CN103937552B - A kind of three-section type entrained flow bed coal hydrogenation gasification stove and combined operation system - Google Patents
A kind of three-section type entrained flow bed coal hydrogenation gasification stove and combined operation system Download PDFInfo
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- CN103937552B CN103937552B CN201410110834.8A CN201410110834A CN103937552B CN 103937552 B CN103937552 B CN 103937552B CN 201410110834 A CN201410110834 A CN 201410110834A CN 103937552 B CN103937552 B CN 103937552B
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- return passage
- combustion chamber
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- back flow
- flow plate
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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 present invention discloses a kind of three-section type entrained flow bed coal hydrogenation gasification stove, comprise cylindrical body of heater substantially, described body of heater comprises combustion chamber, return passage and upper vaporizer, the end opening of the suitable for reading and return passage of described combustion chamber is connected by reducing throat, and the end opening of the suitable for reading and upper vaporizer of described return passage is connected by reducing throat; Arranged tangential combustion chamber burner on the lower sides of described combustion chamber, on the lower inside wall of described return passage, centering is provided with return passage nozzle, the top of described return passage nozzle is provided with a cone shape back flow plate, and described back flow plate also and between the sidewall of return passage has gap on the central axis of return passage.Back flow plate can limit pulverized coal particle and first enter recirculating zone, and backflow can improve the residence time of pulverized coal particle to a certain extent, thus improves the transformation efficiency of gasification, improves integral coal gasification efficiency.
Description
Technical field
The present invention relates to a kind of coal gasifier.More specifically, a kind of three-section type entrained flow bed coal hydrogenation gasification burner is related to.
Background technology
Energy dilemma and environmental pollution have become the dual-pressure hindering social development.Solve this two problems, can carry out respectively from immediate development and Long-and Medium-term Development two angles.On the one hand, China and even world's Long-and Medium-term Development be adapted to, should new cleaning fuel be greatly developed, biological example matter fuel, sun power, water energy, wind energy, combustible ice, nuclear energy and Geothermal energy etc., fundamentally solve the problem of energy dilemma and environmental pollution.But this process is relatively slow, in the short period of time, novel energy difficulty becomes leading role, and short-term (or transitional period) of therefore still needing on the basis of Long-term planning is planned.As everyone knows, coal is one of the main energy sources in China and even the world, compares in other Energy resources such as oil, Sweet natural gas, the features such as it is huge that coal has reserves, and price is more cheap.Whole world rich coal resources, in more than 40 country of proven reserve, conservative estimation also can resupply the mankind and use 200 years.And under comparing, the oil and gas of proven reserve then can only support decades.Therefore can predict, the status of coal in world energy sources is unshakable, and in the near future can ever more important.Coal once played main energy resource supply role in human industryization process, since entering for 20th century, exploit in a large number along with oil, natural gas source and utilize, and emerging energy is as the development of the technology such as wind energy, water energy, nuclear power, coal proportion in world's energy expenditure declines to some extent, but still occupies critical role.In predictable future, fossil energy will be still the main body energy in China and even the world, and according to predicting the outcome of the Eergy Office of State Council etc. 2007, will account for 81% of the consumption of Chinese primary energy source to the year two thousand thirty fossil oil, wherein coal accounts for 52.9%; To account for 71.5% of Chinese primary energy source consumption to the year two thousand fifty fossil oil, wherein coal accounts for 43.9%.First visible development low-carbon economy, reducing emission of carbon dioxide will pay attention to saving use and the Appropriate application of fossil energy.Thus, the efficient clean utilization technology of Development of Coal all has profound significance in China and even the world.
Coal gasification technology is the basis of numerous cleaning coal utilization technology, has more than 200 years history so far.Develop the common recognition having become energy field scientific and technological circle and business circles based on the coal-based energy of gasification and chemical system, also become hot spot technology that is efficient in world wide, clean, development and utilization coal economically and important development direction.The technical process of gasification has a lot, by the calorific value classification of producing coal gas, coal gasification method can be divided into: 1) produce caloric power of gas lower than 8347kJ/m
3low calorific value coal gas method; 2) caloric power of gas is produced at 16747-33494kJ/m
3middle calorific value of gas method; 3) caloric power of gas is produced higher than 33494kJ/m
3high combustion value coal gas method.Can be divided into by heat-supplying mode: 1) autothermal evaporating method, does not namely have extraneous heat supply in gasification projects, the heat needed for gasification is provided by the heat produced that gasifies; 2) indirect heating evaporating method, namely gasification reaction is originally as thermo-negative reaction, thus needs the input of external heat; 3) steam gasification of coal and hydrogasification combine method, and this method is used for providing the heat needed for coal steam gasification by the heat that coal hydrogenation gasification produces; 4) thermal barrier heat supply, namely in an independent reactor, carry out heat supply with coal or coke and air combustion heat hot carrier, thermal barrier can be solid, liquid fused salt or slag.Can be divided into by vaporized chemical classification: 1) air-steam evaporating method, namely using air and steam as vaporized chemical, air is by coal partial oxidation and produce heat, and steam then carries out gasification reaction with the product of partial oxidation further; 2) oxygen-steam evaporating method, namely using industrial oxygen and water vapour as vaporized chemical, principle and air-steam evaporating method similar; 3) hydrogen evaporating method, namely with H
2or be rich in H
2gas as vaporized chemical, can generate and be rich in CH
4coal gas.Can be divided into by solid-fuelled kinestate classification: 1) moving-bed (fixed bed) evaporating method; 2) fluidized-bed gasification method; 3) entrained flow gasification method.In coal in China gasifying process, using maximum is fixed bed gasification technique, as lurgi pressure gasifier, normal pressure producer, type of furnace two-stage furnace, water-gas generators, water-gas type two-stage furnace etc. occurs.
In numerous Coal Gasification Technology, coal hydrogenation gasification technology is subject to the extensive concern of Chinese scholars because of tool lot of advantages.Such as, coal hydrogenation gasification is thermopositive reaction, does not thus need extra oxygen to carry out combustion heat release; The direct product of coal hydrogenation gasification is CH
4, thus do not need extra CH
4generate stove; The thermo-efficiency of coal hydrogenation gasification is very high, close to 80%; Coal hydrogenation gasification reaction does not need catalyzer.In addition, the such as IGCC of coal hydrogenation gasification or multiple clean coal power generation system and the fuel source of coal-based near zero release power generation system (ZEC).
There is following problem in vapourizing furnace of the prior art, the gas that gasification produces can rise in vapourizing furnace, but when the upwelling movable property life of the gas in vapourizing furnace is uneven, carbon (coal tar) sometimes in coal fully generating gasification flows out from vapourizing furnace before reacting, and reactivity (carbon in coal is to the transformation efficiency of gas reforming) is reduced.Therefore, need to provide a kind of coal can be made to react fully in compact reaction vessel, there is high efficiency coal hydrogenation gasification stove.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of coal hydrogenation gasification stove, this vapourizing furnace can make the distribution of pulverized coal particle in vapourizing furnace be tending towards all with, improve the residence time of pulverized coal particle in stove, thus improve the transformation efficiency of coke, improve integral coal gasification efficiency.
For solving the problems of the technologies described above, the present invention adopts following technical proposals:
A kind of three-section type entrained flow bed coal hydrogenation gasification stove, comprise combustion chamber, return passage and upper vaporizer, the end opening of the suitable for reading and return passage of described combustion chamber is fixedly connected with, and is connected between the suitable for reading and end opening of upper vaporizer of described return passage in undergauge shape; Described return passage sidewall aims at its central axis and is provided with return passage nozzle, the top of described return passage nozzle is provided with one in funnelform back flow plate; The circular in cross-section structure of described back flow plate, vertical section is ladder structure; The central axis of described back flow plate and the central axes of return passage, and between the plate body of back flow plate and the inner side-wall of return passage, there is gap.Described back flow plate can make the air-flow of rising downwards and upwards flow from the gap location between back flow plate and the inner side-wall of return passage, thus backflow is formed in return passage, extend the residence time raising transformation efficiency of pulverized coal particle in return passage, the formation commutating zone, position in undergauge shape between the suitable for reading and end opening of upper vaporizer of described return passage, described commutating zone can make to be positioned at the outside pulverized coal particle upwards vaporizer centre flowing near return passage, pulverized coal particle is uniformly distributed in upper vaporizer, thus improves the transformation efficiency of coal dust.
Preferably, described return passage nozzle is bilayer structure, and it comprises the outer tube for spraying into hydrogen in return passage and arranges manages for spraying in return passage in carbonic acid gas and coal dust within the outer tube.
Preferably, in the inner side-wall same level of described combustion chamber, circumferentially uniform intervals is provided with combustion chamber burner, by from the axis of described each combustion chamber burner during the top view of described combustion chamber with centered by the central axis of described combustion chamber and the diameter imaginary circle less than the internal diameter of combustion chamber configures described combustion chamber burner around the mode that same direction is tangent.
Preferably, described combustion chamber burner is bilayer structure, and it comprises the outer tube for spraying into hydrogen in combustion chamber and arranges manages for spraying in combustion chamber in oxygen within the outer tube.
Preferably, the bottom even of described back flow plate is provided with four supporting legs, and described supporting leg is installed on the inner side-wall of described return passage.
The combined operation system comprising three-section type entrained flow bed coal hydrogenation gasification stove comprises vapourizing furnace, reforming furnace and a calcining furnace, is provided with the first pipeline between the outlet of described vapourizing furnace and reforming furnace, and the first pipeline is provided with the first diverting valve; Between described reforming furnace and calcining furnace, the CaO be provided with for being produced by calcining furnace is transported to the second pipeline in reforming furnace and is used for the CaCO that produced by reforming furnace
3be transported to the 3rd pipeline in calcining furnace; Be provided with the 4th pipeline between described reforming furnace and vapourizing furnace, described 4th pipeline is provided with the second diverting valve, and two outlets of described second diverting valve connect the outer tube of combustion chamber burner and the outer tube of return passage nozzle respectively; The 5th pipeline is provided with between the return passage nozzle of described calcining furnace and vapourizing furnace.
Beneficial effect of the present invention is as follows:
Back flow plate can produce backflow in return passage central region, backflow can improve the residence time of pulverized coal particle to a certain extent, the effect of commutating zone is the centrifugal force of offsetting eddy flow generation, the pulverized coal particle flowed from back flow plate lateral is assembled towards vaporizer center, thus makes the distribution of pulverized coal particle in vaporizer be tending towards even.Thus, adopt this three-section type entrained flow bed hydrogasification stove can improve the transformation efficiency of coke further, improve integral coal gasification efficiency.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in further detail.
Fig. 1 illustrates structural representation of the present invention.
Fig. 2 illustrates the cross sectional representation of combustion chamber of the present invention.
Fig. 3 illustrates the structural representation of back flow plate of the present invention.
Fig. 4 illustrates the structured flowchart of combined operation system of the present invention.
Embodiment
In order to be illustrated more clearly in the present invention, below in conjunction with preferred embodiments and drawings, the present invention is described further.Parts similar in accompanying drawing represent with identical Reference numeral.It will be appreciated by those skilled in the art that specifically described content is illustrative and nonrestrictive, should not limit the scope of the invention with this below.
As shown in Figures 1 to 3, a kind of three-section type entrained flow bed coal hydrogenation gasification stove comprises cylindrical body of heater 1 substantially, body of heater comprises combustion chamber 10, return passage 20 and vaporizer 30, be connected in undergauge shape between the suitable for reading and end opening of return passage of combustion chamber 10, the end opening suitable for reading and upper vaporizer 30 of return passage 20 is that undergauge shape is connected, the formation commutating zone, undergauge place suitable for reading 21 of return passage 20.On the lower inside wall of return passage 20, centering is provided with return passage nozzle 22, the top of return passage nozzle 22 is provided with the back flow plate 23 of upside down funnel shape, the circular in cross-section structure of back flow plate 23, vertical section is ladder structure, back flow plate 23 is fixed on the central axis of return passage 20 by the supporting leg of bottom, has gap between the inner side-wall of back flow plate 23 and return passage 20.In the inner side-wall same level of combustion chamber 10, circumferentially uniform intervals is provided with combustion chamber burner 11, and the axis of each combustion chamber burner 11 is with centered by the central axis of combustion chamber 10 and the diameter imaginary circle less than the internal diameter of combustion chamber 10 arranges combustion chamber burner 11 around the mode that same direction is tangent.Combustion chamber burner 11 and return passage nozzle 22 are bilayer structure, and combustion chamber burner 11 center sprays into oxygen, and skin sprays into hydrogen.Return passage nozzle 22 center sprays into carbonic acid gas and coal dust, and skin sprays into hydrogen.
In vapourizing furnace, vapor pressure is chosen as 7MPa, oxygen and hydrogen quality ratio are 1.5, to spray into from combustion chamber burner 11 with higher inlet velocity (15m/s) and burn, producing high-temperature gas mixture agent (hydrogen and the water vapour) eddy flow of about 1600 DEG C.The hydrogen quality of remaining after combustion and always enter coal mass ratio and be set as 0.3.In vapourizing furnace, air input suitably can be adjusted by coal input quantity, and such as setting coal input quantity is about 5kg/s, to ensure that gas velocity can make to form air flow bed in vapourizing furnace.High-temperature gas mixture agent in combustion chamber 10 enters in return passage 20 after aditus laryngis, mix with the coal dust sprayed into from return passage nozzle 22 and remaining hydrogen and a small amount of carbonic acid gas in return passage 20, wherein the amount of carbonic acid gas can coal powder injection speed as required regulate.Coal dust is after entering return passage 20, and its movement locus is first towards the central motion of return passage 20, and meanwhile, coal dust can be subject to the drag effect spiral of swirling eddy and have the trend of outwards moving because being subject to centrifugal action.Under the drive of return passage 20 bottom upstream and under the restriction of back flow plate 23, the pulverized coal particle sprayed into enters recirculating zone 24.In recirculating zone 24; air stream axle is downward to velocity reversal; simultaneously because particle is subject to action of gravity; therefore after moving upward to certain distance can then move downward; due to centrifugal action; the particle fallen can be subject to the drive of fair speed air-flow in back flow plate 23 bottom outside and rise from back flow plate outer helical, and finally upwards vaporizer 30 center gathering again under the effect of commutating zone 21, to offset the effect of centrifugal force.The coke granule of the synthetic gas that vapourizing furnace produces and flying dust and non-complete reaction is overflowed from furnace roof.
As shown in Figure 4, a kind of combined operation system using above-mentioned vapourizing furnace, comprises vapourizing furnace 1, reforming furnace 200 and calcining furnace 300, is provided with the first pipeline 100, first pipeline 100 and is provided with the first diverting valve 101 between the outlet of described vapourizing furnace 1 and reforming furnace 200; Between described reforming furnace 200 and calcining furnace 300, the CaO be provided with for being produced by calcining furnace 300 is transported to the second pipeline 400 in reforming furnace 200 and is used for the CaCO that produced by reforming furnace 200
3be transported to the 3rd pipeline 500 in calcining furnace 300; Be provided with the 4th pipeline 600 between described reforming furnace 200 and vapourizing furnace 1, described 4th pipeline 600 is provided with the second diverting valve 601, and two outlets of described second diverting valve 601 connect the outer tube of combustion chamber burner and the outer tube of return passage nozzle respectively; The 5th pipeline 700 is provided with between described calcining furnace 300 and the return passage nozzle 22 of vapourizing furnace 1.
The rich CH that vapourizing furnace 1 produces
4synthetic gas is divided into two portions by the first diverting valve 101: a part of rich CH
4synthetic gas can use as industrial chemicals or fuel (for internal combustion turbine or fuel cell etc.); The rich CH of another part
4synthetic gas enters reforming furnace 200, in reforming furnace 200, add H
2o generates H
2and CO
2gas mixture, reforming furnace 200 produce CO
2caCO is generated by the CaO trapping that calcining furnace is transported by the second pipeline 400
3, the H that reforming furnace 200 produces
2the outer tube of combustion chamber burner and the outer tube of return passage nozzle is transported to respectively by the 4th pipeline 600 and the second diverting valve 601.CaCO
3entered in calcining furnace 300 by the 3rd pipeline 500 and carry out calcining generation CaO and CO
2, the carbon of non-complete reaction can as the part of heat energy of calcining furnace 300.The CaO circulation that calcining furnace 300 generates enters in reforming furnace 200 carries out CO
2trapping, the CO that calcining furnace 300 produces
2vapourizing furnace and H is entered from pipe in return passage nozzle by the 5th pipeline 700
2pulverized coal conveying together.This vapourizing furnace combined operation system can realize H
2and CO
2self-sufficient.
Obviously; the above embodiment of the present invention is only for example of the present invention is clearly described; and be not the restriction to embodiments of the present invention; for those of ordinary skill in the field; can also make other changes in different forms on the basis of the above description; here cannot give exhaustive to all embodiments, every belong to technical scheme of the present invention the apparent change of extending out or variation be still in the row of protection scope of the present invention.
Claims (8)
1. a three-section type entrained flow bed coal hydrogenation gasification stove, comprise body of heater, it is characterized in that: described body of heater comprises combustion chamber, return passage and upper vaporizer, the end opening of the suitable for reading and return passage of described combustion chamber is fixedly connected with, and is connected between the suitable for reading and end opening of upper vaporizer of described return passage in undergauge shape; Described return passage sidewall aims at its central axis and is provided with return passage nozzle, the top of described return passage nozzle is provided with one in funnelform back flow plate; The circular in cross-section structure of described back flow plate, vertical section is ladder structure; The central axis of described back flow plate and the central axes of return passage, and between the plate body of back flow plate and the inner side-wall of return passage, there is gap.
2. vapourizing furnace according to claim 1, is characterized in that: described return passage nozzle is sleeve structure; It comprises the outer tube for spraying into hydrogen in return passage and arranges manages for spraying in return passage in carbonic acid gas and coal dust within the outer tube.
3. vapourizing furnace according to claim 1, it is characterized in that: in the sidewall same level of described combustion chamber, circumferentially uniform intervals is provided with combustion chamber burner, centered by the central axis of described combustion chamber, arrange the imaginary circle that a diameter is less than combustion chamber internal diameter, the axis of described combustion chamber burner is around same direction and the tangent setting of this imaginary circle.
4. vapourizing furnace according to claim 3, is characterized in that: described combustion chamber burner is sleeve structure; It comprises the outer tube for spraying into hydrogen in combustion chamber and arranges manages for spraying in combustion chamber in oxygen within the outer tube.
5. vapourizing furnace according to claim 1, is characterized in that: the bottom of described back flow plate is provided with supporting leg, and described supporting leg is installed on the inner side-wall of described return passage.
6. vapourizing furnace according to claim 5, is characterized in that: the cone angle of described back flow plate is 30 °, and back flow plate is 1/3 of return passage height together with the total height of supporting leg, and the height of described supporting leg is 1/3 of back flow plate height.
7. vapourizing furnace according to claim 1, is characterized in that: described return passage nozzle is arranged on the lower position of return passage.
8. one kind comprise as arbitrary in claim 1 ~ 7 as described in the combined operation system of vapourizing furnace, it is characterized in that: this system comprises vapourizing furnace, reforming furnace and calcining furnace, be provided with the first pipeline between the outlet of described vapourizing furnace and reforming furnace, this first pipeline is provided with the first diverting valve;
Between described reforming furnace and calcining furnace, the CaO be provided with for being produced by calcining furnace is transported to the second pipeline in reforming furnace and is used for the CaCO that produced by reforming furnace
3be transported to the 3rd pipeline in calcining furnace;
Also be provided with the 4th pipeline between described reforming furnace and vapourizing furnace, described 4th pipeline is provided with the second diverting valve, and two outlets of described second diverting valve connect the outer tube of combustion chamber burner and the outer tube of return passage nozzle respectively; The 5th pipeline is provided with between the return passage nozzle of described calcining furnace and vapourizing furnace.
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| CN201410110834.8A CN103937552B (en) | 2014-03-24 | 2014-03-24 | A kind of three-section type entrained flow bed coal hydrogenation gasification stove and combined operation system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104388124B (en) * | 2014-11-05 | 2017-02-15 | 新奥科技发展有限公司 | Entrained flow bed gasifier |
| CN105482852B (en) * | 2015-11-20 | 2018-03-30 | 新奥科技发展有限公司 | A kind of gasification furnace and coal hydrogenation gasification method |
| CN108192667B (en) * | 2017-12-29 | 2020-04-10 | 扬州大学 | Biomass gasification furnace and gasification operation method thereof |
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