CN203284201U - Reforming reactor with mixed type gas distributor - Google Patents
Reforming reactor with mixed type gas distributor Download PDFInfo
- Publication number
- CN203284201U CN203284201U CN2013203266296U CN201320326629U CN203284201U CN 203284201 U CN203284201 U CN 203284201U CN 2013203266296 U CN2013203266296 U CN 2013203266296U CN 201320326629 U CN201320326629 U CN 201320326629U CN 203284201 U CN203284201 U CN 203284201U
- Authority
- CN
- China
- Prior art keywords
- gas
- reforming reactor
- gas distributor
- communicated
- hybrid
- 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 - Fee Related
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
A reforming reactor with a mixed type gas distributor is provided with a third water steam inlet pipe on the upper part of the reforming reactor, the bottom of the reforming reactor is communicated with the mixed type gas distributor through a pedestal of a tower-type distribution device, and the lower end of a catalyst material bin is provided with an ascending pipeline; the mixed type gas distributor is constructed by communicating the tower gas distribution device with a gas mixing device and a tee; the upper end of the mixed type gas distribution device is constructed by overlaying a plurality of layers of grate bars forming an umbrella-shaped structure, and the bottom end of the mixed type gas distribution device is communicated with an inner casing pipe and an outer casing pipe through a flange; the inner casing pipe is communicated with a CH4-rich mixed gas inlet pipe and a second water steam inlet pipe; the outer casing pipe is communicated with the tee and a descending pipeline through an elbow pipe component. The reforming reactor is simple in structure, has a small amount of a catalyst and high conversion rate, and is suitable for reforming coke oven gas, coal-bed gas, refinery dry gas or other composite raw materials to prepare synthetic gas.
Description
Technical field
The utility model relates to a kind of methane rich gas mixture and prepares the reactor of synthetic gas, and particularly a kind of gas mixture of methane rich with hybrid gas distributor prepares the reforming reactor of synthetic gas.
Background technology
The coke-oven gas of existing coking enterprise separates and obtains hydrogen and methane rich gas mixture through TSA, PSA technique, hydrogen is used to the high value added products such as synthesizing methanol and dme, and the utilization of methane rich gas mixture is not yet formed the effective treatment process of environmental protection and equipment, this is because the Average bond energy of the c h bond of methane is 4.1 * 10
5J/mol, CH
3The dissociation energy of-H key is up to 4.3 * 10
5J/mol, molecular structure stabilized, be difficult to directly be transformed.
Existing recovery system to coke-oven gas, as CN1428403A for this process design one cover conversion unit, and stable operation, a wider range, energy consumption is little, and can be suitable for various coals.But this cover process equipment amount is limited, also amplifies industrial at present, in actual production, in order to recycle methane rich fuel gas, separately establishes specially a production process equipment in addition, invests very greatly, is difficult to realize industrialization.
Summary of the invention
The facility investment that exists based on above-mentioned prior art is large, the problem of narrow application range, the easy inactivation of catalyzer, and the utility model provides a kind of reforming reactor with hybrid gas distributor.
A kind of reforming reactor with hybrid gas distributor, it is characterized in that: the top of described reforming reactor is provided with the 3rd water vapour import, bottom is communicated with hybrid gas distributor by tower distribution apparatus base, in the lower end of catalyzer feed bin, is provided with uphill line;
Described hybrid gas distributor is to be communicated with and to form with gas mixer and threeway by tower distribution device in gas-fluid; Wherein, the upper end of hybrid distribution device in gas-fluid is to consist of the stack of the fire bars of some layers of umbrella-shaped structure, and bottom is communicated with inner sleeve and outer tube by flange; Inner sleeve is communicated with rich CH
4Combi inlet port pipe and the second water vapor inlet pipe; Outer tube is communicated with threeway and descending pipeline by bending component.
Technical characterictic is further: the diameter of described tower distribution device in gas-fluid is 1/4 ~ 2/5 with the diameter of reforming reactor ratio, and is positioned at reactor bottom face 400 ~ 550mm place; The fire bars of tower distribution device in gas-fluid and the angle of horizontal plane are 45o ~ 60o, and the number of plies is 5 ~ 10 layers; The mixed gas outlet of described gas mixer is higher than bottom face 50 ~ 150mm in reforming reactor; Described tower sparger base is higher than bottom face 160 ~ 250mm in reactor; Described gas mixer is set to respectively mixed gas outlet, gas injection section and the gas section of converging successively, and lower end is provided with rich CH
4Combi inlet port and the second water vapor import; The diameter ratio of described inner sleeve diameter and outer tube is 1/2 ~ 4/5; The gas section of converging of described hybrid gas distributor and gas jet segment inside are filled with stainless steel ripple filler; Described threeway is provided with the first water vapor import and air intlet.
