the combined reactor sketch that the heat transfer reactor of two playscript with stage directions utility models composes in parallel, and two reactors respectively carry drum and the circulating pump of adjustable joint pressure for vaporization among the figure, and it is synthetic for example to be used for methyl alcohol, and every reactor is equipped with 100m
3Catalyst, take water as heat transferring medium, 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 enter respectively about two towers react, reaction heat is absorbed generation steam by the water in pipe, and the methyl alcohol molar content reaches 11% and converges to house steward by outlet at bottom again 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 namely the inlet gas from house steward all enters left tower or right tower, and the outlet at bottom reaction gas send right tower or the reaction of left tower again after the reaction, and then reactor outlet goes the heat exchange refrigerated separation.The advantage that adopts the former two tower parallel connections 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 large tower of a tower is little, affects combined coefficient.The tower pressure drop is large when adopting latter's cascade 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 the activity of two tower catalyst, and the section temperature is reacted under the optimum response in the hope of realizing before and after the independent conditioned reaction process.
Embodiment 7
Fig. 6 is Horizontal water cooling reactor C and the tandem compound reactor sketch around the pipe type heat transfer reactor A of the present utility model, the advanced heat transfer reactor A reaction of reaction gas, heat transfer reactor of the present utility model adopts around pipe, heat exchange area is large, it is strong to move heat energy power, it is large to satisfy reaction reaction heat in early stage, fully remove reaction heat, avoid the catalyst overheating inactivation, the horizontal tower of connecting behind the pipe type heat transfer reactor, the authorized name of visible the applicant of structure of Horizontal water cooling reactor C is called the patent of invention of " transverse pipe type heat transfer equipment " (patent No. is ZL200410103104).The gas transverse of the Horizontal water cooling reactor C catalytic bed circulating face that flows is large, 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 again resistance, reduce energy consumption.
Claims (10)
1. wound tube heat exchanger, comprise inlet header, outlet header and heat exchange internals, it is characterized in that: described heat exchange internals comprise around tubular axis core and heat exchanger tube, described heat exchanger tube is along twining twist layout around the tubular axis core, form a plurality of take around the tubular axis core as the center of circle, the heat-exchanging tube bundle in different circles footpath, described heat exchanger tube two ends are connected with outlet header with inlet header respectively.
2. wound tube heat exchanger as claimed in claim 1, it is characterized in that: described inlet header is one, described outlet header is more than 2 and is even number that described outlet header is symmetrically and evenly to be arranged.
3. wound tube heat exchanger as claimed in claim 1, it is characterized in that: the heat exchanger tube tube wall spacing of adjacent heat exchange tubes bundle same level face is greater than the tube wall spacing of neighbouring heat exchanger tube in the same heat-exchanging tube bundle.
4. wound tube heat exchanger as claimed in claim 1, it is characterized in that: the heat exchanger tube tube wall spacing of adjacent heat exchange tubes bundle same level face is greater than 2mm.
5. wound tube heat exchanger as claimed in claim 1 is characterized in that: described heat exchanger tube and horizontal plane angle twine less than 35 degree, and the winding direction of adjacent two layers heat-exchanging tube bundle is opposite.
6. wound tube heat exchanger as claimed in claim 1, it is characterized in that: neighbouring heat exchanger tube tube wall spacing is 0-5mm in the described same heat-exchanging tube bundle.
7. wound tube heat exchanger as claimed in claim 1 is characterized in that: the diameter of described heat exchanger tube is≤30mm.
8. one kind around the pipe type heat transfer reactor, it is characterized in that: have a reactor shell, be provided with in it such as the described heat exchanger of the arbitrary claim of claim 1-7, loading catalyst between described heat exchanger tube, described heat exchanger tube spacing is: the heat exchanger tube tube wall spacing of adjacent heat exchange tubes bundle same level face is 2～8 times of the catalyst particle size that uses.
9. one kind is utilized the composite set around the pipe type heat transfer reactor as claimed in claim 8, it is characterized in that: be comprised of serial or parallel connection before and after many described heat transfer reactors.
10. one kind is utilized the composite set around the pipe type heat transfer reactor as claimed in claim 8, it is characterized in that: be composed in series by described heat transfer reactor and around pipe air cooling reactor or Horizontal water cooling reactor; Described heat transfer reactor is with when pipe air cooling reactor front and back series combination becomes large-scale reactor combined unit, the shell side gas outlet of described heat transfer reactor and link around the shell side air inlet of pipe air cooling reactor, described around the tube side gas outlet of pipe air cooling reactor and the shell side air inlet binding of described heat transfer reactor; When tandem compound becomes large-scale reactor combined unit before and after described heat transfer reactor and the Horizontal water cooling reactor, be connected the shell side air inlet and connect in the shell side gas outlet of heat transfer reactor with the Horizontal water cooling reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220234489 CN202747831U (en) | 2012-05-07 | 2012-05-07 | Spiral coil heat exchanger and reactor with heat exchanger structure |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220234489 CN202747831U (en) | 2012-05-07 | 2012-05-07 | Spiral coil heat exchanger and reactor with heat exchanger structure |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202747831U true CN202747831U (en) | 2013-02-20 |
Family
ID=47707211
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220234489 Expired - Lifetime CN202747831U (en) | 2012-05-07 | 2012-05-07 | Spiral coil heat exchanger and reactor with heat exchanger structure |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202747831U (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103785367A (en) * | 2014-02-27 | 2014-05-14 | 上海龙净环保科技工程有限公司 | Annular dividing wall type activated coke purification moving bed regeneration tower and activated coke regeneration method |
| CN104419440A (en) * | 2013-08-22 | 2015-03-18 | 杭州林达化工技术工程有限公司 | Method and apparatus for producing hydrocarbons by synthesis gas from coal |
| CN105800554A (en) * | 2016-04-29 | 2016-07-27 | 南京国昌化工科技有限公司 | External header type water cooling controlled shift reactor |
| EP3199231A4 (en) * | 2014-09-24 | 2018-08-01 | Ren Lou | Large reactor and device and process thereof |
| WO2018154063A1 (en) * | 2017-02-24 | 2018-08-30 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e. V. | Heat exchanger and reactor |
| CN109173939A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | A kind of water cooling methanol synthesis reactor |
-
2012
- 2012-05-07 CN CN 201220234489 patent/CN202747831U/en not_active Expired - Lifetime
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104419440A (en) * | 2013-08-22 | 2015-03-18 | 杭州林达化工技术工程有限公司 | Method and apparatus for producing hydrocarbons by synthesis gas from coal |
| CN103785367A (en) * | 2014-02-27 | 2014-05-14 | 上海龙净环保科技工程有限公司 | Annular dividing wall type activated coke purification moving bed regeneration tower and activated coke regeneration method |
| CN103785367B (en) * | 2014-02-27 | 2016-02-10 | 上海龙净环保科技工程有限公司 | Annular dividing wall type activated coke purification moving bed regenerator and reactive coke regeneration method |
| EP3199231A4 (en) * | 2014-09-24 | 2018-08-01 | Ren Lou | Large reactor and device and process thereof |
| CN105800554A (en) * | 2016-04-29 | 2016-07-27 | 南京国昌化工科技有限公司 | External header type water cooling controlled shift reactor |
| WO2018154063A1 (en) * | 2017-02-24 | 2018-08-30 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e. V. | Heat exchanger and reactor |
| CN110494208A (en) * | 2017-02-24 | 2019-11-22 | 弗劳恩霍夫应用研究促进协会 | Heat exchanger and reactor |
| US10737232B2 (en) | 2017-02-24 | 2020-08-11 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. | Heat exchanger and reactor |
| CN110494208B (en) * | 2017-02-24 | 2022-07-12 | 弗劳恩霍夫应用研究促进协会 | Heat exchanger and reactor |
| CN109173939A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | A kind of water cooling methanol synthesis reactor |
| CN109173939B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | Water-cooling methanol synthesis reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202747831U (en) | Spiral coil heat exchanger and reactor with heat exchanger structure | |
| CN103240036B (en) | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application | |
| WO2016045585A1 (en) | Large reactor and device and process thereof | |
| CN100528320C (en) | Transverse pipe type heat transfer reaction unit | |
| CN101723775B (en) | Method and equipment for preparing hydrocarbon by methyl alcohol or/ and dimethyl ether | |
| CN101773808B (en) | Combined reaction device | |
| CN201168595Y (en) | Composite reaction equipment | |
| CN203096014U (en) | Device for producing natural gas from factory waste gas | |
| CN102160981B (en) | Catalytic reaction equipment | |
| CN102850183B (en) | Methanol synthesis system and method | |
| CN103063057B (en) | Feed gas chiller three plume low temperature wrap-round tubular heat exchangers | |
| CN103017573B (en) | Low-temperature spiral wound heat exchanger for non-converted gas cooler | |
| CN204365252U (en) | A kind of large-scale reactor and device thereof | |
| CN202460592U (en) | Temperature stress resistant heat transfer reactor and composite device thereof | |
| CN103033074B (en) | Low-temperature wound-tube heat exchanger used for converted gas cooler | |
| CN100386138C (en) | Process and equipment for internal heat exchanging catalytic reaction | |
| CN103585933B (en) | A kind of corrugated plate dst samming hydrogenation reactor | |
| CN202808648U (en) | Methanol synthetic system | |
| CN2903059Y (en) | Production apparatus of producing dimethyl ether by gas phase catalyzing methanol dehydrolysis | |
| CN2845904Y (en) | Lateral tubular heat exchanging reaction device | |
| CN114307869A (en) | Ammonia synthesis reactor | |
| CN203568842U (en) | Combined conversion device for synthesized gas CO | |
| CN202762411U (en) | Horizontal type water-cooling reactor | |
| CN203648501U (en) | Corrugated plate type uniform-temperature hydrogenation reactor | |
| CN102744018B (en) | Fixed bed catalytic reaction device with adjustable inlet material temperature |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130220 |