CN104927924A - Protrusion type partition reactor - Google Patents
Protrusion type partition reactor Download PDFInfo
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- CN104927924A CN104927924A CN201510323043.8A CN201510323043A CN104927924A CN 104927924 A CN104927924 A CN 104927924A CN 201510323043 A CN201510323043 A CN 201510323043A CN 104927924 A CN104927924 A CN 104927924A
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- subregion
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Abstract
The invention relates to a protrusion type partition reactor. The protrusion type partition reactor comprises a reaction chamber 17 and a cooling chamber 20, the reaction chamber 17 is communicated with the cooling chamber 20 through a slag port 18, and the reaction chamber 17 and the cooling chamber 20 have the joint central axis. Compared with an existing gasifier, the protrusion type partition reactor has the advantages of being large in coal feeding amount, high in gasification efficiency, long in service life of a refractory lining and the like. Synthesis gas produced by utilizing the protrusion type partition reactor can be used as chemical engineering raw material gas and fuel gas, can be used for preparing hydrogen and synchronizing liquid fuels and the like, and is extremely wide in application.
Description
[technical field]
The invention belongs to clean energy efficient technique of rainwater utilization field.More specifically, the present invention relates to a kind of convex type subregion reactor.
[background technology]
Be that the gasification technology of raw material is widely used in synthetic ammonia, synthesizing methanol industry, the generating technical field such as (IGCC), coal liquifaction with hydrocarbon polymer, this reactor is producing synthesis gas CO+H
2key equipment, therefore, numerous scientific and technical personnel develop various types of reactor.In the entrained flow bed gasification technology of existing advanced person, the reactor of use comprises coal slurry gasifier, GSP, Xie Er powder coal gasification furnace etc.Meanwhile, according to the difference of feeding manner, furnace lining, number of nozzle and layout, described reactor can be divided into single-nozzle gasifier and multi nozzle of gasification furnace, different vapourizing furnaces has respective relative merits.
The advantage of single nozzle direct injection vapourizing furnace is structure and control is simple, cost is low, but because pressurized gasification process relates to high temperature, high pressure, fluid flowing under heterogeneous conditions and the chemical reaction process of associated transmittance process and complexity, single-nozzle gasifier production capacity is very restricted, and therefore cannot meet the demand of larger-scale unit development.
Multi-products production vapourizing furnace easily causes internal refractories ablation because flame field distribution is uneven, affects refractory brick work-ing life, thus also can have a strong impact on vapourizing furnace production capacity.
Therefore, in order to overcome above-mentioned prior art defect, the present inventor, on the basis of summing up prior art, by lot of experiments, completes the present invention finally.
[summary of the invention]
[technical problem that will solve]
The object of this invention is to provide a kind of convex type subregion reactor.
[technical scheme]
The present invention is achieved through the following technical solutions.
The present invention relates to a kind of convex type subregion reactor.
Convex type subregion reactor of the present invention comprises reaction chamber 17 and cooling room 20.Reaction chamber 17 is communicated with cooling room 20 by cinder notch 18, and reaction chamber 17 and cooling room 20 have common center axle;
Reaction chamber 17 reacts subregion 13 by a vertical reaction subregion 14 with even number side direction and forms; The side direction reaction subregion 13 of perpendicular configuration is set in the lower end of vertical reaction subregion 14, and they with vertically react the axisymmetric mode in subregion 14 center and configure; At vertical reaction subregion 14 top, nozzle 16 is set;
By vertically reacting subregion 14 and side direction, to react the region that subregion 13 forms be reaction zone; And the region be made up of straight length 11 lower rim wire and cinder notch 18 upper end of side direction reaction subregion 13 is reaction gas mixed flow region.
A preferred embodiment of the invention, vertical reaction subregion 14 reacts subregion 13 with side direction and is bell-jar structure, nozzle installing port 15 for installing nozzle 16 is all set at their top, the central axis of nozzle 16 and corresponding reaction regional center (RC) dead in line are installed.
A preferred embodiment of the invention, the angle that the longitudinal axis of vertical reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 30 °≤α≤150 °.
A preferred embodiment of the invention, the ratio that vertically reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 0.5 ~ 4.0.
A preferred embodiment of the invention, vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 0.2 ~ 3.0 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.
A preferred embodiment of the invention, reaction chamber 17 inwall lays refractory liner 7.
A preferred embodiment of the invention, arranges pressure tap 8 and temperature-measuring port 9 in cylindrical shell 10 bottom of reaction chamber 17 bottom.
A preferred embodiment of the invention, cooling room 20 is a kind of cylindrical tubes, arranges water cooler 6 at its top, and water cooler 6 upper end is connected with reaction chamber 17 lower end, and water cooler 6 lower end is connected with interior gas cylinder 3; At interior gas cylinder 3) outside outer gas cylinder 2 is set), and at interior gas cylinder 3) and outer gas cylinder 2) between form a circular channel;
Cooling room 20 cylindrical tube arranges liquidometer mouth 4, water-in 5 and syngas outlet 19 respectively; Heisui River outlet 1 is set in cooling room 20 bottom, and pulp water outlet 21 is set bottom cooling room 20).
In more detail the present invention will be described below.
The present invention relates to a kind of convex type subregion reactor.Convex type subregion reactor of the present invention can improve the Flow Field Distribution in existing traditional hot wall type gasifying reactor, improves the work-ing life of refractory liner; Can also be increased substantially by raising inlet amount with hydrocarbon polymer is material gasification producing synthesis gas CO+H
2the production capacity of device.
Convex type subregion reactor of the present invention comprises reaction chamber 17 and cooling room 20.Reaction chamber 17 is communicated with cooling room 20 by cinder notch 18, and reaction chamber 17 and cooling room 20 have common center axle;
Reaction chamber 17 reacts subregion 13 by a vertical reaction subregion 14 with even number side direction and forms.Side direction reaction subregion 13 is even number, and namely side direction reaction subregion 13 number is the integral multiple of 2 or 2, and relative between two to ensure side direction reaction subregion 13, place at grade, is conducive to reaction mass like this and fully mixes, reach gasification reaction fully and completely.In the present invention, such as, the number of side direction reaction subregion 13 is 2-12.
Vertical reaction subregion 14 reacts subregion 13 with side direction and is bell-jar structure, and their top all adopts round or ellipse end socket, and the other end of end socket is connected with the straight length of respective reaction subregion.These end socket central positions arrange nozzle installing port 15, and it is for installing nozzle 16; And the central axis of nozzle 16 and corresponding reaction regional center (RC) dead in line are installed.
The side direction reaction subregion 13 of perpendicular configuration is set in the lower end of vertical reaction subregion 14, and they with vertically react the axisymmetric mode in subregion 14 center and configure.
Preferably, the angle that vertically longitudinal axis of reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 30 °≤α≤150 °.
According to the present invention, if the angle α that the longitudinal axis of vertical reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is less than 30 °, the degree of mixing of the jet collision rift of each reaction zone then can be made bad, major part particle accelerates to flee from reaction chamber cinder notch, and part streams may be caused to have neither part nor lot in gasification reaction; If angle α is greater than 150 °, then side direction can be made to react the jet of subregion 13 and the jet collision rift vertically reacting subregion 14, and the jet of side direction reaction subregion 13 can be partial to side, furnace wall, can produce seriously wash away furnace wall refractory brick; Therefore, the angle α that vertically longitudinal axis of reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 30 °≤α≤150 ° is rational; More preferably 60 °≤α≤120 °.
According to the present invention, the ratio that vertically reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 0.5 ~ 4.0.If the ratio of H1 and H2 is less than 0.5, then can cause the high-temperature zone of reaction chamber 17 is moved, easily cause vertically reaction subregion 14 top overtemperature; If the ratio of H1 and H2 is greater than 4.0, the jet vertically reacting subregion 14 then can be made when colliding to have reached the degradation period of jet, and the jet of side direction reaction subregion 13 does not also carry out a gasification reaction just mutual shock, easily cause reaction chamber flow field irrational distribution, affect gasification index; Therefore, the ratio of H1 and H2 is 0.5 ~ 4.0 is appropriate, and preferably, the ratio of H1 and H2 is 1.0 ~ 3.0; More preferably, the ratio of H1 and H2 is 1.2 ~ 2.4.
According to the present invention, vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 0.2 ~ 3.0 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.If the ratio of H1 and H3 is less than 0.2, then the high-temperature zone of the room that can induce reaction is moved, cinder notch 18 temperature is too low, is unfavorable for that molten slag is discharged from cinder notch 18; If the ratio of H1 and H3 is greater than 3.0, then the percussion flow of vertically reaction subregion 14 and side direction reaction subregion 13 can be caused to cause cinder notch and to wash away, some particles also may be made not carry out gasification reaction completely simultaneously and just flee from slag notch 18; Therefore, the ratio of H1 and H3 is 0.2 ~ 3.0 is appropriate, and preferably, the ratio of H1 and H3 is 0.5 ~ 2.0; More preferably, the ratio of H1 and H3 is 0.6 ~ 1.2.
By vertically reacting subregion 14 and side direction, to react the region that subregion 13 forms be reaction zone; And the region be made up of straight length 11 lower rim wire and cinder notch 18 upper end of side direction reaction subregion 13 is reaction gas mixed flow region.
In the present invention, reaction chamber 17 inwall lays refractory liner 7.Refractory liner 7 is the refractory liners building block with highiy refractory brick, and described highiy refractory brick is product sold in the market, such as by Luoyang Refractory Institute Co., Ltd., SINO Steel Corporation with trade(brand)name high-chrome brick product sold.
According to the present invention, arrange pressure tap 8 and temperature-measuring port 9 in cylindrical shell 10 bottom of reaction chamber 17 bottom, they are respectively used to setting pressure detector and hygrosensor, so that the pressure of Real-Time Monitoring reactor when it runs and temperature variation.
In the present invention, cooling room 20 is a kind of cylindrical tubes, arranges water cooler 6 at its top, and water cooler 6 upper end is connected with reaction chamber 17 lower end, and water cooler 6 lower end is connected with interior gas cylinder 3; Outer gas cylinder 2 is set outside interior gas cylinder 3, and forms a circular channel between interior gas cylinder 3 and outer gas cylinder 2.
Cooling room 20 cylindrical tube arranges liquidometer mouth 4, water-in 5 and syngas outlet 19 respectively, and wherein water-in 5 and syngas outlet 19 are positioned at the top of cooling room 20; Arrange Heisui River outlet 1 in cooling room 20 bottom, and bottom cooling room 20, arrange pulp water outlet 21, wherein Heisui River outlet 1 exports with pulp water the bottom that 21 are positioned at cooling room 20.
According to the present invention, be wherein that one or more are selected from containing hydrocarbon raw material slurry, pressed powder containing feedstock hydrocarbon or the gaseous state raw material containing feedstock hydrocarbon by the gasified raw material of nozzle 16.Preferably, containing hydrocarbon raw material slurry be the slurry be made up of coal dust, refinery coke, coke powder, semicoke, coal liquefaction residue and composition thereof.Pressed powder is coal dust, coke powder etc. and their mixture containing feedstock hydrocarbon.Gaseous state is CH containing feedstock hydrocarbon
4gas.
In the present invention, need to pass into O while passing into gasified raw material
2main gasifying medium, suitably can also pass into H
2o, CO
2or their mixture is as auxiliary gasifying medium.
When using convex type subregion reactor of the present invention to prepare synthetic gas, the operational condition of control is as follows:
Temperature of reaction is 1100 DEG C-1650 DEG C, and working pressure is 0.1-20MPa, and deslagging mode is slag tap or dry ash extraction.
According to the present invention, the mutual independent operation of multiple nozzles of convex type subregion reactor, these nozzles can be allowed slurry, pressed powder or gaseous state to be sprayed into reaction chamber containing feedstock hydrocarbon and oxygenant simultaneously, also can allow one of them or several nozzle that slurry, pressed powder or gaseous state are sprayed into reaction chamber containing feedstock hydrocarbon and oxygenant, and the inlet amount of each nozzle also can be different.
Allowing these nozzles simultaneously and with identical amount, slurry, pressed powder or gaseous state being sprayed into reaction chamber containing feedstock hydrocarbon and oxygenant is a specific embodiment.
Convex type subregion reactor implementation process of the present invention is as follows: first one or more are selected from slurry, pressed powder or gaseous state and extremely vertically react subregion 14 top jet nozzle 16 containing feedstock hydrocarbon and oxygenant through positive delivery, after nozzle 16 is atomized, spray into high temperature containing feedstock hydrocarbon together with oxygenant and vertically react subregion 14, generating portion oxidizing reaction under the hot environment of vertically reacting subregion 14, generates with CO, CO
2and H
2for the crude synthesis gas of main component.
Then, one or more are selected from slurry, pressed powder or gaseous state and react the nozzle 16 of subregion 13 containing feedstock hydrocarbon and oxygenant through positive delivery to side direction, after nozzle 16 is atomized, high temperature side is sprayed into reaction subregion 13 together with oxygenant containing feedstock hydrocarbon, generating portion oxidizing reaction under the hot environment of side direction reaction subregion 13, generates with CO, CO
2and H
2for the crude synthesis gas of main component.What spray from each nozzle collides with the medullary ray intersection vertically reacting subregion 14 at side direction reaction subregion 13 in the unreacted streams of each reaction subregion, temperature 1100 DEG C-1650 DEG C, pressure is, under the condition of 0.1-20MPa, secondary combustion and gasification reaction occur, and generates with CO, CO
2and H
2for the synthetic gas of main component, synthetic gas, the lime-ash of generation enter cooling room 20 by reaction chamber 17 bottom cinder notch 18.
Cooling room 20 top is provided with water cooler 6, and water coolant enters from water-in 5, directly enters water cooler 6 cavity from bottom to top, and after being full of chilled water in water cooler 6 inner chamber body, overflow is to interior gas cylinder 3 inwall.Inner at interior gas cylinder 3, water coolant and the high-temperature synthesis gas of discharging from reactor cinder notch 18 also flow and and carry out heat exchange, partial-chilled water vapor also carries out quenching, cooling to synthetic gas and slag.The synthetic gas of cooling declines along interior gas cylinder 3 inside and enters the bottom water-bath of cooling room 20, after cooling washing further, rise along on the circular channel between outer gas cylinder 2 and interior gas cylinder 3, discharge through outer gas cylinder 2 upper outlet, finally leave this reactor from syngas outlet 19, enter follow-up system and process.
The lime-ash that cinder notch 18 is discharged drops to the water-bath district of cooling room 20 bottom in interior gas cylinder 3 after cooling, and the lime-ash through cooling twice discharges this reactor from pulp water outlet 21.Circulation Heisui River is discharged from Heisui River outlet 1, and lime-ash exports 21 by pulp water and discharges.Liquidometer mouth 4 is equipped with in cooling room 20 outside, for installing liquidometer, and monitors the liquid level change of cooling room.
Compared with current existing vapourizing furnace, convex type subregion reactor of the present invention has the features such as coal feeding amount is large, gasification efficiency is high, refractory liner long service life.The synthetic gas using convex type subregion reactor of the present invention to produce can be used as material gas, fuel gas, hydrogen manufacturing, synthetic liquid fuel etc., and purposes is very extensive.
[beneficial effect]
The invention has the beneficial effects as follows:
Reaction chamber of the present invention is reacted subregion by multiple side direction and is vertically reacted subregion and forms, and increasing substantially of reactor production capacity, is adapted to the suitability for industrialized production needs of large charging capacity gasification installation reactor.
The present invention adopts side direction to react subregion and vertically reaction subregion charging simultaneously, first time partial oxidation reaction is there is under hydrocarbon polymer and the oxygenant hot environment first in vertical reaction subregion and side direction reaction subregion, the jet do not reacted collides in the center of reaction chamber, there is second time burning and gasification reaction, synthetic gas index can be effectively improved by secondary reaction, improve the thermo parameters method in reactor, and reduce high temperature logistics washing away inside reactor refractory liner.
The present invention adopts multiple feed nozzle and multiple reaction subregion, the gasified raw material of can simultaneously gasify different sorts, different flow, flexible configuration, can carry out adjusting and distributing according to application enterprise practical situation.
[accompanying drawing explanation]
Fig. 1 is the structural representation of convex type subregion reactor of the present invention;
In figure:
In the outlet of 1-Heisui River, the outer gas cylinder of 2-, 3-, gas cylinder, 4-liquidometer mouth, 5-water-in, 6-water cooler, 7-refractory liner, 8-pressure tap, 9-temperature-measuring port, 10-cylindrical shell, 11-straight length, 12-end socket, 13-side direction reaction subregion, 14-vertically react subregion, 15-nozzle installing port, 16-nozzle, 17-reaction chamber, 18-cinder notch, 19-syngas outlet, 20-cooling room, the outlet of 21-pulp water.
[embodiment]
The present invention can be understood better by following embodiment.
Embodiment 1: convex type subregion reactor of the present invention
The embodiment of this embodiment is as follows:
Convex type subregion reactor of the present invention comprises reaction chamber 17 and cooling room 20.Reaction chamber 17 is communicated with cooling room 20 by cinder notch 18, and reaction chamber 17 and cooling room 20 have common center axle; Reaction chamber 17 inwall is equipped with the refractory liner 7 that highiy refractory brick builds block.
Reaction chamber 17 reacts subregion 13 by a vertical reaction subregion 14 with 2-12 side direction and forms, vertical reaction subregion 14 reacts subregion 13 with side direction and is bell-jar structure, nozzle installing port 15 for installing nozzle 16 is all set at their top, the central axis of nozzle 16 and corresponding reaction regional center (RC) dead in line are installed; The side direction reaction subregion 13 (longitudinal axis namely vertically reacting subregion (14) and side direction react the longitudinal axis of subregion (13) angle α be 90 °) of perpendicular configuration is set in the lower end of vertical reaction subregion 14, and they are to react the axisymmetric mode in subregion 14 center configure with vertical; At vertical reaction subregion 14 top, nozzle 16 is set; The ratio that vertical reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 3.0.Vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 0.6 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.
By vertically reacting subregion 14 and side direction, to react the region that subregion 13 forms be reaction zone; And the region be made up of straight length 11 lower rim wire and cinder notch 18 upper end of side direction reaction subregion 13 is reaction gas mixed flow region.
Pressure tap 8 and temperature-measuring port 9 are set in cylindrical shell 10 bottom of reaction chamber 17 bottom.
Cooling room 20 is a kind of cylindrical tubes, arranges water cooler 6 at its top, and water cooler 6 upper end is connected with reaction chamber 17 lower end, and water cooler 6 lower end is connected with interior gas cylinder 3; Outer gas cylinder 2 is set outside interior gas cylinder 3, and forms a circular channel between interior gas cylinder 3 and outer gas cylinder 2;
Cooling room 20 cylindrical tube arranges liquidometer mouth 4, water-in 5 and syngas outlet 19 respectively; Heisui River outlet 1 is set in cooling room 20 bottom, and pulp water outlet 21 is set bottom cooling room 20.
Embodiment 2: convex type subregion reactor of the present invention
The embodiment of this embodiment and the identical of embodiment 1, just arrange side direction reaction subregion 13 in the lower end of vertically reacting subregion 14, and the angle α that the longitudinal axis of vertical reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 30 °.The ratio that vertical reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 1.0.Vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 0.2 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.
Embodiment 3: convex type subregion reactor of the present invention
The embodiment of this embodiment and the identical of embodiment 1, just arrange side direction reaction subregion 13 in the lower end of vertically reacting subregion 14, and the angle α that the longitudinal axis of vertical reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 150 °.The ratio that vertical reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 2.4.Vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 3.0 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.
Embodiment 4: convex type subregion reactor of the present invention
The embodiment of this embodiment is identical with embodiment 1, just arranges side direction reaction subregion 13 in the lower end of vertically reacting subregion 14, and the angle α that the longitudinal axis of vertical reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 60 °.The ratio that vertical reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 0.5.Vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 0.5 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.
Embodiment 5: convex type subregion reactor of the present invention
The embodiment of this embodiment is identical with embodiment 1, just arranges side direction reaction subregion 13 in the lower end of vertically reacting subregion 14, and the angle α that the longitudinal axis of vertical reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 120 °.The ratio that vertical reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 4.0.Vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 2.0 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.
Embodiment 6: convex type subregion reactor of the present invention
The embodiment of this embodiment is identical with embodiment 1, just arranges side direction reaction subregion 13 in the lower end of vertically reacting subregion 14, and the angle α that the longitudinal axis of vertical reaction subregion 14 and side direction react the longitudinal axis of subregion 13 is 100 °.The ratio that vertical reaction subregion 14 length H1 and side direction react subregion 13 length H2 is 1.2.Vertical reaction subregion 14 height H 1 on reaction chamber 17 top is 1.2 with the ratio of cylindrical shell 10 height H 3 in reaction chamber 17 bottom.
Claims (8)
1. a convex type subregion reactor, this subregion reactor comprises reaction chamber (17) and cooling room (20), it is characterized in that reaction chamber (17) is communicated with cooling room (20) by cinder notch (18), and reaction chamber (17) and cooling room (20) has common center axle;
Reaction chamber (17) vertically reacts subregion (14) and even number side direction by one and reacts subregion (13) and form; Side direction reaction subregion (13) of perpendicular configuration is set in the lower end of vertically reacting subregion (14), and they with vertically react the axisymmetric mode in subregion (14) center and configure; Nozzle (16) is set vertically reacting subregion (14) top;
By vertically reacting subregion (14) and side direction, to react the region that subregion (13) forms be reaction zone; And to react by side direction the region that straight length (11) the lower rim wire of subregion (13) and cinder notch (18) upper end form be reaction gas mixed flow region.
2. convex type subregion reactor according to claim 1, it is characterized in that vertically reacting subregion (14) to react subregion (13) with side direction and be bell-jar structure, nozzle installing port (15) for installing nozzle (16) is all set at their top, the central axis of nozzle (16) and corresponding reaction regional center (RC) dead in line are installed.
3. convex type subregion reactor according to claim 1, it is characterized in that vertically reacting the angle that the longitudinal axis of subregion (14) and side direction react the longitudinal axis of subregion (13) is 30 °≤α≤150 °.
4. convex type subregion reactor according to claim 1, it is characterized in that vertically reacting the ratio that subregion (14) length H1 and side direction react subregion (13) length H2 is 0.5 ~ 4.0.
5. convex type subregion reactor according to claim 1, is characterized in that vertical reaction subregion (14) height H 1 on reaction chamber (17) top is 0.2 ~ 3.0 with the ratio of cylindrical shell (10) height H 3 in reaction chamber (17) bottom.
6. convex type subregion reactor according to claim 1, is characterized in that laying refractory liner (7) on reaction chamber (17) inwall.
7. convex type subregion reactor according to claim 1, is characterized in that arranging pressure tap (8) and temperature-measuring port (9) in cylindrical shell (10) bottom of reaction chamber (17) bottom.
8. convex type subregion reactor according to claim 1, it is characterized in that cooling room (20) is a kind of cylindrical tube, water cooler (6) is set at its top, water cooler (6) upper end is connected with reaction chamber (17) lower end, and water cooler (6) lower end is connected with interior gas cylinder (3).Outer gas cylinder (2) is set outside interior gas cylinder (3), and forms a circular channel between interior gas cylinder (3) and outer gas cylinder (2);
Cooling room (20) cylindrical tube arranges liquidometer mouth (4), water-in (5) and syngas outlet (19) respectively; Heisui River outlet (1) is set in cooling room (20) bottom, and pulp water outlet (21) is set in cooling room (20) bottom.
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| CN104449868A (en) * | 2013-09-24 | 2015-03-25 | 中国石油大学(华东) | Entrained flow gasifier for swirling melt cinder solidification |
| CN204752637U (en) * | 2015-06-12 | 2015-11-11 | 西安元创化工科技股份有限公司 | Protruding formula subregion reactor |
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2015
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| CN202912915U (en) * | 2012-03-23 | 2013-05-01 | 任相坤 | Multi-furnace head water cooled wall coal water slurry gasifier |
| CN103320172A (en) * | 2012-03-23 | 2013-09-25 | 王庆 | Water wall coal water slurry gasifier provided with plurality of ignition furnace heads |
| CN202849349U (en) * | 2012-06-04 | 2013-04-03 | 上海锅炉厂有限公司 | Dry pulverized coal graded compression gasification device |
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