A kind of reforming reactor with hybrid gas distributor that the utility model is above-mentioned, compared with prior art, its advantage is with positively effect: described reforming reactor has not only been realized fully mixing of methane rich gas mixture and water vapor, and water vapor and the reaction of charcoal generating gasification, increase gas production rate, also overcome simultaneously the blast problem that may cause while passing into air.
The utility model reforming reactor takes full advantage of high temperature and the methane rich gas mixture resource in reactor, realize effective utilization of the energy and the reasonable disposition of equipment in technological process, be suitable for the combination raw materials preparing synthetic gas by reforming such as coke-oven gas, coal-seam gas and coking plant dry gas, have good economic benefit and social benefit.
Description of drawings
Fig. 1 is the structural representation of reforming reactor.
Fig. 2 is the structural representation of the hybrid gas distributor of Fig. 1.
In figure: water vapor import in 1: the first; 2: air intlet; Water vapor import in 3: the second; 4: pillar; 5: rich CH
4Combi inlet port; 6: hybrid gas distributor; 7: ash silo; 8: ash-pushing machine; 9: gas mixer; 10: thermal insulation layer; 11: tower distribution device in gas-fluid; 12: the three water vapor inlet pipes; 13: reforming reactor; 14: the catalyzer feed bin; 15: uphill line; 16: remove pre-heat recovery system pipeline; 17: go to the clean tubulation of synthetic gas road; 18: descending pipeline; 19: threeway; 20: outer tube; 21: inner sleeve; 22: tensimeter; 23: blow-off valve; 24: thermal insulation layer; 25: ash removing hole; 26: get air valve; 27: tensimeter; 28: temperature indicator; 29: tower distribution apparatus base; 30: thermopair; 31: fire bars; 32: the gas mixer outlet; 33: the gas injection section; 34: the gas section of converging; 35: bending component; 36: flange.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is made and being further illustrated.
Embodiment 1
As illustrated in figs. 1 and 2, implement a kind of reforming reactor with hybrid gas distributor provided by the utility model, hybrid gas distributor 6 upper ends of adopting are provided with tower distribution apparatus 11, lower end is connected with gas mixer 9 by inner core, bottom righthand side is connected with threeway 19 pipelines, is respectively arranged with air intlet 2 and the first water vapor import 1 in threeway 19 pipelines.Tower distribution device in gas-fluid 11 diameters are 1/4 ~ 2/5 with the ratio of reactor diameter, mixer outlet 32 is higher than reactor bottom 50 ~ 150mm, tower sparger base 29 is higher than reactor bottom 160 ~ 250mm, tower distribution apparatus 11 is higher than reactor bottom 300 ~ 550mm, fire bars 31 is 45o ~ 60o with the angle of horizontal plane, and the set number of plies is 5 ~ 10 layers.The inner sleeve 21 of gas mixer is connected with urceolus 20 by flange 36, forms the sleeve channel architecture.Gas mixer 9 pipe diameters and Outer Tube diameter ratio are 1/2 ~ 4/5, gas mixer top is provided with thermopair 30, temperature indicator 28, tensimeter 27, gets air valve 26, is used for analyzing and detecting mixed gas composition, pressure and the temperature that enters in catalyticreactor.Gas mixer 9 torso portion are by rich CH
4 Combi inlet port 5, water vapor import 3, the gas section of converging 34, gas injection section 33, mixing device outlet 32 form, and, for preventing that water vapor was condensed into liquid water before entering mixing tank, in water vapor intake ducting periphery, are provided with thermal insulation layer 24 in addition; Hybrid gas distributor bottom is provided with blow-off valve 23, tensimeter 22, ash removing hole 25 for liquid water and the interior residual coal ash of peripheral conduits in time got rid of in pipeline.
Above-mentioned tower distribution apparatus 11 is to be communicated with the upwards conical shelves carbon slab of convergent on tower distribution apparatus 29, and successively downwards by being provided with the annular brace ring layer layer socket of several pneumatic outlets, then by circular baffle plate, bind and form tower-like distributed architecture.
Below by the reaction process of implementing the above-mentioned whole reactor of the utility model, embodiment of the present utility model is further illustrated.
As illustrated in figs. 1 and 2, a kind of reforming reaction technique of the reforming reactor with hybrid gas distributor, at first this technique be to blow intensification: namely be blown into air in reforming reactor 13, blow-time is 28 ~ 32s, in catalyst layer burning heat release, improve temperature of reactor, rise to 1100 ℃-1350 ℃, the blowing air after burning is through uphill line 15 and go residual neat recovering system pipeline 16 to enter residual neat recovering system.Next is to carry out water vapour cleaning: namely water vapor enters reforming reactor 13 through the first water vapor inlet pipe 1, cleaning time 1 ~ 3s, with remaining blowing air through uphill line 15 with go residual neat recovering system pipeline 16 to enter pre-heat recovery system.The 3rd is the gas processed of reforming: namely water vapor is through the second water vapor inlet pipe 3 and through rich CH
4The methane rich gas mixture that combi inlet port pipe 5 enters is in the interior mixing of hybrid gas mixer 11, then enter catalytic reforming reactor, carry out reforming reaction at the high temperature catalyst bed of material, the synthetic gas that makes through sleeve clearance channel, uphill line 15 and go synthetic gas only system pipeline 17 processed enter synthetic gas system processed only, then enter gas reservoir.Water vapor passes into time 28 ~ 32s, rich CH
4It is 18 ~ 22s that gas mixture passes into the time, rich CH
4Initial the passing into of gas mixture is later than water vapor 3 ~ 7s.The 4th is to carry out down blowing gas: namely water vapor enters reforming reactor 13 through the 3rd water vapor inlet pipe 12, down blowing gas time 62 ~ 68s, water vapor is from top to bottom through catalyzer bed of material gas processed, the synthetic gas that makes through descending pipeline 18 and go synthetic gas only system pipeline 17 processed enter synthetic gas system processed only.This stage is tended to balance material layer temperature.The 5th is that to carry out blowing up explosion-proof: namely water vapor enters reforming reactor 13 through the first water vapor inlet pipe 1, blowing up time 8 ~ 12s, through descending pipeline 15 and go synthetic gas only system pipeline 17 processed enter synthetic gas system processed only.This stage Main Function is that the synthetic gas of reforming reactor bottom is blown off, and for being blown into air, prepares.The 6th is to carry out air purging: namely air enters reforming reactor through air intlet pipe 1, blows off time 1 ~ 2s, will remain in reforming reactor and ducted synthetic gas through descending pipeline 15 and go synthetic gas only system pipeline 17 processed enter synthetic gas system processed only.
Claims (8)
1. with the reforming reactor of hybrid gas distributor, it is characterized in that: the top of described reforming reactor (13) is provided with the 3rd water vapour import (12), bottom is communicated with hybrid gas distributor (6) by tower distribution apparatus base (29), in the lower end of catalyzer feed bin (14), is provided with uphill line (15);
Described hybrid gas distributor (6) is to be communicated with formation by tower distribution device in gas-fluid (11) with gas mixer (9) and threeway (19); Wherein, the upper end of hybrid distribution device in gas-fluid (11) is that bottom is communicated with inner sleeve (21) and outer tube (20) by flange (36) by fire bars (31) the stack formation of some layers of umbrella-shaped structure; Inner sleeve (21) is communicated with rich CH
4Combi inlet port pipe (5) and the second water vapor inlet pipe (3); Outer tube (20) is communicated with threeway (19) and descending pipeline (18) by bending component (35).
2. the reforming reactor with hybrid gas distributor as claimed in claim 1, it is characterized in that: the diameter ratio of the diameter of described tower distribution device in gas-fluid (11) and reforming reactor (13) is 1/4 ~ 2/5, and is positioned at reactor bottom face 400 ~ 550mm place; The fire bars (31) of tower distribution device in gas-fluid (11) is 45o ~ 60o with the angle of horizontal plane, and the number of plies is 5 ~ 10 layers.
3. the reforming reactor with hybrid gas distributor as claimed in claim 1, it is characterized in that: the outlet (32) of described gas mixer (9) is higher than bottom face 50 ~ 150mm in reforming reactor.
4. the reforming reactor with hybrid gas distributor as claimed in claim 1, it is characterized in that: described tower sparger base (29) is higher than bottom face 160 ~ 250mm in reactor.
5. the reforming reactor with hybrid gas distributor as claimed in claim 1, it is characterized in that: described gas mixer (9) is set to respectively mixed gas outlet (32), gas injection section (33) and the gas section of converging (34) successively, and lower end is provided with rich CH
4Combi inlet port (5) and the second water vapor import (3).
6. the reforming reactor with hybrid gas distributor as claimed in claim 1, it is characterized in that: the diameter ratio of described inner sleeve (21) diameter and outer tube (20) is 1/2 ~ 4/5.
7. the reforming reactor with hybrid gas distributor as claimed in claim 1, it is characterized in that: the gas section of converging (34) of described hybrid gas distributor (6) and gas jet segment (33) inside are filled with stainless steel ripple filler.
8. the reforming reactor with hybrid gas distributor as claimed in claim 1, it is characterized in that: described threeway (19) is provided with the first water vapor import (1) and air intlet (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203266296U CN203284201U (en) | 2013-06-07 | 2013-06-07 | Reforming reactor with mixed type gas distributor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203266296U CN203284201U (en) | 2013-06-07 | 2013-06-07 | Reforming reactor with mixed type gas distributor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203284201U true CN203284201U (en) | 2013-11-13 |
Family
ID=49540575
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013203266296U Expired - Fee Related CN203284201U (en) | 2013-06-07 | 2013-06-07 | Reforming reactor with mixed type gas distributor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203284201U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103303865A (en) * | 2013-06-07 | 2013-09-18 | 太原理工大学 | Reforming reactor with mixed type gas distributor and process thereof |
-
2013
- 2013-06-07 CN CN2013203266296U patent/CN203284201U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103303865A (en) * | 2013-06-07 | 2013-09-18 | 太原理工大学 | Reforming reactor with mixed type gas distributor and process thereof |
| CN103303865B (en) * | 2013-06-07 | 2015-12-02 | 太原理工大学 | A kind of reforming reactor with hybrid gas distributor and technique thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN203668319U (en) | Biomass gasifying device | |
| CN103923705A (en) | Device and method for preparing hydrogen-rich gas by gasifying biomass | |
| CN108048140B (en) | Method and device for co-producing oil gas by pyrolysis and gasification coupling | |
| CN103303865B (en) | A kind of reforming reactor with hybrid gas distributor and technique thereof | |
| CN204211707U (en) | Utilize the device of coke-oven gas and blast furnace gas combination producing Sweet natural gas and liquefied ammonia | |
| US20150005399A1 (en) | Method and device for producing synthetic gas and method and device for synthesizing liquid fuel | |
| CN101293804B (en) | Fluidizer and method for preparing ethylene with ethanol dehydration | |
| CN106635113B (en) | A kind of device and method for improving tar yield through catalytic reforming using coke-stove gas as raw material | |
| CN201381844Y (en) | Catalyzing device for increasing underground coal gasification gas quality | |
| CN109399564B (en) | Device and method for preparing high-purity hydrogen by directly utilizing high-temperature coke oven crude gas | |
| CN106367122A (en) | Device and method for preparing synthetic gas by gasification of biomass carrier of oxygen | |
| CN203284201U (en) | Reforming reactor with mixed type gas distributor | |
| CN103045276A (en) | Pyrolyzing furnace for powdered coal | |
| CN106995724A (en) | A kind of system and method that water-gas is prepared with oven gas and water-coal-slurry | |
| CN206279172U (en) | A kind of biomass carrier of oxygen vaporizing system for synthesis gas device | |
| CN105623688A (en) | Powdered coal pyrolysis method through rapid reaction of hot carrier gas during lifting process | |
| CN201971794U (en) | Coal gasification furnace | |
| CN204589098U (en) | Utilize the pyrolysis of coal system of spouted bed bioreactor | |
| CN205061885U (en) | Carbon dioxide conversion device | |
| CN105368514B (en) | Produce the method and device of synthetic natural gas | |
| CN206109338U (en) | Coke oven gas methanation device with membrane separator | |
| CN103708417B (en) | A kind of method and device utilizing high-temperature vapor gasified bio-matter hydrogen making | |
| RU2679770C1 (en) | Thermal-chemical generator | |
| CN203700292U (en) | Carbonaceous substance reaction system | |
| CN206219524U (en) | Pot destroying process hydrocarbon gas combine coal gasification preparing synthetic gas apparatus and system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20131113 Termination date: 20160607 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |