CN2758233Y - Thermal activation type multistage hydrocarbon conversion reactor - Google Patents
Thermal activation type multistage hydrocarbon conversion reactor Download PDFInfo
- Publication number
- CN2758233Y CN2758233Y CN 200420117191 CN200420117191U CN2758233Y CN 2758233 Y CN2758233 Y CN 2758233Y CN 200420117191 CN200420117191 CN 200420117191 CN 200420117191 U CN200420117191 U CN 200420117191U CN 2758233 Y CN2758233 Y CN 2758233Y
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- China
- Prior art keywords
- hydrocarbon conversion
- housing
- utility
- section
- gas
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- Expired - Fee Related
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 27
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 27
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 title abstract description 20
- 238000007725 thermal activation Methods 0.000 title 1
- 230000003197 catalytic effect Effects 0.000 claims abstract description 17
- 239000003054 catalyst Substances 0.000 claims abstract description 7
- 239000000203 mixture Substances 0.000 claims abstract description 4
- 230000035939 shock Effects 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 8
- 229910000831 Steel Inorganic materials 0.000 claims description 2
- 238000012856 packing Methods 0.000 claims description 2
- 239000010959 steel Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 22
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 8
- 239000001301 oxygen Substances 0.000 abstract description 8
- 229910052760 oxygen Inorganic materials 0.000 abstract description 8
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 238000000034 method Methods 0.000 abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000000567 combustion gas Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000003345 natural gas Substances 0.000 abstract description 3
- 239000012495 reaction gas Substances 0.000 abstract description 2
- 230000004913 activation Effects 0.000 abstract 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 230000000295 complement effect Effects 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 235000009508 confectionery Nutrition 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003063 flame retardant Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Landscapes
- Hydrogen, Water And Hydrids (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a heat activation type multistage hydrocarbon conversion reactor which belongs to the technical field of the production of synthesis gas. The utility model is composed of an outer shell, a gaseous hydrocarbon and steam mixture inlet, multistage catalytic beds, an interstage combustion gas inlet, catalyst loading and unloading ports of all the stages, a synthetic gas outlet, etc., wherein each stage of catalytic bed is composed of an upper fireproof ball layer, a catalyst layer, a lower fireproof ball layer and a porous supporting plate, and the porous supporting plate is connected with a shell body. The utility model adopts natural gas or other hydrocarbons and the combustion gas of oxygen or air to be directly mixed with reaction gas, (namely the heat activation method) to provide heat for reaction. The self supply of heat is realized, and simultaneously, the carbon complement is carried out to the reaction process. The utility model has the advantages of simple device structure, high heat utilization, low device investment and high productive efficiency.
Description
Technical field
The utility model relates to a kind of new device of producing synthetic gas, and relating in particular to a kind of is raw material with the gaseous hydrocarbons, transforms to be coupled by hydro carbons partial combustion and water vapor and produces the heat shock formula multistage hydrocarbon conversion reactions device of synthetic gas.
Background technology
The most complex structure of the device of present industrial hydrocarbon-converting synthetic gas producing, the energy consumption height, the facility investment height as the box tubulation converter of directly burning type, is made up of the nozzle structure and the high pressure steam system of bulky complex.Fuel such as the outer straight burning Sweet natural gas of reaction tubes, for inner reaction tube provides required heat, its weak point is: be subjected to the restriction of conversion tube material, directly burning type tubulation converter can not satisfy the requirement of high methane conversion, for improving methane conversion, need to increase by two sections conversion reactors of autothermal.Two sections conversion reactors are the single hop fixed-bed reactor, produce high temperature in conversion reactor top bubbling air (or oxygen-rich air, oxygen) and hydrogen generation combustion reactions in one section reforming gas, enter fixed catalytic bed interior further water vapor conversion reaction, the complex process of taking place then.Utilize this device to transform in addition and produce in the synthetic gas and need burn section H
2Regulate hydrogen-carbon ratio, this just causes and consumes greatly, energy utilizes unreasonable.
Summary of the invention
The utility model is for overcoming shortcoming of the prior art, and a kind of simple in structure, device that the multistage hydrocarbon conversion that efficient is high generates synthetic gas is provided.
The utility model is achieved by following technical scheme:
A kind of heat shock formula multistage hydrocarbon conversion reactions device, it is made of closed shell and porous support plate, and porous support plate layering successively is located within the housing, and is connected with housing, and described porous support plate is provided with the refractory ball layer; Form the catalytic bed of one section catalyzer of can packing between last refractory ball layer and the following refractory ball layer; One side of housing is provided with intersegmental burning gas import, and the opposite side of housing is provided with the catalyst loading and unloading mouth of each section, and the top of housing is provided with mixing burner, and mixing burner is provided with gaseous hydrocarbons and vapor mixture import, and syngas outlet is in lower part of frame.
Described catalytic bed can be the 2-8 section, and the best is the 3-5 section; Described shell is made up of housing, adiabator layer, refractory masses and water jacket etc.; Described intersegmental burning gas enters reactor and is set to many mouthfuls of tangential directions and enters.
It is the method for heat shock that the utility model directly mixes at the incomplete combustion gas of intersegmental employing Sweet natural gas or other hydro carbons and oxygen or air and reaction gas that epimere comes out, for reaction provides heat, realizes the heat self-sufficiency; Simultaneously, also implemented benefit carbon, made H for reaction process
2/ CO ratio can be adjustable in the 1.5-3.0 scope, to be fit to the needs that follow-up methyl alcohol and F-T synthetic fluid hydrocarbon fuel are produced.
The utility model compared with prior art, its significant advantage comprises:
1. adopt the multi-stage type catalytic bed, compare with directly burning type tubulation primary reformer, save the conversion tube that uses the high temperature high voltage resistant that reaches hundreds of, it is much simple that structure is wanted.
2. flame retardant coating, thermal insulation layer and water add cover and have guaranteed that the temperature of equipment metal shell is lower, so shell can adopt the lower material of price to make, and facility investment reduces greatly.
3. compared with prior art, the supply of heat is distributed in multistage, and it is too high that every section inlet temperature is unlikely, thereby guaranteed activity of such catalysts, and prolong the work-ing life of catalyzer.
4. the utility model adopts the mode of mending carbon to regulate synthetic gas H
2/ CO reduces in the synthetic gas method of hydrogen content with hydrogen in existing one section reforming gas of burning and compares, and is a kind of positive H
2/ CO control method, save energy, the raw material consumption that reduces, the production efficiency height, cost reduces.
5. owing in burner, adopt hydrocarbon gas and the reaction of oxygen generation incomplete combustion, be mixed with water vapour or CO in the oxygen
2Reducing the temperature in the burner, and reduced the possibility of carbon distribution.
Description of drawings
Fig. 1 is a setting drawing of the present utility model.
Embodiment
The utility model is further described below in conjunction with accompanying drawing:
As shown in Figure 1, heat shock formula multistage hydrocarbon conversion reactions device is made of closed shell 102 and porous support plate 112, and porous support plate 112 layerings are located within the housing, and are connected with housing; Described porous support plate 112 is provided with the refractory ball layer, and top refractory ball layer 109, catalyst layer 110, bottom refractory ball layer 111 forms one section catalytic bed 103 of every section, two sections catalytic beds 105, three sections catalytic beds 107; One side of housing is provided with intersegmental burning gas import 104,106, the opposite side of housing is provided with the catalyst loading and unloading mouth 113 of each section, the top of housing is provided with mixing burner 101, mixing burner 101 is provided with gaseous hydrocarbons and vapor mixture import 117,118, and syngas outlet 108 is in lower part of frame.
Described heat shock formula multistage hydrocarbon conversion reactions device, its catalytic bed can be the 2-8 section, and the best is the 3-5 section; Shell 102 by steel water add cover 114, adiabator layer 115, refractory masses 116 are formed; Intersegmental burning gas import 104,106 is set to many mouthfuls of tangential directions and enters.
Reaction process is: the raw material hydrocarbon gas enters the mouth by 118 after desulfurization and preheating, spray in the upper space of conversion reactor with the water vapor after 117 inlets enter the preheating of mixing burner 101 and the miscellany of oxygen, partial oxidation reaction at first takes place, and enters one section catalytic bed 103 then hydrocarbon steam conversion reaction and the conversion reaction of hydro carbons carbonic acid gas take place.
Hydrocarbon fuel through desulfurization and preheating sprays in one or the two intersegmental external burners, with the miscellany mixing generation partial oxidation reaction of oxygen and water vapor.
The high-temperature part oxic gas of being come out by burner is by between the tangential direction approach section, enter two sections catalytic beds 105 with one section reactant gases after mixed and react, from two sections reaction gases that come out with enter after two or three intersegmental part oxic gas are mixed three sections catalytic beds 107 further the generation steam reforming react.Enter subsequent handling by three sections synthetic gas that come out through exporting 108.
The utility model also can be and is set to the multistage catalytic bed, and it is better to be generally 2-8 section effect, 3-5 section the best.The utility model device structure is simple, the heat utilization efficiency height, and facility investment is low, the production efficiency height.
Claims (5)
1, a kind of heat shock formula multistage hydrocarbon conversion reactions device is characterized in that it is made of closed shell and porous support plate, and porous support plate layering successively is located within the housing, and is connected with housing; Described porous support plate is provided with the refractory ball layer, forms the catalytic bed of one section catalyzer of can packing between last refractory ball layer and the following refractory ball layer; One side of housing is provided with the catalyst loading and unloading mouth of each section, and the opposite side of housing is provided with intersegmental burning gas import, and the top of housing is provided with mixing burner, and mixing burner is provided with gaseous hydrocarbons and vapor mixture import, and syngas outlet is in lower part of frame.
2, heat shock formula multistage hydrocarbon conversion reactions device as claimed in claim 1 is characterized in that described catalytic bed is the 2-8 section.
3, heat shock formula multistage hydrocarbon conversion reactions device as claimed in claim 1 is characterized in that described catalytic bed is the 3-5 section.
4, heat shock formula multistage hydrocarbon conversion reactions device as claimed in claim 1 is characterized in that described shell adds cover, adiabator layer, refractory masses by steel water and forms.
5, heat shock formula multistage hydrocarbon conversion reactions device as claimed in claim 1 is characterized in that described intersegmental burning gas import is set to many mouthfuls of tangential directions and enters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200420117191 CN2758233Y (en) | 2004-12-17 | 2004-12-17 | Thermal activation type multistage hydrocarbon conversion reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200420117191 CN2758233Y (en) | 2004-12-17 | 2004-12-17 | Thermal activation type multistage hydrocarbon conversion reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2758233Y true CN2758233Y (en) | 2006-02-15 |
Family
ID=36078378
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200420117191 Expired - Fee Related CN2758233Y (en) | 2004-12-17 | 2004-12-17 | Thermal activation type multistage hydrocarbon conversion reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2758233Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101721957B (en) * | 2009-12-03 | 2011-08-31 | 太原理工大学 | Continuous carbon catalytic CH4-CO2 reforming reactor |
-
2004
- 2004-12-17 CN CN 200420117191 patent/CN2758233Y/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101721957B (en) * | 2009-12-03 | 2011-08-31 | 太原理工大学 | Continuous carbon catalytic CH4-CO2 reforming reactor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |