CN103937552A - Three-section entrained flow bed hydrogenation vaporizing furnace and combined operation system - Google Patents
Three-section entrained flow bed hydrogenation vaporizing furnace and combined operation system Download PDFInfo
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- CN103937552A CN103937552A CN201410110834.8A CN201410110834A CN103937552A CN 103937552 A CN103937552 A CN 103937552A CN 201410110834 A CN201410110834 A CN 201410110834A CN 103937552 A CN103937552 A CN 103937552A
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- return passage
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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 discloses a three-section entrained flow bed hydrogenation vaporizing furnace. The furnace comprises a furnace body which is in a cylindrical shape in general; the furnace body comprises a combustion chamber, a reflux chamber, and an upper vaporizing chamber; the upper opening of the combustion chamber is connected to the lower opening of the reflux chamber through a reducing throat part; the upper opening of the reflux chamber is connected to the lower opening of the upper vaporizing chamber through a reducing throat part; a combustion chamber nozzle is tangentially arranged on the lower part of the side wall of the combustion chamber; a reflux chamber nozzle is arranged on the middle of the lower part of the internal side wall of the reflux chamber; a reflux plate in a cone shape is arranged above the reflux chamber nozzle; the reflux plate is arranged on the central axis of the reflux chamber, and a gap exists between the reflux plate and the side wall of the reflux chamber. The reflux plate can prevent the coal particles from entering the reflux area immediately so as to prolong the residence time of the coal particles, thus the conversion rate of coal gasification is improved, and the whole coal gasification efficiency is improved.
Description
Technical field
The present invention relates to a kind of coal gasifier.More specifically, relate to a kind of three-section type entrained flow bed coal hydrogenation gasification burner.
Background technology
Energy dilemma and environmental pollution have become the dual-pressure that hinders social development.Solve this two problems, can carry out respectively from immediate development and two angles of Long-and Medium-term Development.On the one hand, adapt to China and even world's Long-and Medium-term Development, should greatly develop new cleaning fuel, 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, the difficult one-tenth of novel energy leading role in the short period of time, short-term (or transitional period) planning of therefore still needing on the basis of long-term planning.The features such 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 gases, and 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 can only be supported decades.Therefore can predict, the status of coal in world energy sources is unshakable, and in the near future can ever more important.Coal had once been played the part of main energy resource supply role in mankind's process of industrialization, since entering for 20th century, along with oil, natural gas source are exploited in a large number 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 is still the main body energy in China and even the world, according to predicting the outcome of the Eergy Office of State Council etc. 2007, to the year two thousand thirty fossil oil will account for 81% of Chinese primary energy source consumption, wherein coal accounts for 52.9%; To 71.5% of will the account for Chinese primary energy source consumption of 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 be paid attention to the saving of fossil energy and use and rationally utilize.Thereby 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 that numerous Filter Tuber For Clean Coals utilize technology, and existing more than 200 years so far historical.The common recognition that the coal-based energy of development based on gasification and chemical system have become energy field scientific and technological circle and business circles, is also becoming efficient in world wide, clean, hot spot technology and the important development direction of development and utilization coal economically.The technical process of gasification has a lot, and the calorific value classification by producing coal gas, can be divided into coal gasification method: 1) produce caloric power of gas lower than the low calorific value coal gas method of 8347kJ/m3; 2) produce caloric power of gas in the middle calorific value of gas method of 16747-33494kJ/m3; 3) produce caloric power of gas higher than the high combustion value coal gas method of 33494kJ/m3.By heat-supplying mode, can be divided into: 1) autothermal evaporating method, in the engineering that gasifies, there is no extraneous heat supply, the required heat of gasification is provided by the heat producing that gasifies; 2) indirect heating evaporating method, gasification reaction this as thermo-negative reaction, thereby need the input of external heat; 3) steam gasification of coal and the hydrogasification method that combines, this method is that heat that coal hydrogenation gasification is produced is for providing coal steam gasification required heat; 4) thermal barrier heat supply, in an independent reactor, carries out heat supply with coal or coke and air combustion heat hot carrier, and thermal barrier can be solid, liquid fused salt or slag.By vaporized chemical classification, can be divided into: 1) air-steam gasification method, using air and steam as vaporized chemical, air is by coal partial oxidation and produce heat, and steam further carries out gasification reaction with the product of partial oxidation; 2) oxygen-steam gasification method, usings industrial oxygen and water vapour as vaporized chemical, and principle and air-steam gasification method are similar; 3) hydrogen evaporating method, the gas of usining H2 or being rich in H2, as vaporized chemical, can generate the coal gas that is rich in CH4.By solid-fuelled kinestate classification, can be divided into: 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, two sections of stoves of the type of furnace, water-gas generators, two sections of stoves of water-gas type etc. occur.
In numerous Coal Gasification Technology, coal hydrogenation gasification technology is subject to the extensive concern of Chinese scholars because of tool lot of advantages.For example, coal hydrogenation gasification is thermopositive reaction, thereby does not need the heat release of burning of extra oxygen; The direct product of coal hydrogenation gasification is CH4, thereby does not need extra CH4 to generate stove; The thermo-efficiency of coal hydrogenation gasification is very high, approaches 80%; Coal hydrogenation gasification reaction does not need catalyzer.In addition the fuel source such as IGCC and coal-based near zero release power generation system (ZEC) of coal hydrogenation gasification or multiple clean coal power generation system.
There is following problem in vapourizing furnace of the prior art, the gas that gasification produces can rise in vapourizing furnace, but during the raw inequality of the upwelling movable property of the gas in vapourizing furnace, carbon in coal (coal tar) flows out from vapourizing furnace before generating gasification reaction fully sometimes, and reactivity (carbon in coal is to the transformation efficiency of gas reforming) is reduced.Therefore, need to provide a kind of coal that can make in compact reaction vessel, to react fully, have 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, thereby 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 three-section type entrained flow bed coal hydrogenation gasification stove, comprises combustion chamber, return passage and upper vaporizer, and the end opening of the suitable for reading and return passage of described combustion chamber is fixedly connected with, and is undergauge shape and is connected between the end opening of the suitable for reading and upper vaporizer of described return passage; On described return passage sidewall, centering is provided with return passage nozzle, and the top of described return passage nozzle is provided with one and is down funnelform back flow plate; The rounded structure of cross section 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 there is gap between the plate body of back flow plate and the inner side-wall of return passage.Described back flow plate can make the air-flow rising upwards flow downwards and from the gap location between back flow plate and the inner side-wall of return passage, thereby form and reflux in return passage, extend the residence time raising transformation efficiency of pulverized coal particle in return passage, the formation commutating zone, position that is undergauge shape between the end opening of the suitable for reading and upper vaporizer of described return passage, described commutating zone can make to be positioned at outside pulverized coal particle near the return passage vaporizer centre that makes progress and flow, pulverized coal particle is uniformly distributed in upper vaporizer, thereby has improved the transformation efficiency of coal dust.
Preferably, described return passage nozzle is bilayer structure, and it comprises for spraying into the outer tube of hydrogen and arrange within the outer tube for spray into the inner tube of carbonic acid gas and coal dust in return passage in return passage.
Preferably, in the inner side-wall same level of described combustion chamber, along even circumferential, be arranged at intervals with combustion chamber burner, so that top from described combustion chamber is observed described in centered by axis and the central axis by described combustion chamber of each combustion chamber burner and the diameter imaginary circle less than the internal diameter of combustion chamber around the tangent mode of same direction, configure described combustion chamber burner.
Preferably, described combustion chamber burner is bilayer structure, and it comprises for spraying into the outer tube of hydrogen and arrange within the outer tube for spray into the inner tube of oxygen in combustion chamber in combustion chamber.
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 that comprises 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; The CaO being provided with between described reforming furnace and calcining furnace for calcining furnace is produced is transported to the second pipeline and the CaCO for reforming furnace is produced in reforming furnace
3be transported to the 3rd pipeline in calcining furnace; Between described reforming furnace and vapourizing furnace, be provided with the 4th pipeline, described the 4th pipeline is provided with the second diverting valve, and two outlets of described the second diverting valve connect respectively the outer tube of combustion chamber burner and the outer tube of return passage nozzle; Between the return passage nozzle of described calcining furnace and vapourizing furnace, be provided with the 5th pipeline.
Beneficial effect of the present invention is as follows:
Back flow plate can produce and reflux 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 to offset the centrifugal force that eddy flow produces, pulverized coal particle mobile from back flow plate lateral is assembled towards vaporizer center, thereby made the distribution of pulverized coal particle in vaporizer be tending towards even.Thereby, adopt this three-section type entrained flow bed hydrogasification stove can further improve the transformation efficiency of coke, 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 below, should not limit the scope of the invention with this.
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, between the end opening of the suitable for reading and return passage of combustion chamber 10, being undergauge shape is connected, the end opening suitable for reading and upper vaporizer 30 of return passage 20 is undergauge shape and is connected, the formation recirculating zone, undergauge suitable for reading place 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 rounded structure of cross section 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, between back flow plate 23 and the inner side-wall of return passage 20, has gap.In the inner side-wall same level of combustion chamber 10, along even circumferential, be arranged at intervals with combustion chamber burner 11, centered by the axis of each combustion chamber burner 11 and central axis by combustion chamber 10 and the diameter imaginary circle less than the internal diameter of combustion chamber 10 around the tangent mode of same direction, combustion chamber burner 11 is set.Combustion chamber burner 11 and return passage nozzle 22 are bilayer structure, and combustion chamber burner 11 centers spray into oxygen, and skin sprays into hydrogen.Return passage nozzle 22 centers spray into carbonic acid gas and coal dust, and skin sprays into hydrogen.
In vapourizing furnace, vapor pressure is chosen as 7MPa, and oxygen and hydrogen quality ratio are 1.5, with higher inlet velocity (15m/s), from combustion chamber burner 11, sprays into and burns, and produces high-temperature gas mixture agent (hydrogen and the water vapour) eddy flow of 1600 ℃ of left and right.Remaining hydrogen quality and always enter coal mass ratio and be set as 0.3 after burning.Air input can suitably be adjusted by coal input quantity in vapourizing furnace, and for example setting coal input quantity is 5kg/s left and right, to guarantee that gas velocity can make to form in vapourizing furnace air flow bed.High-temperature gas mixture agent in combustion chamber 10 enters in return passage 20 after aditus laryngis, in return passage 20, mix with the coal dust spraying into from return passage nozzle 22 and remaining hydrogen and a small amount of carbonic acid gas, 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 power of the dragging effect spiral of swirling eddy and because being subject to centrifugal action, have the trend of outside motion.Under the drive of return passage 20 bottom upstreams and under the restriction of back flow plate 23, the pulverized coal particle spraying 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 meeting then move downward after moving upward to certain distance; due to centrifugal action; the particle falling can back flow plate 23 bottom outside be subject to fair speed air-flow drive and from spiral outside back flow plate, last under the effect of commutating zone 21 again upwards vaporizer 30 centers assemble, to offset the effect of centrifugal force.The synthetic gas that vapourizing furnace produces and flying dust and the not coke granule of complete reaction are overflowed from furnace roof.
As shown in Figure 4, a kind of combined operation system that uses above-mentioned vapourizing furnace, comprises vapourizing furnace 1, reforming furnace 200 and calcining furnace 300, is provided with the first pipeline 100, the first pipelines 100 and is provided with the first diverting valve 101 between the outlet of described vapourizing furnace 1 and reforming furnace 200; The CaO being provided with between described reforming furnace 200 and calcining furnace 300 for calcining furnace 300 is produced is transported to the second pipeline 400 and the CaCO for reforming furnace 200 is produced in reforming furnace 200
3be transported to the 3rd pipeline 500 in calcining furnace 300; Between described reforming furnace 200 and vapourizing furnace 1, be provided with the 4th pipeline 600, described the 4th pipeline 600 is provided with the second diverting valve 601, and two outlets of described the second diverting valve 601 connect respectively the outer tube of combustion chamber burner and the outer tube of return passage nozzle; Between described calcining furnace 300 and the return passage nozzle 22 of vapourizing furnace 1, be provided with the 5th pipeline 700.
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 be used as industrial chemicals or fuel (for internal combustion turbine or fuel cell etc.) is used; The rich CH of another part
4synthetic gas enters reforming furnace 200, in reforming furnace 200, adds H
2o generates H
2and CO
2gas mixture, the CO that reforming furnace 200 produces
2the CaO trapping being transported by the second pipeline 400 by calcining furnace generates CaCO
3, the H that reforming furnace 200 produces
2by the 4th pipeline 600 and the second diverting valve 601, be transported to respectively the outer tube of combustion chamber burner and the outer tube of return passage nozzle.CaCO
3by the 3rd pipeline 500, enter in calcining furnace 300 and calcine and generate CaO and CO
2, the carbon of complete reaction not can be used as the part of heat energy of calcining furnace 300.The CaO circulation that calcining furnace 300 generates enters carries out CO in reforming furnace 200
2trapping, the CO that calcining furnace 300 produces
2by the 5th pipeline 700, from the inner tube of return passage nozzle, enter vapourizing furnace and H
2pulverized coal conveying together.This vapourizing furnace combined operation system can be realized 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 all embodiments exhaustive, every still row in protection scope of the present invention of apparent variation that technical scheme of the present invention extends out or change that belong to.
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 undergauge shape and is connected between the end opening of the suitable for reading and upper vaporizer of described return passage; On described return passage sidewall, centering is provided with return passage nozzle, and the top of described return passage nozzle is provided with one and is down funnelform back flow plate; The rounded structure of cross section 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 there is gap between the plate body of back flow plate and the inner side-wall of return passage.
2. vapourizing furnace according to claim 1, is characterized in that: described return passage nozzle is sleeve structure; It comprises for spraying into the outer tube of hydrogen and arrange within the outer tube for spray into the inner tube of carbonic acid gas and coal dust in return passage in return passage.
3. vapourizing furnace according to claim 1, it is characterized in that: in the sidewall same level of described combustion chamber, along even circumferential, be arranged at intervals with combustion chamber burner, the imaginary circle that one diameter is less than combustion chamber internal diameter is set centered by the central axis of described combustion chamber, and 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 for spraying into the outer tube of hydrogen and arrange within the outer tube for spray into the inner tube of oxygen in combustion chamber in combustion chamber.
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
°, back flow plate is 1/3 of return passage height together with the total height of supporting leg, 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. a combined operation system that comprises vapourizing furnace as described in claim 1～7, it is characterized in that: this system comprises vapourizing furnace, reforming furnace and calcining furnace, between the outlet of described vapourizing furnace and reforming furnace, be provided with the first pipeline, this first pipeline is provided with the first diverting valve;
The CaO being provided with between described reforming furnace and calcining furnace for calcining furnace is produced is transported to the second pipeline and the CaCO for reforming furnace is produced in reforming furnace
3be transported to the 3rd pipeline in calcining furnace;
Between described reforming furnace and vapourizing furnace, be also provided with the 4th pipeline, described the 4th pipeline is provided with the second diverting valve, and two outlets of described the second diverting valve connect respectively the outer tube of combustion chamber burner and the outer tube of return passage nozzle; Between the return passage nozzle of described calcining furnace and vapourizing furnace, be provided with the 5th pipeline.
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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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|---|---|---|---|
| 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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| CN103937552A true CN103937552A (en) | 2014-07-23 |
| CN103937552B CN103937552B (en) | 2015-11-18 |
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Cited By (3)
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| CN104388124A (en) * | 2014-11-05 | 2015-03-04 | 新奥科技发展有限公司 | Entrained flow bed gasifier |
| CN105482852A (en) * | 2015-11-20 | 2016-04-13 | 新奥科技发展有限公司 | Gasification furnace and hydrogasification method for coal |
| CN108192667A (en) * | 2017-12-29 | 2018-06-22 | 扬州大学 | A kind of biomass gasifying furnace and its gasification operation method |
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| CN108192667A (en) * | 2017-12-29 | 2018-06-22 | 扬州大学 | A kind of biomass gasifying furnace and its gasification operation 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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| Publication number | Publication date |
|---|---|
| CN103937552B (en) | 2015-11-18 |
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