CN201900005U - Heat exchange type reforming furnace - Google Patents
Heat exchange type reforming furnace Download PDFInfo
- Publication number
- CN201900005U CN201900005U CN2010206011844U CN201020601184U CN201900005U CN 201900005 U CN201900005 U CN 201900005U CN 2010206011844 U CN2010206011844 U CN 2010206011844U CN 201020601184 U CN201020601184 U CN 201020601184U CN 201900005 U CN201900005 U CN 201900005U
- Authority
- CN
- China
- Prior art keywords
- heat
- conversion tube
- bearing shell
- pressure
- adds
- 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
Abstract
The utility model provides a heat exchange type reforming furnace which comprises a pressure-bearing shell, a conversion pipe, a first heating channel and a second heating channel, wherein the conversion pipe is vertically arranged in the pressure-bearing shell and is internally filled with catalyst; the conversion pipe is respectively communicated with a raw gas inlet and a reforming gas outlet which are arranged on the pressure-bearing shell; the first heating channel is arranged to be adjacent to the side wall of the conversion pipe; the inlet end of the first heating channel is arranged to be adjacent to the upper end of the conversion pipe; the outlet end of the first heating channel is arranged to be adjacent to the lower end of the conversion pipe; the second heating channel is arranged to be adjacent to the side wall of the conversion pipe; the inlet end of the second heating channel is arranged to be adjacent to the lower end of the conversion pipe; and the outlet end of the second heating channel is arranged to be adjacent to the upper end of the conversion pipe. The heat exchange type reforming furnace enhances the coefficient of heat transfer of raw gas, thus improving the conversion efficiency of hydrocarbon gas in the raw gas and obtaining good energy-saving and gas-saving effects.
Description
Technical field
The utility model relates to a kind of heat exchange type converting apparatus structure technology, relates in particular to a kind of heat-exchanged reformer.
Background technology
Auto-thermal reforming process is the energy-conservation advanced technologies of a kind of solar term, and abroad in the eighties in last century, Britain I.C.I company at first realizes industrialization.Middle nineteen nineties in last century China's chemical industry to take the lead in succeeding in developing with the natural gas be raw material, produce 15000 tons of small-sized synthetic ammonia installations per year, the solar term effect is remarkable.The key equipment of realizing this heat exchange type conversion technology is exactly a heat-exchanged reformer, and its major function is exactly to add water vapour to form unstripped gas in hydrocarbon gas, and the hydrocarbon gas in the unstripped gas carries out conversion reaction under the effect of catalyst.Hydrocarbon gas in the unstripped gas mainly is a methane, and this reaction is the endothermic reaction, and the chemical equation that methane carries out conversion reaction is:
CH
4+H
2O↑＝CO+3H
2-Q
The groundwork principle of heat-exchanged reformer is that conversion tube is set in pressure-bearing shell, fill in the conversion tube with catalyst, in an end of conversion tube, feed hydrocarbon gas and water vapour, in pressure-bearing shell, conversion tube is heated, normally outside conversion tube, the unstripped gas in the conversion tube is heated with the heat air of carrying heat, make it under the effect of catalyst, transform into reformed gas, discharge from the other end of conversion tube.Because the reformed gas that obtains is a high temperature, so toward contact reformed gas is recycled in the pressure-bearing shell as heat air.
Find to have following problem at least in the application in practice process of heat-exchanged reformer: one, the inlet temperature of heat air and outlet temperature are about 1017 ℃ and 715 ℃ respectively outside the conversion tube of existing heat-exchanged reformer, and unstripped gas inlet temperature and outlet temperature are about 595 ℃ and 915 ℃ respectively in the conversion tube.Because the flow direction of unstripped gas and the outer heat air of pipe is normally opposite in the pipe, so the unstripped gas inlet temperature is about 715 ℃-595 ℃=120 ℃ with the outlet temperature difference of the outer heat air of pipe in the pipe, the less motive force of the export-oriented conversion of conversion tube intraductal heat transfer that causes of this temperature difference is little, the unstripped gas programming rate is more slow in the pipe of conversion tube porch, and the transformation efficiency of the methane in the unstripped gas is not high.Two, the outer heat air of pipe in pressure-bearing shell in the process of flowing temperature descend gradually, when being higher than 800 ℃, based on radiant heat transfer, convection heat transfer' heat-transfer by convection is auxilliary to unstripped gas in managing, when being lower than 800 ℃, just the opposite.The temperature of the outer heat air of pipe is reduced to 715 ℃ by 1017 ℃ of inlet when exporting, then gas flow rate is low when the temperature of heat air outside the pipe is lower than 800 ℃, can not effectively be heated in the conversion tube of corresponding section, and cause the transformation efficiency of the methane in the unstripped gas not high with this place's gas.
Methane content still has 15%～35% not wait in the gas of discharging after above-mentioned conversion process, and methane content can be with unstripped gas kind, transfer pressure, temperature is different and different.In order further to reduce remaining methane content in the reformed gas, prior art can be provided with two reburners, i.e. one-stage converter and secondary reformer.The gas that one-stage converter is discharged is called one section reformed gas.One section reformed gas is sent into secondary reformer again and is carried out the degree of depth and transform, and makes in two sections reformed gas methane content reduce to CH
4＜1%.Common so-called two-part Auto-thermal reforming process that Here it is, but obviously the equipment cost of two-part Auto-thermal reforming process increases.
The utility model content
The utility model provides a kind of heat-exchanged reformer, to improve the gas transformation efficiency in the heat-exchanged reformer.
The utility model embodiment provides a kind of heat-exchanged reformer, comprising:
Pressure-bearing shell;
Conversion tube vertically is arranged in the described pressure-bearing shell, is filled with catalyst in the described conversion tube, described conversion tube respectively with described pressure-bearing shell on the unstripped gas inlet that is provided with and reformed gas export and be connected;
First adds heat passage, the sidewall setting of contiguous described conversion tube, and described first arrival end that adds heat passage is adjacent to the upper end of described conversion tube, and described first port of export that adds heat passage is adjacent to the lower end of described conversion tube;
Second adds heat passage, the sidewall setting of contiguous described conversion tube, and described second arrival end that adds heat passage is adjacent to the lower end of described conversion tube, and described second port of export that adds heat passage is adjacent to the upper end of described conversion tube;
Aforesaid heat-exchanged reformer, the shape of cross section of described conversion tube are annular, and the described first heating channel setting is in the inside of described conversion tube, and the described second heating channel setting is in the outside of described conversion tube.
Aforesaid heat-exchanged reformer, the described conversion tube and first quantity that adds heat passage are a plurality of, and described second quantity that adds heat passage is one, and each described conversion tube is arranged on one described second and adds in the heat passage.
Aforesaid heat-exchanged reformer, also comprise: gas distributor, be arranged in the described pressure-bearing shell, the arrival end of described gas distributor links to each other by first heated air inlet that discharge and described pressure-bearing shell top are provided with, and the port of export of described gas distributor links to each other with each described first arrival end that adds heat passage.
Aforesaid heat-exchanged reformer, described first length that adds heat passage is 7～13 meters; Described first nominal diameter that adds heat passage is 14～32 millimeters; The length of described conversion tube is 7～13 meters; The nominal diameter of described conversion tube is 38～76 millimeters.
Aforesaid heat-exchanged reformer is provided with deflection plate in the described pressure-bearing shell, is formed on described second and adds in the heat passage.
Aforesaid heat-exchanged reformer, the described deflection plate density that is provided with in pressure-bearing shell increases in described pressure-bearing shell from down to up gradually.
Aforesaid heat-exchanged reformer, described conversion tube outer wall is around being provided with fin.
Aforesaid heat-exchanged reformer, described pressure-bearing shell outer wall is provided with cooling water jecket, and described cooling water jecket is provided with chuck cooling water inlet and chuck coolant outlet, and described pressure-bearing shell inwall adopts refractory liner.
As shown from the above technical solution, the utility model adds heat passage by being provided with two, make heat air respectively and add heat passage by two from bottom to top the unstripped gas in the conversion tube is heated from top to bottom, to improve the temperature difference of unstripped gas porch unstripped gas and heat air, promote heat air and conduct heat to unstripped gas.The relative heated air stream of two-way direction makes the conversion tube upper and lower side can both be subjected to the heat transmission of high temperature heat air, improves gas flow rate, and then has improved gas reversion rate in the unstripped gas, has improved the solar term energy-saving effect.
Description of drawings
The cross-sectional view of the heat-exchanged reformer that Fig. 1 provides for the utility model embodiment one;
The cross-sectional view of the heat-exchanged reformer that Fig. 2 provides for the utility model embodiment two;
Fig. 3 is the local structure for amplifying schematic diagram of conversion tube among the utility model embodiment two;
Fig. 4 is the second local structure for amplifying schematic diagram that adds heat passage among the utility model embodiment two.
Reference numeral:
The 1-pressure-bearing shell; The 2-conversion tube; 3-first adds heat passage;
4-second adds heat passage; The 5-catalyst; 6-unstripped gas inlet;
The outlet of 7-reformed gas; 8-first heat air inlet; 9-second heat air inlet;
The 10-gas distributor; The 11-discharge; The 12-deflection plate;
The 13-cooling water jecket; 14-chuck cooling water inlet; 15-chuck coolant outlet;
The 16-refractory liner; The 31-baffle plate; The 32-through hole.
The specific embodiment
For the purpose, technical scheme and the advantage that make the utility model embodiment clearer, below in conjunction with the accompanying drawing among the utility model embodiment, technical scheme among the utility model embodiment is clearly and completely described, obviously, described embodiment is the utility model part embodiment, rather than whole embodiment.Based on the embodiment in the utility model, those of ordinary skills are not making the every other embodiment that is obtained under the creative work prerequisite, all belong to the scope of the utility model protection.
Embodiment one
The cross-sectional view of the heat-exchanged reformer that Fig. 1 provides for the utility model embodiment one, as shown in Figure 1, this heat-exchanged reformer comprises that pressure-bearing shell 1, conversion tube 2, first add heat passage 3 and second and add heat passage 4.In the present embodiment, pressure-bearing shell 1 is provided with unstripped gas inlet 6 and reformed gas outlet 7; Conversion tube 2 vertically is arranged in the pressure-bearing shell 1, is filled with the used catalyst 5 of reaction in the conversion tube 2, and the two ends of conversion tube 2 are connected with unstripped gas inlet 6 and reformed gas outlet 7 respectively; First adds the sidewall setting of heat passage 3 contiguous conversion tubes 2, first arrival end that adds heat passage 3 is adjacent to the upper end of conversion tube 2, first port of export that adds heat passage 3 is adjacent to the lower end of conversion tube 2, heat air adds heat passage 3 by first and flows from top to bottom, and to the heating of the unstripped gas in the conversion tube 2; Second adds the sidewall setting of heat passage 4 contiguous conversion tubes 2, second arrival end that adds heat passage 4 is adjacent to the lower end of conversion tube 2, second port of export that adds heat passage 4 is adjacent to the upper end of conversion tube 2, heat air adds heat passage 4 by second and flows from bottom to top, and to the heating of the unstripped gas in the conversion tube 2.
In the present embodiment, conversion tube 2 can be columned pipeline, first adds heat passage 3 and second, and to add heat passage 4 can be the pipeline that is separately positioned on conversion tube 2 both sides, pyrolytic conversion gas in employing is recycled to reburner is during as heat air, the conversion tube 2 passable ports of export can add heat passage 4 by second and be communicated to reformed gas outlet 7, and the reformed gas that flows out from conversion tube 2 this moment also double as heat air is used; When adopting other high-temperature gases, then can utilize independently pipeline that reformed gas is derived from pressure-bearing shell 1 as heat air.
In the present embodiment, the concrete course of work of heat-exchanged reformer is: pressure is the hydrocarbon gas of 1.0MPa～5.0MPa, after desulfurization is handled and is allocated a certain amount of water vapour into, be preheated to 500 ℃～650 ℃ (for example 595 ℃), enter into the conversion tube 2 that is filled with catalyst 5 by the inlet of the unstripped gas on the pressure-bearing shell 16, hydrocarbon gas is specifically as follows natural gas.Temperature is about 1000 ℃ (for example 1017 ℃), pressure is the heat air of 1.0MPa～5.0MPa, separated into two parts, part heat air adds heat passage 3 by first and gives the heating of the unstripped gas in the conversion tube 2 from top to bottom, and another part heat air adds heat passage 4 by second and gives the heating of the unstripped gas in the conversion tube 2 from bottom to up.Concrete, heat air can be the pyrolytic conversion gas from autothermal reformer.The heat of two-way pyrolytic conversion gas passes to unstripped gas in the conversion tube 2 by catalyst 5, and the hydrocarbon gas in the gas of supplying raw materials transforms required heat.Unstripped gas is by the high temperature heating and under the effect of catalyst, and taking place becomes reformed gas after the conversion reaction, mixes the back with the reformed gas that heat is provided and discharges from the reformed gas outlet 7 on the pressure-bearing shell, has just finished the conversion process of unstripped gas.
The pyrolytic conversion gas that the two-way flow direction is relative acts on the unstripped gas in the conversion tube 2 simultaneously, has remedied the defective of heating deleterious after the mobile heat air of single direction is lowered the temperature gradually.The reformed gas of conversion tube 2 porch and the temperature difference of unstripped gas are about 1017 ℃-595 ℃=422 ℃, strengthened the motive force that unstripped gas conducts heat in conversion tube 2, the temperature of conversion tube 2 porch unstripped gas can be promoted quickly, thereby improve gas reversion efficient in the unstripped gas.
Embodiment two
The cross-sectional view of the heat-exchanged reformer that Fig. 2 provides for the utility model embodiment two.In the present embodiment, the shape of cross section of conversion tube 2 is specially annular, helps commercial Application and promotes.Preferably, first adds the inside that heat passage 3 can be arranged on conversion tube 2, carry out heat transmission by 5 pairs of unstripped gas of the catalyst in the conversion tube 2 from inside to outside by first heat air that adds heat passage 3, second adds the outside that heat passage 4 is arranged on conversion tube 2, carries out heat transmission by 5 pairs of unstripped gas of the catalyst in the conversion tube 2 from outside to inside by second heat air that adds heat passage 4.Make unstripped gas be heated evenly, help improving the gas reversion rate in the unstripped gas.Be illustrated in figure 3 as the local structure for amplifying schematic diagram of conversion tube among the utility model embodiment two, the lower end of conversion tube 2 can be provided with baffle plate 31, baffle plate is provided with the through hole 32 of array arrangement, baffle plate 31 is used for supporting the catalyst 5 of conversion tube 2, on the other hand, unstripped gas can also be by 32 circulations of the through hole on the baffle plate 31.
The quantity that conversion tube 2 in the present embodiment and first adds heat passage 3 can be a plurality of, and the unstripped gas demultiplexing enters in the conversion tube 2 and transforms, and has increased heating surface area.The quantity of conversion tube 2 can be provided with according to manufacturing specification request.The arrangement mode of conversion tube 2 can be arranged for equilateral triangle, also can arrange for the circular concentric formula, and perhaps be other arrangement modes.Second quantity that adds heat passage 4 is one, and each conversion tube 2 is arranged on one second and adds in the heat passage 4.Concrete, second adds heat passage 4 can be for the inner space of the pressure-bearing shell 1 at conversion tube 2 places, to provide heat to all conversion tubes 2.Heat air enters in the pressure-bearing shell 1 by second heat air inlet 9 that is arranged on the pressure-bearing shell 1, by the second unstripped gas heat supply that adds in 4 pairs of conversion tubes of heat passage 2.
Heat-exchanged reformer in the present embodiment also is provided with gas distributor 10, gas distributor 10 is arranged in the pressure-bearing shell 1, the arrival end of gas distributor 10 links to each other by first heat air inlet 8 that discharge 11 and pressure-bearing shell 1 top are provided with, the port of export of gas distributor links to each other with each first arrival end that adds heat passage 3, concrete, first mode of communicating that adds heat passage 3 and gas distributor 10 as shown in Figure 4.Heat air is by entering into gas distributor 10 with first heat air inlet, 8 discharges that link to each other 11, enters into respectively first then and adds heat passage 3.By the setting of gas distributor 10, it is more even to be assigned to each first heat air that adds in the heat passage 3, and the unstripped gas that helps in each conversion tube 2 is heated evenly, and makes hydrocarbon gas transformation efficiency equilibrium in each conversion tube 2.
In the present embodiment, first adds the length of heat passage 3 and nominal diameter can be respectively be provided with according to the length and the nominal diameter of conversion tube 2, concrete, first length that adds heat passage 3 can be 7～13 meters, first nominal diameter that adds heat passage 3 is 14～32 millimeters, the length of conversion tube 2 is 7～13 meters, and the nominal diameter of conversion tube 2 is 38～76 millimeters.Preferably, first length that adds heat passage 3 equates substantially with the length of conversion tube 2, helps unstripped gas and can both be subjected to the heat that adds the heat air of heat passage 3 from first at the whole flow process of conversion tube 2.
In the present embodiment, can also be provided with deflection plate 12 in the pressure-bearing shell 1, be formed on second and add in the heat passage 4, specifically can be arranged in the pressure-bearing shell 1 by pull bar.By the setting of deflection plate 12, can limit second circulation path that adds the heat air in the heat passage 4, to improve utilization ratio to the heat of heat air.
Preferably, the be provided with density of deflection plate 12 in pressure-bearing shell 1 increases in pressure-bearing shell 1 from down to up gradually.Heat air adds the arrival end temperature of heat passage 4 than higher second, serve as the main heat that transmits to conversion tube 2 in the heat radiation mode this moment, and when heat air added the port of export of heat passage 4 near second, temperature descended, the heat transmission is based on convection current, but this moment, the heat air flow velocity slowed down.By equidistantly not being provided with to deflection plate 12, partly arrange less several deflection plates 12 at second arrival end that adds heat passage 4, main rising supported positioning action, but second add heat passage 4 near port of export part several deflection plates 12 are set suitably more, to increase the flow velocity of heat air, improve the heat transfer coefficient of heat air, help the gas reversion in the unstripped gas in the conversion tube 2.
In the present embodiment, conversion tube 2 outer walls are around being provided with fin, increasing the heat exchange area of conversion tube 2, and then enhanced heat exchange.
In the above-described embodiments, pressure-bearing shell 1 outer wall can also be provided with cooling water jecket 13, cooling water jecket is provided with chuck cooling water inlet 14 and chuck coolant outlet 15, cooling water enters into cooling water jecket 13 from the chuck cooling water inlet 14 on the pressure-bearing shell 1, by fully contacting with pressure-bearing shell 1, pressure-bearing shell 1 external temperature is descended, cooling water after the heat absorption flows out from chuck coolant outlet 15 again, effectively reduce the temperature of pressure-bearing shell 1, to improve the running safety of heat-exchanged reformer.Pressure-bearing shell 1 inwall can adopt refractory liner 16, further reduces the temperature of pressure-bearing shell 1.
The heat-exchanged reformer that the utility model provides, add the setting of heat passage by two-way, improved heat exchange coefficient, can satisfy the required heat of hydrocarbon gas conversion in the unstripped gas, after the heat-exchanged reformer that makes unstripped gas provide through the utility model transforms, the content of the hydrocarbon gas in the unstripped gas (mainly being methane) can be reduced to below 2.5%, again with after reformed gas as the low methane content of heat air mixes, the content of methane can be reduced to below 0.5%, therefore do not need to carry out degree of depth conversion through secondary reformer again and just can obtain the required reformed gas of industry, obtain good solar term energy-saving effect, conversion system equipment can be changed into and only use the one-part form reburner, can reduce equipment cost.
It should be noted that at last: above embodiment only in order to the explanation the technical solution of the utility model, is not intended to limit; Although the utility model is had been described in detail with reference to previous embodiment, those of ordinary skill in the art is to be understood that: it still can be made amendment to the technical scheme that previous embodiment is put down in writing, and perhaps part technical characterictic wherein is equal to replacement; And these modifications or replacement do not make the essence of appropriate technical solution break away from the spirit and scope of each embodiment technical scheme of the utility model.
Claims (9)
1. a heat-exchanged reformer is characterized in that, comprising:
Pressure-bearing shell;
Conversion tube vertically is arranged in the described pressure-bearing shell, is filled with catalyst in the described conversion tube, described conversion tube respectively with described pressure-bearing shell on the unstripped gas inlet that is provided with and reformed gas export and be connected;
First adds heat passage, the sidewall setting of contiguous described conversion tube, and described first arrival end that adds heat passage is adjacent to the upper end of described conversion tube, and described first port of export that adds heat passage is adjacent to the lower end of described conversion tube;
Second adds heat passage, the sidewall setting of contiguous described conversion tube, and described second arrival end that adds heat passage is adjacent to the lower end of described conversion tube, and described second port of export that adds heat passage is adjacent to the upper end of described conversion tube.
2. heat-exchanged reformer according to claim 1 is characterized in that:
The shape of cross section of described conversion tube is an annular, and the described first heating channel setting is in the inside of described conversion tube, and the described second heating channel setting is in the outside of described conversion tube.
3. heat-exchanged reformer according to claim 1 and 2 is characterized in that: the described conversion tube and first quantity that adds heat passage are a plurality of, and described second quantity that adds heat passage is one, and each described conversion tube is arranged on one described second and adds in the heat passage.
4. heat-exchanged reformer according to claim 3 is characterized in that, described reburner also comprises:
Gas distributor is arranged in the described pressure-bearing shell, and the arrival end of described gas distributor links to each other by first heated air inlet that discharge and described pressure-bearing shell top are provided with, and the port of export of described gas distributor links to each other with each described first arrival end that adds heat passage.
5. heat-exchanged reformer according to claim 2 is characterized in that: described first length that adds heat passage is 7～13 meters; Described first nominal diameter that adds heat passage is 14～32 millimeters; The length of described conversion tube is 7～13 meters; The nominal diameter of described conversion tube is 38～76 millimeters.
6. heat-exchanged reformer according to claim 3 is characterized in that: be provided with deflection plate in the described pressure-bearing shell, be formed on described second and add in the heat passage.
7. heat-exchanged reformer according to claim 6 is characterized in that: the be provided with density of described deflection plate in pressure-bearing shell increases in described pressure-bearing shell from down to up gradually.
8. heat-exchanged reformer according to claim 2 is characterized in that: described conversion tube outer wall is around being provided with fin.
9. heat-exchanged reformer according to claim 1, it is characterized in that: described pressure-bearing shell outer wall is provided with cooling water jecket, described cooling water jecket is provided with chuck cooling water inlet and chuck coolant outlet, and described pressure-bearing shell inwall adopts refractory liner.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206011844U CN201900005U (en) | 2010-11-08 | 2010-11-08 | Heat exchange type reforming furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206011844U CN201900005U (en) | 2010-11-08 | 2010-11-08 | Heat exchange type reforming furnace |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201900005U true CN201900005U (en) | 2011-07-20 |
Family
ID=44270607
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010206011844U Expired - Lifetime CN201900005U (en) | 2010-11-08 | 2010-11-08 | Heat exchange type reforming furnace |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201900005U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103332651A (en) * | 2013-06-20 | 2013-10-02 | 中石化宁波工程有限公司 | Method for preventing harp-type converter lower gas collection branch tube from thermal deformation |
-
2010
- 2010-11-08 CN CN2010206011844U patent/CN201900005U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103332651A (en) * | 2013-06-20 | 2013-10-02 | 中石化宁波工程有限公司 | Method for preventing harp-type converter lower gas collection branch tube from thermal deformation |
| CN103332651B (en) * | 2013-06-20 | 2015-07-08 | 中石化宁波工程有限公司 | Method for preventing harp-type converter lower gas collection branch tube from thermal deformation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204247177U (en) | A kind of thermal insulation-isothermal methanation reactor | |
| EP3199231B1 (en) | Large reactor and device and process thereof | |
| CN101254442B (en) | Use of gas-solid catalytic reactor in preparing methanol | |
| CN103240036B (en) | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application | |
| CN1736574A (en) | Non-hot spot calandria type fixed bed reactors | |
| CN201519571U (en) | Shell and tube reactor for producing chloroethylene by utilizing acetylene method | |
| CN201900005U (en) | Heat exchange type reforming furnace | |
| CN102980166B (en) | Steam-water circulating system utilizing waste heat of high-temperature calcined coke generated by pot calciner | |
| CN201850132U (en) | Heat exchange reformer | |
| CN100593677C (en) | Mine wind-lacked gas thermal oxidizing apparatus | |
| CN215003079U (en) | High-efficiency energy-saving heat exchanger | |
| CN201980995U (en) | Heat transferring reformer | |
| CN106693849A (en) | Methanation reactor and methanation technology | |
| CN210438410U (en) | Natural gas hydrogen production conversion device | |
| CN212269454U (en) | Conversion tube and converter for hydrogen production | |
| CN204122092U (en) | Thimble tube heat-exchanged reformer | |
| CN203428908U (en) | Novel heat transfer type reformer | |
| CN203030262U (en) | Large hanging-basket sealing heat exchange type one-stage converter | |
| CN203648501U (en) | Corrugated plate type uniform-temperature hydrogenation reactor | |
| CN102133512A (en) | Reactor applied to gas-phase exothermic reaction | |
| CN202752008U (en) | Gas phase hydrogenation reactor | |
| CN202208644U (en) | Polycrystalline silicon hydrogenation furnace | |
| CN201684584U (en) | Vinyl acetate reactor | |
| CN201253566Y (en) | Heat exchange type reborner | |
| CN206109337U (en) | Multistage cold shock formula coke oven gas methanation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: The new Sichuan tonre Engineering Technology Co Ltd Assignor: Pang Yuxue Contract record no.: 2012510000033 Denomination of utility model: Process for producing rising pipe in heat exchanging reforming furnace Granted publication date: 20110720 License type: Exclusive License Record date: 20120426 |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20110720 |