CN104611063A - Entrained-bed gasifier - Google Patents
Entrained-bed gasifier Download PDFInfo
- Publication number
- CN104611063A CN104611063A CN201510004604.8A CN201510004604A CN104611063A CN 104611063 A CN104611063 A CN 104611063A CN 201510004604 A CN201510004604 A CN 201510004604A CN 104611063 A CN104611063 A CN 104611063A
- Authority
- CN
- China
- Prior art keywords
- inner core
- vapourizing furnace
- urceolus
- reaction inner
- nozzle
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
Abstract
The invention discloses an entrained-bed gasifier, relates to the technical field of gasifiers, and solves the problems that the hydrogen consumption is relatively high and the carbon converting efficiency is relatively low in coal hydrogenation gasification process because during gasification reaction of the existing entrained-bed gasifier, combustion of a part of hydrogen is required for preheating, and semicoke is not effectively utilized. The entrained-bed gasifier provided by the invention comprises a gasifier outer barrel, wherein a reaction inner barrel is fixed in an upper area inside the gasifier outer barrel; a solid material nozzle is formed in the top end of the gasifier outer barrel; the solid material nozzle is formed by facing a top inlet of the reaction inner barrel; a baffle is arranged below a bottom outlet of the reaction inner barrel; a feed gas nozzle is formed in the side wall of the gasifier outer barrel; the feed gas nozzle is formed in the upper side of the baffle; a gasifying agent inlet is formed in the bottom end of the gasifier outer barrel. The entrained-bed gasifier is mainly applied to hydrogenation gasification reaction of coal.
Description
Technical field
The present invention relates to vapourizing furnace technical field, particularly relate to a kind of airflow bed gasification furnace.
Background technology
The gasification reaction of coal hydrogenation is a thermochemical process, and using fine coal (fine coal that general diameter is less than 75 μm) as raw material, using hydrogen as vaporized chemical, under high-temperature and high-pressure conditions, reaction generates raw gas and tar light oil.Wherein, raw gas can obtain methane-rich gas after the operations such as separation.
At present, fine coal hydrogasification technique mainly adopts airflow bed gasification furnace.In prior art, airflow bed gasification furnace is usually provided with coal nozzle at the top of vapourizing furnace and hydrogen nozzle, bottom are provided with raw gas outlet and semicoke outlet; Wherein, hydrogen nozzle exterior is connected with hydrogen process furnace usually, a large amount of cold hydrogen and a small amount of oxygen is passed in hydrogen process furnace, a small amount of oxygen and hydrogen partial burn and make remaining hydrogen temperature increase, promote the hydrogen after temperature in gasifying furnace nozzle again partial combustion make to enter the temperature that the hydrogen reacted with coal dust in vapourizing furnace reaches needs.Particularly, after fine coal and hydrogen carry out gasification reaction in the vapourizing furnace of high temperature, high pressure, generate raw gas, a small amount of tar light oil and a large amount of semicoke (coal of non-complete reaction); Wherein, product semicoke is usually direct discharges from semicoke outlet.
Above-mentioned vapourizing furnace is in coal hydrogenation gasification process, utilize hydrogen portion to burn and carry out the hydrogen that preheating can waste a large amount of preciousness, and mainly comprise carbon in semicoke, can to react generation hydrogen with water vapour or oxygen, and release a large amount of heat, in prior art, semicoke is usually direct discharges from semicoke outlet, therefore the hydrogen source in the carbon source in semicoke, semicoke reaction product and thermal source are not effectively utilized, thus cause that the hydrogen gas consumption in coal hydrogenation gasification technique is comparatively large, carbon conversion efficiency is lower.
Summary of the invention
The invention provides a kind of airflow bed gasification furnace, solve when utilizing airflow bed gasification furnace of the prior art to carry out gasification reaction, combustion parts hydrogen is needed to carry out preheating, and semicoke is not utilized effectively, thus cause the problem that in coal hydrogenation gasification technique, hydrogen gas consumption is comparatively large, carbon conversion efficiency is lower.
For achieving the above object, the present invention adopts following technical scheme:
A kind of airflow bed gasification furnace, comprise vapourizing furnace urceolus, the upper area in described vapourizing furnace urceolus is fixed with reaction inner core, and described vapourizing furnace urceolus top is provided with solid materials nozzle, and described solid materials nozzle is arranged towards the top inlet of described reaction inner core; Baffle plate is provided with below the bottom end outlet of described reaction inner core; Described vapourizing furnace outer tube side wall is provided with unstripped gas nozzle, and described unstripped gas nozzle is positioned on the upside of described baffle plate; Described vapourizing furnace urceolus bottom is provided with gasification agent inlet.
Wherein, described baffle plate is the circular arcuation baffle plate raised up.
Particularly, the peripheral diameter of described circular arcuation baffle plate is the 6/5-3/2 of described reaction inner core barrel dliameter; Spacing between the top of described circular arcuation baffle plate and the bottom of described reaction inner core is the 4/5-6/5 of described reaction inner core barrel dliameter.
During practical application, described solid materials nozzle at least comprises the central nozzle that a central position being positioned at described vapourizing furnace urceolus is arranged vertically downward.
Wherein, described solid materials nozzle also comprises at least 2 peripheral injector nozzles, and described peripheral injector nozzles is that circumferential uniform pitch is arranged around described central nozzle; The incident direction of described peripheral injector nozzles and the angle of described central nozzle incident direction are 30-45 degree.
Particularly, described unstripped gas nozzle at least comprises two; Described unstripped gas nozzle is evenly distributed on the sidewall of described vapourizing furnace urceolus.
Further, described unstripped gas nozzle is concordant with the bottom end outlet of described reaction inner core.
Preferably, the incident direction of described unstripped gas nozzle is for tilting upward, and the angle of described incident direction and horizontal plane is 30-60 degree.
During practical application, described vapourizing furnace urceolus inner side-wall is fixed with gas distribution grid; Described gas distribution grid is positioned at the bottom section of described vapourizing furnace urceolus.
Wherein, described reaction inner core barrel dliameter is the 2/3-2/5 of described vapourizing furnace urceolus barrel dliameter; Described reaction inner core tube length is the 3/8-5/8 of described vapourizing furnace urceolus tube length; Gap between the top of described reaction inner core and the top of described vapourizing furnace urceolus is less than the barrel dliameter of described reaction inner core.
Particularly, the sidewall of described vapourizing furnace urceolus is also provided with product gas outlet; Described product gas outlet is positioned at the upper area of described vapourizing furnace urceolus, and the top inlet region of corresponding described reaction inner core is arranged.
Further, the sidewall of described vapourizing furnace urceolus is also provided with slag-drip opening; Described slag-drip opening is positioned at the lower region of described vapourizing furnace urceolus, and the underside area of corresponding described baffle plate is arranged.
Preferably, described slag-drip opening comprises two; Two described slag-drip openings are tilted to down and are symmetrical arranged, and are 30-60 degree with the angle of described vapourizing furnace outer tube side wall.
In airflow bed gasification furnace provided by the invention, be described for the hydrogasification of coal reaction, fine coal can enter reaction inner core from solid materials nozzle, hydrogen can enter the annular space between vapourizing furnace urceolus and reaction inner core from unstripped gas nozzle, and move upward from reaction inner core top inlet enter reaction inner core react with fine coal generation coal hydrogenation gasification, generate rich hydrogen raw gas (H2 content is more, CH4 content is less) and semicoke.Wherein, rich hydrogen raw gas from the bottom end outlet of reaction inner core out time run into baffle plate, just baffling phenomenon occurs, namely circulation moves upward; Semicoke is then under the centrifugation and the action of gravity of self of gas, drop the lower region of vapourizing furnace urceolus from the surrounding of baffle plate, with the oxygen entered from gasification agent inlet or water vapour again generating gasification react, produce raw gas, raw gas moves upward to meet with rich hydrogen raw gas (containing part high-temperature hydrogen in raw gas), move upward along the annular space between reaction inner core and vapourizing furnace urceolus together, and after mixing with the fresh cold hydrogen that unstripped gas nozzle sprays into, enter in reaction inner core and continue to react with fine coal generation coal hydrogenation gasification; Wherein, the circulation of rich hydrogen raw gas effectively can realize the preheating of cold hydrogen, also can increase the residence time of hydrogen in vapourizing furnace, improves the utilising efficiency of hydrogen; The high temperature rough gas that char Gasification produces contains a certain amount of hydrogen, can the cold hydrogen of preheating, also can provide hydrogen source for fine coal hydrogasification reaction.Analyze known thus, in airflow bed gasification furnace provided by the invention, be provided with reaction inner core, baffle plate, gasification agent inlet, and the lower end area of vapourizing furnace urceolus can carry out the gasification reaction of semicoke, semicoke is fully effectively used, namely generate the preheating of high temperature rough gas for coal hydrogenation gasification hydrogen in reaction, avoid burning hydrogen of the prior art and carry out preheating; The gasification reaction of coal hydrogenation can be carried out in reaction inner core, therefore airflow bed gasification furnace provided by the invention is internal recycle two-part structure, the hydrogasification of fine coal, the regasifying of semicoke can be realized in a reaction unit, and the circulation of the preheating of hydrogen and Fu Qing raw gas, thus reduce the consumption of hydrogen, and improve carbon conversion efficiency, and then entirety improves the efficiency of coal hydrogenation gasification technique.
Accompanying drawing explanation
The structural representation of a kind of coal hydrogenation gasification stove that Fig. 1 provides for the embodiment of the present invention;
The structural representation of the another kind of coal hydrogenation gasification stove that Fig. 2 provides for the embodiment of the present invention.
In figure, 1-vapourizing furnace urceolus; 2-reacts inner core; 3-solid materials nozzle; 31-central nozzle; 32-peripheral injector nozzles; 4-(circular arcuation) baffle plate; 5-unstripped gas nozzle; 6-gasification agent inlet; 7-gas distribution grid; 8-product gas outlet; 9-slag-drip opening; The lower region of A-vapourizing furnace urceolus; The working cycle of the rich hydrogen raw gas of a-; The working cycle of b-raw gas.
Embodiment
Below in conjunction with accompanying drawing, a kind of coal hydrogenation gasification stove that the embodiment of the present invention provides is described in detail.
The embodiment of the present invention provides a kind of airflow bed gasification furnace, as shown in Figure 1, comprise vapourizing furnace urceolus 1, the upper area in vapourizing furnace urceolus 1 is fixed with reaction inner core 2, vapourizing furnace urceolus 1 top is provided with solid materials nozzle 3, and the top inlet of solid materials nozzle 3 orientating reaction inner core 2 is arranged; Baffle plate 4 is provided with below the bottom end outlet of reaction inner core 2; Vapourizing furnace urceolus 2 sidewall is provided with unstripped gas nozzle 5, and unstripped gas nozzle 5 is positioned on the upside of baffle plate 4; Vapourizing furnace urceolus 2 bottom is provided with gasification agent inlet 6.
In the airflow bed gasification furnace that the embodiment of the present invention provides, be described for the hydrogasification of coal reaction, fine coal can enter reaction inner core from solid materials nozzle, hydrogen can enter the annular space between vapourizing furnace urceolus and reaction inner core from unstripped gas nozzle, and move upward from reaction inner core top inlet enter reaction inner core react with fine coal generation coal hydrogenation gasification, generate rich hydrogen raw gas (H2 content is more, CH4 content is less) and semicoke.Wherein, rich hydrogen raw gas from the bottom end outlet of reaction inner core out time run into baffle plate, just baffling phenomenon occurs, namely circulation moves upward; Semicoke is then under the centrifugation and the action of gravity of self of gas, drop the lower region of vapourizing furnace urceolus from the surrounding of baffle plate, with the oxygen entered from gasification agent inlet or water vapour again generating gasification react, produce raw gas, raw gas moves upward to meet with rich hydrogen raw gas (containing part high-temperature hydrogen in raw gas), move upward along the annular space between reaction inner core and vapourizing furnace urceolus together, and after mixing with the fresh cold hydrogen that unstripped gas nozzle sprays into, enter in reaction inner core and continue to react with fine coal generation coal hydrogenation gasification; Wherein, the circulation of rich hydrogen raw gas effectively can realize the preheating of cold hydrogen, also can increase the residence time of hydrogen in vapourizing furnace, improves the utilising efficiency of hydrogen; The high temperature rough gas that char Gasification produces contains a certain amount of hydrogen, can the cold hydrogen of preheating, also can provide hydrogen source for fine coal hydrogasification reaction.Analyze known thus, in the airflow bed gasification furnace that the embodiment of the present invention provides, be provided with reaction inner core, baffle plate, gasification agent inlet, and the lower end area of vapourizing furnace urceolus can carry out the gasification reaction of semicoke, semicoke is fully effectively used, namely generate the preheating of high temperature rough gas for coal hydrogenation gasification hydrogen in reaction, avoid burning hydrogen of the prior art and carry out preheating; The gasification reaction of coal hydrogenation can be carried out in reaction inner core, therefore the airflow bed gasification furnace that the embodiment of the present invention provides is internal recycle two-part structure, the hydrogasification of fine coal, the regasifying of semicoke can be realized in a reaction unit, and the circulation of the preheating of hydrogen and Fu Qing raw gas, thus reduce the consumption of hydrogen, and improve carbon conversion efficiency, and then entirety improves the efficiency of coal hydrogenation gasification technique.
It should be added that, the temperature of the raw gas that char Gasification produces is about 1000 DEG C, and raw gas carries out circulation time can provide enough thermals source for the hydrogasification of coal herein; Wherein, the hydrogen partial contained in raw gas, can provide enough hydrogen sources for the hydrogasification of coal.Particularly, the raw gas that the rich hydrogen raw gas that coal hydrogenation gasification produces, char Gasification produce and the mixed gas temperature of fresh cold hydrogen that unstripped gas nozzle sprays into remain on 800-900 DEG C, meet the temperature requirement of coal hydrogenation gasification.
Coal hydrogenation gasification of the prior art, needs hydrogen partial burning to carry out preheating, to reach the temperature of reaction requirement usually.The airflow bed gasification furnace that the embodiment of the present invention provides, only need pass into hot hydrogen in the initial reaction moment, react to make itself and fine coal generating gasification, thus along with the carrying out reacted, the raw gas that rich hydrogen raw gas and char Gasification produce can provide certain thermal source and hydrogen source for coal hydrogenation gasification, namely realizes the circulation time of follow-up raw gas, the high-temperature hydrogen in raw gas is mixed with the follow-up cold hydrogen passed into, realize the efficient preheating of cold hydrogen, to reduce the demand of hot hydrogen gradually; Meanwhile, the airflow bed gasification furnace that the embodiment of the present invention provides, can increase the residence time of hydrogen in vapourizing furnace, thus effectively improve the utilising efficiency of hydrogen.
When actual production manufactures, baffle plate 4 can be straight plate structure, such as circular baffle plate or rectangle baffle plate, but in the airflow bed gasification furnace that the embodiment of the present invention provides, in order to improve the baffling effect of baffle plate 4 pairs of gases, as shown in Figure 1, baffle plate 4 can for the circular arcuation baffle plate 4 raised up, and namely the concrete structure of circular arcuation baffle plate 4 can be elliposoidal.Wherein, circular arcuation baffle plate 4 by between himself and reaction inner core 2, and/or can be arranged support (not shown) and is fixed installation between himself and vapourizing furnace urceolus 1; Particularly, support can be made up of multiple metal rod and/or metal tube, multiple metal rod and/or metal tube and circular arcuation baffle plate 4, reacts between inner core 2, vapourizing furnace urceolus 1, and the mode of welding can be adopted to be fixed.Certainly, this is not restricted for the concrete fixed form of baffle plate 4, and those skilled in the art can select other rational method.
Particularly, the peripheral maximum diameter of circular arcuation baffle plate 4 can be the 6/5-3/2 of reaction inner core 2 barrel dliameter, spacing between the top of circular arcuation baffle plate 4 and the bottom end outlet of reaction inner core 2 can for reacting the 4/5-6/5 of inner core 2 barrel dliameter, thus circular arcuation baffle plate 4 can ensure that rich hydrogen raw gas that hydrogasification produces is when running into baffle plate 4, good baffling phenomenon can be there is, and upwards cyclic motion, simultaneously, semicoke can under the centrifugation of gas and the action of gravity of self, successfully enter vapourizing furnace urceolus 1 lower region on the downside of it from the periphery of circular arcuation baffle plate 4.Wherein, spacing between the top of circular arcuation baffle plate 4 and the bottom end outlet of reaction inner core 2, can be preferably equal with the barrel dliameter of reaction inner core 2, thus the speed of circulation of gas can either be ensured, semicoke is avoided to pile up, too much gas can be avoided again to run downside into baffle plate 4, affect baffling effect.
It should be added that herein, the baffle plate 4 of reclinate arc-shaped structure in the airflow bed gasification furnace that the embodiment of the present invention provides, rich hydrogen raw gas generation baffling phenomenon out from reaction inner core 2 can not only be made, but also effectively can reduce rich hydrogen raw gas to the impact of baffle plate 4, thus prevent semicoke (particle) accumulation on baffle plate 4, affect the gasification reaction of follow-up semicoke.In addition, after the raw gas that semicoke regasifies generation runs into circular arcuation baffle plate 4, move upward along vapourizing furnace urceolus 1 and the annular space reacted between inner core 2 together with the rich hydrogen raw gas that can produce with coal hydrogenation gasification, the raw gas preventing semicoke from regasifying generation directly enters from the bottom of reaction inner core 2, contrary flow direction is produced, the proper flow of gas in impact reaction inner core 2 with the gas in reaction inner core 2.
Further, solid materials nozzle 3 can be one, and the central position being positioned at vapourizing furnace urceolus 1 is arranged vertically downward, thus ensures that all fine coal that solid materials nozzle 3 sprays can both enter in reaction inner core 2 and carry out gasification reaction.Wherein, in order to fine coal can be dispersed at the top inlet place of reaction inner core 2, as shown in Figure 1, solid materials nozzle 3 can comprise central nozzle 31 that a central position being positioned at vapourizing furnace urceolus 1 arranges vertically downward and the peripheral injector nozzles 32 that multiple (at least 2) are arranged in circumferential uniform pitch around central nozzle 31, particularly, the central position that central nozzle 31 can be positioned at vapourizing furnace urceolus 1 is arranged vertically downward, peripheral injector nozzles 32 symmetrical can be inclined at the periphery of central nozzle 31, and can be preferably 30-45 degree with the angle of central nozzle 31, thus can not only ensure that all fine coal that solid materials nozzle 3 sprays can both enter in reaction inner core 2, multiple different spray nozzles (31 can also be made, 32) there is collision mutually at the top inlet place of reaction inner core 2 in the fine coal sprayed into, and then play the effect of dispersed fine coal, it is enable fully to contact with hydrogen, as often as possible react.
Preferably, in order to make to be uniformly distributed in the annular space of hydrogen between reaction inner core 2 and vapourizing furnace urceolus 1, as shown in Figure 1, unstripped gas nozzle 5 can at least comprise two; Multiple above-mentioned raw materials gas jets 5 can be evenly distributed on the sidewall of vapourizing furnace urceolus 1, thus the hydrogen in above-mentioned annular space can be uniformly distributed, and then enter from all directions reaction inner core 2 at the top inlet place of reaction inner core 2, avoid hydrogen to concentrate to enter reaction inner core 2 from a direction, fully cannot contact with fine coal.Wherein, unstripped gas nozzle 5 can be concordant with the bottom end outlet of reaction inner core 2, namely unstripped gas nozzle 5 is highly consistent in the horizontal direction with the bottom end outlet place of reaction inner core 2, thus can contact with the hot gas in annular space in the very first time through the cold hydrogen that unstripped gas nozzle 5 sprays into, and flow through whole annular space from bottom to up and fully mix, to realize the at utmost preheating of cold hydrogen.Particularly, the incident direction of unstripped gas nozzle 5 can for tilting upward, namely unstripped gas nozzle 5 can for tilting upward injection, and this incident direction can be 30-60 degree with the angle of horizontal plane, namely the input angle that unstripped gas nozzle 5 sprays can be 30-60 degree, thus the hydrogen reducing to spray into is to the direct impact of reaction inner core 2 sidewall; Meanwhile, the loop direction of the raw gas of the incident direction of hydrogen and rich hydrogen raw gas and char Gasification is consistent, and then is conducive to the Rapid Circulation of gas.
During practical application, in order to the gas enabling gasification agent inlet 6 enter is uniformly distributed, as shown in Figure 2, vapourizing furnace urceolus 1 inner side-wall can be provided with gas distribution grid 7.Particularly, gas distribution grid 7 can be positioned at the bottom section of vapourizing furnace urceolus 1, and it is corresponding with gasification agent inlet 6, gas distribution grid 7 can be provided with multiple through hole (not shown) simultaneously, thus the water vapour entered through gasification agent inlet 6 and/or oxygen and/or air, can through the multiple through holes on gas distribution grid 7, even diffusion profile, at the lower region of vapourizing furnace urceolus 1, carries out gasification reaction fully with semicoke.
Preferably, in order to avoid the moieties in vapourizing furnace urceolus 1 lower region falls to expiring whole gas distribution grid 7, the through hole on gas distribution grid 7 is caused to block, affect the dispersion effect of vaporized chemical, as shown in Figure 2, gas distribution grid 7 can be downward-sloping conical hopper formula structure, thus drops on the material on gas distribution grid 7, landing to the central zone of gas distribution grid 7, can ensure that the through hole in other region still keeps unimpeded voluntarily.Because gasification agent inlet 6 can correspondingly with the central zone of gas distribution grid 7 vertically to be arranged, thus also can play through the vaporized chemical that gasification agent inlet 6 sprays into the effect dispelling gas distribution grid 7 central zone material.
Wherein, in order to ensure that fine coal can fully gasify in reaction inner core 2, as depicted in figs. 1 and 2, the barrel dliameter of reaction inner core 2 can be the 2/3-2/5 of the barrel dliameter of vapourizing furnace urceolus 1, the tube length of reaction inner core 2 can be the 3/8-5/8 of the tube length of vapourizing furnace urceolus 1, thus according to the bottle coal ratio in real reaction and coal input quantity, to meet the residence time of fine coal in reaction inner core 2 in 10-20 second, and then can be gasified fully.Gap between the top inlet of reaction inner core 2 and the top of vapourizing furnace urceolus 1 can be less than the barrel dliameter reacting inner core 2, and the fine coal sprayed into realize solid materials nozzle 3 can enter in reaction inner core 2 rapidly, reacts with hydrogen generating gasification; Meanwhile, the good circulation that will ensure to react gas in annular space between inner core 2 and vapourizing furnace urceolus 1 should be considered.Particularly, by the erecting frame (not shown) in the multiple vertical and level of top and the bottom welding of reaction inner core 2, thus well fixing reaction inner core 2 can be realized.Certainly, this is not restricted for the concrete fixed form of reaction inner core 2, and those skilled in the art can select other rational method.
During practical application, as shown in Figure 2, the sidewall of vapourizing furnace urceolus 1 is also provided with product gas outlet 8 and slag-drip opening 9.Wherein, product gas outlet 8 can be positioned at the upper area of vapourizing furnace urceolus 1, thus realizes the collection of raw gas; Slag-drip opening 9 can be positioned at the lower region of vapourizing furnace urceolus 1, thus realizes the collection of residue.
Particularly, as shown in Figure 2, product gas outlet 8 can align with the top inlet of reaction inner core 2 and arrange, and to make the raw gas of discharging from product gas outlet 8, obtains pure methane and pure cold hydrogen through dedusting after being separated; Wherein, pure cold hydrogen can also spray in coal hydrogenation gasification stove by unstripped gas nozzle 5 again, carries out gasification reaction with fine coal.In the airflow bed gasification furnace that the embodiment of the present invention provides, in order to the flowing preventing the flow effect of the raw gas of discharging from product gas outlet 8 from entering the gas reaction inner core 2 from annular space to coal hydrogenation gasification stove, be preferably the top inlet setting of product gas outlet 8 a little less than reaction inner core 2.During practical application, the underside area that slag-drip opening 9 can be positioned at baffle plate 4 is arranged, thus ensure semicoke regasify height, the i.e. reaction times of semicoke, make semicoke have enough residence time at the lower region of vapourizing furnace urceolus 1, usually should remain on 5-30 minute according to the reactivity of Coal rank semicoke and be advisable.
Preferably, in order to enable reacted residue discharge quickly and smoothly, as shown in Figure 2, slag-drip opening 9 can comprise two.Wherein, two slag-drip openings 9 can be tilted to down and be symmetrical arranged, and are 30-60 degree with the angle of vapourizing furnace urceolus 1 sidewall, thus ensure that the residue after char Gasification can be discharged smoothly.
Airflow bed gasification furnace of the prior art, usually (often react 1 kilogram of coal needs the hydrogen of burning about 0.5 cubic metre to carry out preheating to preheating reaction gas to utilize hydrogen portion to burn, this hydrogen partial does not participate in reaction, and just burning provides heat), cause hydrogen to waste; And the hydrogen in raw gas turns back to vapourizing furnace after being separated, calorific loss is comparatively serious; In reaction process, efficiency of carbon conversion is low, and generally about 45%, directly discharge after a large amount of semicokes of generation Quench bottom vapourizing furnace, the carbon residue in semicoke is not utilized effectively.But, the airflow bed gasification furnace that the embodiment of the present invention provides, achieve the hydrogasification of fine coal, the regasifying of semicoke, the efficient preheating of cold hydrogen and the circulation of Fu Qing raw gas, improve the efficiency of whole coal hydrogenation gasification technique, overall carbon conversions brings up to more than 90% simultaneously.Wherein, regasifying of semicoke not only makes semicoke obtain efficient conversion, and recycles fully, and provides hydrogen source and a large amount of thermals source for coal hydrogenation gasification reacts.
Particularly, as depicted in figs. 1 and 2, in the airflow bed gasification furnace that the embodiment of the present invention provides, the hydrogenation of fine coal is carried out in reaction inner core 2, and the working cycle of the rich hydrogen raw gas of generation is as shown in dotted arrow a; Regasifying of semicoke is carried out in the lower region of vapourizing furnace urceolus 1, region as shown in solid line arrow A, and the working cycle of the raw gas of generation is as shown in dotted arrow b.
The above; be only the specific embodiment of the present invention, but protection scope of the present invention is not limited thereto, is anyly familiar with those skilled in the art in the technical scope that the present invention discloses; change can be expected easily or replace, all should be encompassed within protection scope of the present invention.Therefore, protection scope of the present invention should described be as the criterion with the protection domain of claim.
Claims (13)
1. an airflow bed gasification furnace, it is characterized in that, comprise vapourizing furnace urceolus, the upper area in described vapourizing furnace urceolus is fixed with reaction inner core, described vapourizing furnace urceolus top is provided with solid materials nozzle, and described solid materials nozzle is arranged towards the top inlet of described reaction inner core;
Baffle plate is provided with below the bottom end outlet of described reaction inner core; Described vapourizing furnace outer tube side wall is provided with unstripped gas nozzle, and described unstripped gas nozzle is positioned on the upside of described baffle plate; Described vapourizing furnace urceolus bottom is provided with gasification agent inlet.
2. airflow bed gasification furnace according to claim 1, is characterized in that, described baffle plate is the circular arcuation baffle plate raised up.
3. airflow bed gasification furnace according to claim 2, is characterized in that, the peripheral diameter of described circular arcuation baffle plate is the 6/5-3/2 of described reaction inner core barrel dliameter; Spacing between the top of described circular arcuation baffle plate and the bottom of described reaction inner core is the 4/5-6/5 of described reaction inner core barrel dliameter.
4. airflow bed gasification furnace according to claim 1, is characterized in that, described solid materials nozzle at least comprises the central nozzle that a central position being positioned at described vapourizing furnace urceolus is arranged vertically downward.
5. airflow bed gasification furnace according to claim 4, is characterized in that, described solid materials nozzle also comprises at least 2 peripheral injector nozzles, and described peripheral injector nozzles is that circumferential uniform pitch is arranged around described central nozzle; The incident direction of described peripheral injector nozzles and the angle of described central nozzle incident direction are 30-45 degree.
6. airflow bed gasification furnace according to claim 1, is characterized in that, described unstripped gas nozzle at least comprises two; Described unstripped gas nozzle is evenly distributed on the sidewall of described vapourizing furnace urceolus.
7. airflow bed gasification furnace according to claim 6, is characterized in that, described unstripped gas nozzle is concordant with the bottom end outlet of described reaction inner core.
8. airflow bed gasification furnace according to claim 6, is characterized in that, the incident direction of described unstripped gas nozzle is for tilting upward, and the angle of described incident direction and horizontal plane is 30-60 degree.
9. airflow bed gasification furnace according to claim 1, is characterized in that, described vapourizing furnace urceolus inner side-wall is fixed with gas distribution grid; Described gas distribution grid is positioned at the bottom section of described vapourizing furnace urceolus.
10. airflow bed gasification furnace according to claim 1, is characterized in that, described reaction inner core barrel dliameter is the 2/3-2/5 of described vapourizing furnace urceolus barrel dliameter; Described reaction inner core tube length is the 3/8-5/8 of described vapourizing furnace urceolus tube length; Gap between the top of described reaction inner core and the top of described vapourizing furnace urceolus is less than the barrel dliameter of described reaction inner core.
11. airflow bed gasification furnaces according to claim 1, is characterized in that, the sidewall of described vapourizing furnace urceolus is also provided with product gas outlet; Described product gas outlet is positioned at the upper area of described vapourizing furnace urceolus, and the top inlet region of corresponding described reaction inner core is arranged.
12. airflow bed gasification furnaces according to claim 1, is characterized in that, the sidewall of described vapourizing furnace urceolus is also provided with slag-drip opening; Described slag-drip opening is positioned at the lower region of described vapourizing furnace urceolus, and the underside area of corresponding described baffle plate is arranged.
13. airflow bed gasification furnaces according to claim 12, is characterized in that, described slag-drip opening comprises two; Two described slag-drip openings are tilted to down and are symmetrical arranged, and are 30-60 degree with the angle of described vapourizing furnace outer tube side wall.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510004604.8A CN104611063B (en) | 2015-01-06 | 2015-01-06 | A kind of airflow bed gasification furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510004604.8A CN104611063B (en) | 2015-01-06 | 2015-01-06 | A kind of airflow bed gasification furnace |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104611063A true CN104611063A (en) | 2015-05-13 |
| CN104611063B CN104611063B (en) | 2017-04-05 |
Family
ID=53145717
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510004604.8A Active CN104611063B (en) | 2015-01-06 | 2015-01-06 | A kind of airflow bed gasification furnace |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104611063B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018152A (en) * | 2015-07-03 | 2015-11-04 | 新奥科技发展有限公司 | High-temperature semicoke cooling system and cooling method |
| CN107721112A (en) * | 2017-11-21 | 2018-02-23 | 湖北加德科技股份有限公司 | Municipal sludge desiccation pyrolytic gasification is controlled oneself CIU |
| CN107880942A (en) * | 2017-12-13 | 2018-04-06 | 新奥科技发展有限公司 | A kind of gasification furnace and gasification system |
| CN108753366A (en) * | 2018-06-04 | 2018-11-06 | 新奥科技发展有限公司 | A kind of airflow bed gasification furnace |
| CN109453824A (en) * | 2018-11-15 | 2019-03-12 | 新奥科技发展有限公司 | Catalyst carrying method and catalytic hydrogenation gasification process |
| CN110832057A (en) * | 2017-07-05 | 2020-02-21 | 新东工业株式会社 | Biomass gasification device |
| CN112461017A (en) * | 2020-11-13 | 2021-03-09 | 浙江启尔机电技术有限公司 | Thermal buffer tank, liquid supply device using the same and thermal buffer method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB944845A (en) * | 1959-07-07 | 1963-12-18 | Giovanni Hilgers | A method of gasifying liquid hydrocarbon fuels |
| CN101868520A (en) * | 2007-10-10 | 2010-10-20 | 鲁奇清洁煤炭技术有限公司 | Gas generator for gasifying solid granular fuels by applying pressure |
| CN102234546A (en) * | 2010-04-23 | 2011-11-09 | 武汉海德新能源投资有限公司 | Biomass gasifier |
| CN103031156A (en) * | 2012-12-13 | 2013-04-10 | 新奥科技发展有限公司 | Dry-process slag discharge device and method for entrained flow bed |
| CN203715582U (en) * | 2013-12-27 | 2014-07-16 | 新奥科技发展有限公司 | Multi-nozzle gasification furnace |
| CN203960148U (en) * | 2014-06-19 | 2014-11-26 | 新奥科技发展有限公司 | A kind of airflow bed gasification furnace |
-
2015
- 2015-01-06 CN CN201510004604.8A patent/CN104611063B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB944845A (en) * | 1959-07-07 | 1963-12-18 | Giovanni Hilgers | A method of gasifying liquid hydrocarbon fuels |
| CN101868520A (en) * | 2007-10-10 | 2010-10-20 | 鲁奇清洁煤炭技术有限公司 | Gas generator for gasifying solid granular fuels by applying pressure |
| CN102234546A (en) * | 2010-04-23 | 2011-11-09 | 武汉海德新能源投资有限公司 | Biomass gasifier |
| CN103031156A (en) * | 2012-12-13 | 2013-04-10 | 新奥科技发展有限公司 | Dry-process slag discharge device and method for entrained flow bed |
| CN203715582U (en) * | 2013-12-27 | 2014-07-16 | 新奥科技发展有限公司 | Multi-nozzle gasification furnace |
| CN203960148U (en) * | 2014-06-19 | 2014-11-26 | 新奥科技发展有限公司 | A kind of airflow bed gasification furnace |
Non-Patent Citations (1)
| Title |
|---|
| 李明等: "生物质两段式制氢反应炉原理及热态实验研究", 《太阳能学报》 * |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018152A (en) * | 2015-07-03 | 2015-11-04 | 新奥科技发展有限公司 | High-temperature semicoke cooling system and cooling method |
| CN105018152B (en) * | 2015-07-03 | 2017-08-25 | 新奥科技发展有限公司 | A kind of high-temperature semi-coke cooling system and cooling means |
| CN110832057A (en) * | 2017-07-05 | 2020-02-21 | 新东工业株式会社 | Biomass gasification device |
| CN110832057B (en) * | 2017-07-05 | 2021-09-03 | 新东工业株式会社 | Biomass gasification device |
| CN107721112A (en) * | 2017-11-21 | 2018-02-23 | 湖北加德科技股份有限公司 | Municipal sludge desiccation pyrolytic gasification is controlled oneself CIU |
| CN107880942A (en) * | 2017-12-13 | 2018-04-06 | 新奥科技发展有限公司 | A kind of gasification furnace and gasification system |
| CN108753366A (en) * | 2018-06-04 | 2018-11-06 | 新奥科技发展有限公司 | A kind of airflow bed gasification furnace |
| CN108753366B (en) * | 2018-06-04 | 2019-11-26 | 新奥科技发展有限公司 | A kind of airflow bed gasification furnace |
| CN109453824A (en) * | 2018-11-15 | 2019-03-12 | 新奥科技发展有限公司 | Catalyst carrying method and catalytic hydrogenation gasification process |
| CN109453824B (en) * | 2018-11-15 | 2021-09-10 | 新奥科技发展有限公司 | Catalyst loading method and catalytic hydro-gasification method |
| CN112461017A (en) * | 2020-11-13 | 2021-03-09 | 浙江启尔机电技术有限公司 | Thermal buffer tank, liquid supply device using the same and thermal buffer method |
| CN112461017B (en) * | 2020-11-13 | 2022-08-30 | 浙江启尔机电技术有限公司 | Thermal buffer tank, liquid supply device using the same, and thermal buffer method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104611063B (en) | 2017-04-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104611063A (en) | Entrained-bed gasifier | |
| US9481839B2 (en) | Hot oxygen nozzle and uses thereof in gasifiers | |
| US6960234B2 (en) | Multi-faceted gasifier and related methods | |
| CN100366710C (en) | Multi-nozzle coal water mixture or fine coal gasifying furnace and its industrial application | |
| CN101392191B (en) | Two stage type dry coal powder entrained flow gasifier | |
| KR101633951B1 (en) | Process and apparatus for utilizing the enthalpy of a synthesis gas by means of additional and post-gassing of renewable fuels | |
| CN102134512B (en) | Staged powder spraying entrained bed gasification furnace and gasification method thereof | |
| CN101985568B (en) | Two-stage oxygen supply dry slag removal pressurized gas flow bed gasification furnace | |
| CN101285006B (en) | Gasification process of water/gas mixed partial-chilled dry powder fuel and device | |
| CN102492478A (en) | Novel two-stage multi-nozzle pressurized gasifier and its gasification method | |
| KR101371291B1 (en) | Non-slagging and partial-slagging gasifier | |
| CN103555370A (en) | Method for gasifying carbonaceous organic materials and gasification furnace | |
| CN101845326B (en) | Spiral-flow melting pond gasifier | |
| CN201046953Y (en) | Circulating fluidized bed gas generating furnace | |
| KR101096632B1 (en) | Top feeding dual swirling gasifier | |
| CN104593083A (en) | Novel biomass step-by-step gasification method and device | |
| CN105154140A (en) | Multi-stage entrained-flow coal gasification method and equipment capable of realizing coupling high temperature shift | |
| CN105482852B (en) | A kind of gasification furnace and coal hydrogenation gasification method | |
| CN102492477B (en) | Hierarchical oxygen supply and controllable flame coal water slurry entrained bed combined nozzle | |
| CN109054901A (en) | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device | |
| CN102517088A (en) | Novel gasification furnace of pressurized aerated bed | |
| CN204417437U (en) | A kind of novel biomass substep gasification installation | |
| CN102433162B (en) | Entrained-flow bed gasifier with staged oxygen feeding and gasification method thereof | |
| CN203923116U (en) | A kind of down-draft type gasifying furnace with tar degradation function | |
| CN203960148U (en) | A kind of airflow bed gasification furnace |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |