CN101982528B - Gasification device for classified gasification of moving bed, method for gasifying coal and applications thereof - Google Patents
Gasification device for classified gasification of moving bed, method for gasifying coal and applications thereof Download PDFInfo
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- CN101982528B CN101982528B CN 201010557366 CN201010557366A CN101982528B CN 101982528 B CN101982528 B CN 101982528B CN 201010557366 CN201010557366 CN 201010557366 CN 201010557366 A CN201010557366 A CN 201010557366A CN 101982528 B CN101982528 B CN 101982528B
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Abstract
The invention provides a gasification device for the classified gasification of a moving bed, and a method for classified gasifying of coal and applications thereof. The device comprises a compression shell, a coal filling hopper, a coal distributor, a stirrer, axially symmetrical water clamping sleeves, a slag chilling chamber, a circulatory chilled water inlet, a circulatory chilled water outlet, and a slag seal hopper, wherein, the top and the bottom of the compression shell are respectively provided with a first opening and a second opening, the upper lateral side of the compression shellis provided with a first coal gas outlet, and the same horizontal level at lower part of the compression shell is evenly provided with at least two gasification agent nozzles; the coal filling hopperis arranged on the first opening at the top of the compression shell; the coal distributor is arranged at the upper part in the compression shell; an axially symmetrical water clamping sleeve is arranged in the inner side below the first coal gas outlet of the compression shell, and the inner part of the axially symmetrical water clamping sleeve forms a gasification chamber; the slag chilling chamber is arranged below the second opening at the bottom of the compression shell; and the slag seal hopper is arranged below the slag chilling chamber. The invention is characterized in that at least two fine coal and gasification agent burners are evenly arranged at the lower part of the compression shell of the gasification device and the same horizontal level of the at least two gasification agent nozzles in a staggering manner.
Description
Technical field
The present invention relates in general to the gasification field that a kind of carbon raw material is produced coal gas, in particular to a kind of moving-bed gasification device of classification gasification, coal grading gasification process and uses thereof.
Background technology
Gasification of coal is the crucial leading technology that the coal clean and effective transforms, and is developed rapidly along with the construction of coal system oil Coal Chemical Industry project.Moving-bed in the gasification technology, fluidized-bed and entrained flow gasification respectively have relative merits, all obtain in various degree industrial application in China.
The normal pressure moving-bed gasification has obtained being extensive use of in China because of technology maturation, simple to operate.Wherein producer gas is low because of effective constituent, calorific value is low mainly as industrial fuel gas.Water-gas generators then is mainly used in small and medium chemical fertilizer, adopt periodical operation to produce water-gas or semi-water gas, this gasification technology be owing to must use anthracite block coal (or coke) to be raw material, not only the price height, and periodical operation causes gasification efficiency low, so the production cost height.For further improving gasification efficiency and reducing the pollution that blowing air is directly discharged generation, in recent years, some enterprises used the oxygen-rich gasification method of operate continuously to produce nitrogenous coal gas, but still had the dependence problem to anthracite block coal.
For improving vapourizing furnace throughput and improving caloric power of gas, enlarge the use range of coal simultaneously, external strange (Lurgi) pressurized-gasification furnace in Shandong of dry method ash discharge and two kinds of moving-bed gasification technologies of BGL pressurized-gasification furnace of slag tap successively developed.
Lurgi (Shandong is strange) pressurized-gasification furnace technology is ripe, and by the exploitation of German LURGI, its working pressure 2.0～4.0MPa, product coal gas be through recovery of heat and oil removing, contains have an appointment 8%～12% methane and unsaturated hydrocarbons, and is suitable as town gas or carry out Poly-generation.Raw gas can be used as synthetic gas after hydro carbons separation and steam reforming, but relative long flow path, it is bigger to produce a large amount of phenolic wastewater and intractability, has influenced the economic target of this gasification technology to a certain extent.
Fixed bed slag tap gasification (BGL stove) technology is s-generation static bed coal gasification technology, by the BGC of company of Centrica and the cooperative development of Lurgi company, called after BGL, working pressure is 2.5～3.0MPa, gasification temperature is at 1400～1600 ℃, cancelled travelling grate, lime-ash is discharged with liquid form.Because high-temperature operation, steam consumption significantly reduces, and steam decomposition rate is higher.The gasification intensity of BGL vapourizing furnace improves 3 to 4 times than Lurgi stove.Because steam consumption significantly reduces CO in the raw gas
2Content is down to 3%～5% by 30%, and the calorific value of coal gas improves about 1/4th.
At present these two kinds of gasification technologies all are being applied in big moulded coal system oil Coal Chemical Industry project, uses except in by force other coal the caking coal be gasified raw material.But mainly use lump coal to be raw material at present, as brown coal, long-flame coal, meager lean coal.And along with a large amount of uses of mechanical coal mining technology, the lump coal productive rate is descended, so the feed coal source is limited, price is higher than fine coal.In addition, preferably adopt forming technique to make moulded coal earlier to the bad coal of thermostability, add vapourizing furnace again, this will increase raw materials cost undoubtedly.Therefore, in the face of the predicament of raw material, be necessary to develop a kind of novel gasification installation that is fit to lump coal and coal gasification simultaneously.
Summary of the invention
The objective of the invention is on the basis of existing technology, a kind of gasification installation that can use lump coal and fine coal or coal slurry simultaneously is provided, can only be the shortcoming of gasified raw material with lump coal or lump coke to overcome present fixed-bed gasification furnace, reduces production costs simultaneously.In addition, use CO
2During pulverized coal conveying, can reduce oxygen depletion to a certain extent.To solve the present existing technical problem of fixed bed gasification furnace system.
One aspect of the present invention provides a kind of classification gasification moving-bed gasification device, comprising:
Pressure shell, has first opening at the top of pressure shell, has second opening in the bottom of pressure shell, upper side at pressure shell arranges first gas exit, and the same horizontal plane in the pressure shell bottom of classification gasification moving-bed gasification device evenly arranges at least two vaporized chemical nozzles;
Add coal bunker, be arranged on first opening at pressure shell top;
The coal sparger is arranged at the top of pressure shell inside, and the coal sparger comprises agitator;
Axial symmetrical water jacket is arranged on the inboard of first gas exit below of pressure shell, and the inside of axial symmetrical water jacket constitutes vaporizer;
The slag shock chamber is arranged under second opening of pressure shell bottom, and the slag shock chamber comprises circulation chilled water entrance and the outlet of circulation chilled water; And
Seal slag bucket, be arranged on the below of slag shock chamber;
It is characterized in that, pressure shell bottom at classification gasification moving-bed gasification device also alternately evenly arranges at least two duffs and vaporized chemical burner with at least two residing same horizontal planes of vaporized chemical nozzle, wherein at least two vaporized chemical nozzles are evenly arranged in the vapourizing furnace bottom along the vapourizing furnace shell in same horizontal plane, and at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner symmetric arrangement in same horizontal plane.
Preferably, the circulation chilled water entrance of slag shock chamber is in and is lower than circulation chilled water exit.
Preferably, the circulation chilled water entrance of slag shock chamber is in a side of slag shock chamber, and the outlet of circulation chilled water is in the opposite side away from the slag shock chamber of circulation chilled water entrance.
Preferably, at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner are selected from two vaporized chemical nozzles and two duffs and vaporized chemical burner, three vaporized chemical nozzles and three duffs and vaporized chemical burner, four vaporized chemical nozzles and four duffs and vaporized chemical burner, five vaporized chemical nozzles and five duffs and vaporized chemical burner or six vaporized chemical nozzles and six duffs and vaporized chemical burner respectively.
Preferably, four vaporized chemical nozzles and two duffs and vaporized chemical burner are set, the adjacent setting of vaporized chemical nozzle in twos, one of a side arranges two duffs and vaporized chemical burner between the vaporized chemical nozzle of two groups of adjacent settings in twos, namely with the formal ring of vaporized chemical nozzle vaporized chemical nozzle duff and vaporized chemical burner vaporized chemical nozzle vaporized chemical nozzle duff and the vaporized chemical burner pressure shell around vapourizing furnace.
Preferably, duff and vaporized chemical burner are to be made of two-layer at least circulating line, and wherein duff and vaporized chemical are by the pipe-line transportation of the different layers of duff and vaporized chemical burner.
Preferably, add the coal bunker upper end and be provided with the feed coal import, the lower end that adds coal bunker links to each other with first opening at pressure shell top by flange.
Preferably, first gas exit is connected with volume tank.
Volume tank further comprises:
Second gas entry is arranged on the middle part sidewall of volume tank and a little less than first gas exit, and be connected with second gas line and extend into volume tank near the place, bottom,
Second gas exit is arranged on the upper portion side wall or top of volume tank, and is higher than second gas entry,
The ash water outlet is arranged on the bottom of volume tank,
At least one deck gas net that looses is arranged on the below of volume tank, and is installed on the inwall of volume tank and around second gas line, and
At least one deck foam-breaking strip is arranged on the top of gas net of loosing, and is installed on the inwall of volume tank and is positioned at second gas line top that second gas entry connects.
Be loaded with the buck of gas washing at volume tank.Buck can be by being arranged on the grey water outlet discharging of volume tank bottom.At least one deck gas net that looses, be arranged on and be used for the below of buck of gas washing in the volume tank, to be conducive to synthetic gas in the dispersion that is used in the buck of gas washing, and one deck foam-breaking strip at least, be positioned at the top of the buck of gas washing, be used for puncturing the bubble in the synthetic gas of gas washing, to be conducive to remove steam and the solid matter of sweeping along in the bubble.
More preferably, second gas line near bottom place that extends into volume tank further comprises gas distributor, the dispersion of the synthetic gas that is beneficial to generate and washing.
More preferably, evenly be provided with metal prong on each root foam-breaking strip of one deck foam-breaking strip at least.
Preferably, at least two vaporized chemical nozzles removably evenly are crisscross arranged on pressure shell with at least two duffs and vaporized chemical burner.
Preferably, each of at least two duffs and vaporized chemical burner is provided with swirler at the spout place.
Preferably, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-45 °, preferred 0-30 °, more preferably 0-20 °.
Particularly, duff and vaporized chemical burner can be to be constituted or be made of shellring shape pipeline by two-layer circulating line.
For example, duff and vaporized chemical burner are made of two-layer circulating line, then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by outer field circulating line, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct, and vice versa.
If duff and vaporized chemical burner are made of shellring shape pipeline then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by the internal layer circulating line around central duct, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct and outermost circulating line, and vice versa.
Wherein first vaporized chemical is selected from oxygen and water vapour or oxygen and CO
2Second vaporized chemical is selected from one or more the mixture in oxygen, air, oxygen-rich air, carbonic acid gas or the water vapour, second gasified raw material is selected from fine particles containing carbon, contains carbon pastes or carbon containing inflammable gas, fine particles containing carbon is selected from one or more the mixture in coal dust, coal liquefaction residue powder, biomass powder and the organic powder of carbon containing, contains one or more the mixture in coal liquefaction residue, liquefied residue slip, coal oil mixture, methyl alcohol coal slurry, biomass slip, light oil and the heavy oil that carbon pastes is selected from coal water slurry, fusion.
First vaporized chemical can be oxygen or oxygen-rich air etc., and second vaporized chemical also can be oxygen or oxygen-rich air etc.
Second gasified raw material can be dry coal powder, coal water slurry or coal oil mixture.
Second gasified raw material is coal water slurry or coal oil mixture, is then directly carried by pump.
Second gasified raw material is the dry coal powder, then uses nitrogen or carbonic acid gas as the delivery medium of dry coal powder.
Another aspect of the present invention, a kind of coal grading gasification process is provided, comprise: by the coal bunker that adds that is positioned at top of gasification furnace lump coal or type coal gasification raw material are added stove, simultaneously with first vaporized chemical by sending into vapourizing furnace inside at least two vaporized chemical nozzles, second gasified raw material and second vaporized chemical of the setting of vapourizing furnace bottom sides by at least two duffs that constituted by two-layer at least circulating line and vaporized chemical burner in the setting of vapourizing furnace bottom sides
Wherein first vaporized chemical is selected from oxygen and water vapour or oxygen and CO
2Second vaporized chemical is selected from oxygen, air, oxygen-rich air, the mixture of one or more in carbonic acid gas or the water vapour, second gasified raw material is selected from fine particles containing carbon, contain carbon pastes or carbon containing inflammable gas, fine particles containing carbon is selected from coal dust, the coal liquefaction residue powder, the mixture of one or more in the organic powder of biomass powder and carbon containing, contain carbon pastes and be selected from coal water slurry, the coal liquefaction residue of fusion, the liquefied residue slip, coal oil mixture, the methyl alcohol coal slurry, the biomass slip, the mixture of one or more in light oil and the heavy oil
Second gasified raw material and second vaporized chemical be the pipe-line transportation of the different layers by duff and vaporized chemical burner respectively, second gasified raw material that is sprayed into vapourizing furnace by duff and vaporized chemical burner accounts for total furnace coal weight, namely (lump coal+second gasified raw material) amount 10%-50%, the working pressure scope of vapourizing furnace is 0.1-10MPa, base burning district temperature is 1300-1600 ℃, and temperature out is 400-600 ℃.
Preferably, second gasified raw material is selected from dry coal powder, coal water slurry or coal oil mixture, and second gasified raw material that is sprayed into vapourizing furnace by duff and vaporized chemical burner accounts for total furnace coal weight, i.e. the 10%-50% of the amount of (lump coal+duff).
Preferably, second gasified raw material is the dry coal powder, and every cubic metre of conveying solid substance amount is greater than 400kg.
Preferably, second gasified raw material is coal water slurry or coal oil mixture, and the concentration of coal water slurry or coal oil mixture is greater than 60wt%.
Preferably, use nitrogen or carbonic acid gas as the delivery medium of dry coal powder.
Particularly, duff and vaporized chemical burner 7 can be to be constituted or be made of shellring shape pipeline by two-layer circulating line.
For example, duff and vaporized chemical burner 7 are made of two-layer circulating line, then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by outer field circulating line, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct, and vice versa.
If duff and vaporized chemical burner 7 are made of shellring shape pipeline then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by the internal layer circulating line around central duct, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct and outermost circulating line, and vice versa.
Wherein first vaporized chemical can be oxygen or oxygen-rich air etc., and second vaporized chemical also can be oxygen or oxygen-rich air etc.
Second gasified raw material can be dry coal powder, coal water slurry or coal oil mixture.
Second gasified raw material is coal water slurry or coal oil mixture, is then directly carried by pump.
Second gasified raw material is the dry coal powder, then uses nitrogen or carbonic acid gas as the delivery medium of dry coal powder.
Another aspect of the present invention provides the application aspect preparation water-gas, semi-water gas, nitrogenous coal gas, synthetic gas, reducing gas or fuel gas of a kind of classification gasification moving-bed gasification device and coal grading gasification process.
Classification gasification moving-bed gasification device of the present invention has increased fine breeze and vaporized chemical burner, and coal grading gasification process of the present invention has increased the supply of fine breeze and vaporized chemical, thereby has realized the gasification simultaneously in same vapourizing furnace of lump coal and fine coal.In addition because the specific surface area of fine breeze is greater than the specific surface area of lump coal, so the reaction times of fine breeze less than the reaction times of lump coal, under identical vapourizing furnace and gasification pressure condition, gas deliverability that can corresponding raising vapourizing furnace.And the coal gas that fine breeze reaction back generates can continue to participate in reaction in up process, has increased the growing amount of methane to a certain extent.
Description of drawings
Fig. 1 is the classification gasification moving-bed gasification schematic representation of apparatus of a kind of embodiment of the present invention;
Fig. 2 is the synoptic diagram that is provided with the volume tank of loose gas net and foam-breaking strip of the present invention;
Fig. 3 is the structure diagram of the diffusing gas net in the volume tank of Fig. 2 according to the present invention;
Fig. 4 is the structure diagram of the foam-breaking strip in the volume tank of Fig. 2 according to the present invention; And
Fig. 5 a is the vertical view of the swirler that arranges on the duff of Fig. 1 vapourizing furnace according to the present invention and the vaporized chemical burner, and Fig. 5 b is the front view of swirler section;
Fig. 6 is the classification gasification moving-bed gasification schematic representation of apparatus that has Fig. 2 volume tank of another kind of embodiment of the present invention.
Embodiment
The specific embodiment of the present invention below is provided.Those skilled in the art should understand that wherein embodiment only is for illustrative purposes, should not be regarded as limiting by any way the scope of the invention defined by the claims.
An embodiment of the invention provide a kind of classification gasification moving-bed gasification device, comprising: a kind of classification gasification moving-bed gasification device 100 comprises:
Add coal bunker 1, be arranged on first opening 31 at pressure shell top;
Axial symmetrical water jacket 5 is arranged on the inboard of first gas exit, 4 belows of pressure shell 3, and the inside of axial symmetrical water jacket 5 constitutes vaporizer 6;
It is characterized in that, pressure shell 3 bottoms at classification gasification moving-bed gasification device 100 also alternately evenly arrange at least two duffs and vaporized chemical burner 7 with at least two vaporized chemical nozzle 10 residing same horizontal planes, wherein at least two vaporized chemical nozzles are evenly arranged in the vapourizing furnace bottom along vapourizing furnace shell 3 in same horizontal plane, and at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner symmetric arrangement in same horizontal plane.
In a preferred embodiment, the circulation chilled water entrance 81 of slag shock chamber 8 is in and is lower than the circulation chilled water and exports 83 places.
In a preferred embodiment, the circulation chilled water entrance 81 of slag shock chamber 8 is in a side of slag shock chamber 8, circulation chilled water outlet 83 opposite sides that are in away from the slag shock chamber 8 of circulation chilled water entrance 81.
In a preferred embodiment, at least two vaporized chemical nozzles 10 and at least two duffs and vaporized chemical burner 7 are selected from two vaporized chemical nozzles 10 and two duffs and vaporized chemical burner 7, three vaporized chemical nozzles 10 and three duffs and vaporized chemical burner 7, four vaporized chemical nozzles 10 and four duffs and vaporized chemical burner 7, five vaporized chemical nozzles 10 and five duffs and vaporized chemical burner 7 or six vaporized chemical nozzles 10 and six duffs and vaporized chemical burner 7 respectively.
In a preferred embodiment, duff and vaporized chemical burner 7 are to be made of two-layer at least circulating line, and wherein duff and vaporized chemical are by the pipe-line transportation of the different layers of duff and vaporized chemical burner 7.
In a preferred embodiment, add coal bunker 1 upper end and be provided with feed coal import 15, the lower end that adds coal bunker 1 links to each other with first opening 31 at pressure shell top by flange.
In a preferred embodiment, first gas exit 4 is connected with volume tank 45, and volume tank 45 further comprises:
At least one deck gas net 453 that looses is arranged on the below of volume tank 45, and is installed on the inwall of volume tank 45 and around second gas line 459, and
At least one deck foam-breaking strip 456, are arranged on the top of the gas net 453 that looses, and be installed on the inwall of volume tank 45 and be positioned at that second gas entry 452 connects around second gas line, 459 tops.
Be loaded with the buck of gas washing at volume tank.Buck can be by grey water outlet 457 dischargings that are arranged on volume tank 45 bottoms.Wherein one deck gas net 453 that looses is arranged in the buck of gas washing at least, evenly distributes in the buck of gas washing being used for to be conducive to synthetic gas, is beneficial to flush away solid entrainment wherein, as the coal dust of trace etc.And one deck foam-breaking strip 456 is positioned at above the buck of gas washing at least, so that the air pocket of the synthetic gas through washing is smashed, to be conducive to remove the buck of sweeping along in the synthetic gas bubble, further purifies synthetic gas.
One more preferably in the embodiment, second gas line 459 near the place, bottom that extends into volume tank 45 further comprises gas distributor, the dispersion of the synthetic gas that is beneficial to generate and washing.
One more preferably in the embodiment, evenly be provided with metal prong 458 on each root foam-breaking strip of one deck foam-breaking strip 456 at least.
Wherein evenly be provided with metal prong 458 on each root foam-breaking strip of one deck foam-breaking strip 456 at least, be conducive to the small bubbles of the synthetic gas through washing are smashed, to be conducive to remove the buck of sweeping along in the synthetic gas small bubbles, further purify synthetic gas again.In a preferred embodiment, at least two vaporized chemical nozzles 10 removably evenly are crisscross arranged on pressure shell 3 with at least two duffs and vaporized chemical burner 7.
In a preferred embodiment, each of at least two duffs and vaporized chemical burner 7 is provided with swirler 75 at the spout place.
In a preferred embodiment, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-45 °.
In a preferred embodiment, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-30 °.
In another preferred embodiment, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-20 °.
In an embodiment, duff and vaporized chemical burner 7 are made of two-layer circulating line.
In another embodiment, duff and vaporized chemical burner 7 are made of shellring shape pipeline.
For example, duff and vaporized chemical burner 7 are made of two-layer circulating line, then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by outer field circulating line, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct, and vice versa.
If duff and vaporized chemical burner 7 are made of shellring shape pipeline then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by the internal layer circulating line around central duct, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct and outermost circulating line, and vice versa.
Wherein first vaporized chemical is selected from oxygen and water vapour or oxygen and CO
2Second vaporized chemical is selected from one or more the mixture in oxygen, air, oxygen-rich air, carbonic acid gas or the water vapour, second gasified raw material is selected from fine particles containing carbon, contains carbon pastes or carbon containing inflammable gas, fine particles containing carbon is selected from one or more the mixture in coal dust, coal liquefaction residue powder, biomass powder and the organic powder of carbon containing, contains one or more the mixture in coal liquefaction residue, liquefied residue slip, coal oil mixture, methyl alcohol coal slurry, biomass slip, light oil and the heavy oil that carbon pastes is selected from coal water slurry, fusion.
First vaporized chemical can be oxygen or oxygen-rich air etc., and second vaporized chemical also can be oxygen or oxygen-rich air etc.
Second gasified raw material can be dry coal powder, coal water slurry or coal oil mixture.
Second gasified raw material is coal water slurry or coal oil mixture, is then directly carried by pump.
Second gasified raw material is the dry coal powder, uses nitrogen or carbonic acid gas as the delivery medium of dry coal powder.
Another embodiment of the invention, the coal grading gasification process is provided, comprise: by the coal bunker 1 that adds that is positioned at top of gasification furnace lump coal or type coal gasification raw material are added stove, simultaneously with first vaporized chemical by sending into vapourizing furnace inside at least two vaporized chemical nozzles 10, second gasified raw material and second vaporized chemical of the setting of vapourizing furnace bottom sides by at least two duffs that constituted by two-layer at least circulating line and vaporized chemical burner 7 in the setting of vapourizing furnace bottom sides
Wherein first vaporized chemical is selected from oxygen and water vapour or oxygen and CO
2Second vaporized chemical is selected from oxygen, air, oxygen-rich air, the mixture of one or more in carbonic acid gas or the water vapour, second gasified raw material is selected from fine particles containing carbon, contain carbon pastes or carbon containing inflammable gas, fine particles containing carbon is selected from coal dust, the coal liquefaction residue powder, the mixture of one or more in the organic powder of biomass powder and carbon containing, contain carbon pastes and be selected from coal water slurry, the coal liquefaction residue of fusion, the liquefied residue slip, coal oil mixture, the methyl alcohol coal slurry, the biomass slip, the mixture of one or more in light oil and the heavy oil
Second gasified raw material and second vaporized chemical be the pipe-line transportation of the different layers by duff and vaporized chemical burner 7 respectively, second gasified raw material that is sprayed into vapourizing furnace by duff and vaporized chemical burner 7 accounts for total furnace coal weight, namely (lump coal+second gasified raw material) amount 10%-50%, the working pressure scope of vapourizing furnace is 0.1-10MPa, base burning district temperature is 1300-1600 ℃, and temperature out is 400-600 ℃.
In a preferred embodiment, second gasified raw material is selected from dry coal powder, coal water slurry or coal oil mixture, and second gasified raw material that is sprayed into vapourizing furnace by duff and vaporized chemical burner 7 accounts for total furnace coal weight, i.e. the 10%-50% of the amount of (lump coal+duff).
In a preferred embodiment, second gasified raw material is the dry coal powder, and every cubic metre of conveying solid substance amount is greater than 400kg.
In a preferred embodiment, second gasified raw material is coal water slurry or coal oil mixture, and the concentration of coal water slurry or coal oil mixture is greater than 60wt%.
In a preferred embodiment, use nitrogen or carbonic acid gas as the delivery medium of dry coal powder.
In an embodiment, duff and vaporized chemical burner 7 are made of two-layer circulating line.
In another embodiment, duff and vaporized chemical burner 7 are made of shellring shape pipeline.
For example, duff and vaporized chemical burner 7 are made of two-layer circulating line, then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by outer field circulating line, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct, and vice versa.
If duff and vaporized chemical burner 7 are made of shellring shape pipeline then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by the internal layer circulating line around central duct, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct and outermost circulating line, and vice versa.
Wherein first vaporized chemical can be oxygen or oxygen-rich air etc., and second vaporized chemical also can be oxygen or oxygen-rich air etc.
Second gasified raw material can be dry coal powder, coal water slurry or coal oil mixture.
Second gasified raw material is coal water slurry or coal oil mixture, is then directly carried by pump.
Second gasified raw material is the dry coal powder, then uses nitrogen or carbonic acid gas as the delivery medium of dry coal powder.
Another aspect of the present invention provides the application aspect preparation water-gas, semi-water gas, nitrogenous coal gas, synthetic gas, reducing gas or fuel gas of a kind of classification gasification moving-bed gasification device and coal grading gasification process.
Below in conjunction with the drawings and specific embodiments, novel classification gasification moving-bed gasification device provided by the invention is described in detail as follows, it only is for the present invention being given further instruction, should be appreciated that therefore it does not limit interest field of the present invention.
With reference to Fig. 1, a kind of classification gasification moving-bed gasification device 100 is provided, comprising: pressure shell 3, be provided with vertically and add coal bunker 1, coal sparger 2, vaporizer 6, slag shock chamber 8 and sealing slag bucket 9 from top to bottom.
Wherein, the inside of pressure shell 3 is provided with the water jacket 5 of axial symmetry, produces middle pressure steam in gasification.Add the top that coal bunker 1 is positioned at vapourizing furnace, in order to lump coal or type coal gasification raw material are added in the stove.First gas exit 4 is established in side on pressure shell 3 tops of vapourizing furnace, and the raw gas that will reaction generates is discharged vapourizing furnace.Adding the gasified raw material that coal bunker 1 adds from the top of classification gasification moving-bed gasification device is lump coal, moulded coal or the coke of 5-100mm.Preferably, adding the gasified raw material that coal bunker 1 adds from the top of classification gasification moving-bed gasification device can be lump coal, moulded coal or the coke of 20-100mm, the lump coal of 20-80mm, moulded coal or coke, the lump coal of 5-80mm, moulded coal or coke, the lump coal of 20-50mm, moulded coal or coke.
Classification gasification moving-bed gasification device 100 of the present invention is provided with at least two vaporized chemical nozzles 10 simultaneously in vapourizing furnace bottom sides (being the bottom sides of the pressure shell 3 of vapourizing furnace), at least two duffs and vaporized chemical burner 7, at least two vaporized chemical nozzles 10 wherein, at least two duffs and vaporized chemical burner 10 are arranged in the same horizontal plane of vapourizing furnace (being the pressure shell 3 of vapourizing furnace), the difference symmetric arrangement, i.e. at least two vaporized chemical nozzle symmetric arrangement, at least two duffs and vaporized chemical burner be symmetric arrangement also, and at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner are arranged at interval.The spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-45 °.
Preferably, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-30 °, more preferably, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-20 °.
In another preferred embodiment, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 10-20 °.
In another preferred implementation, the spout level of at least two vaporized chemical nozzles and at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-10 °.
According to the capacity difference of vapourizing furnace, the vaporized chemical nozzle number of setting is 2-6, and duff and vaporized chemical burner number are 2-4.Two vaporized chemical nozzles 10 and two duffs and vaporized chemical burner 7 can be set, three vaporized chemical nozzles 10 and three duffs and vaporized chemical burner 7, four vaporized chemical nozzles 10 and four duffs and vaporized chemical burner 7, five vaporized chemical nozzles 10 and five duffs and vaporized chemical burner 7, or six vaporized chemical nozzles 10 and six duffs and vaporized chemical burner 7.Four vaporized chemical nozzles 10 and two duffs and vaporized chemical burner 7 also can be set, vaporized chemical nozzle 10 adjacent settings in twos, one of a side arranges two duffs and vaporized chemical burner 7 between the vaporized chemical nozzle 10 of two groups of adjacent settings in twos, namely with the formal ring of vaporized chemical nozzle 10-vaporized chemical nozzle 10-duff and vaporized chemical burner 7-vaporized chemical nozzle 10-vaporized chemical nozzle 10-duff and vaporized chemical burner 7 pressure shell 3 around vapourizing furnace.
The gasified raw material that adds from the duff of vapourizing furnace bottom sides setting and vaporized chemical burner 7 can be for fine particles containing carbon, contain carbon pastes or carbon containing inflammable gas.Fine particles containing carbon can be any one or the two or more mixtures in coal dust, coal liquefaction residue powder, biomass powder and the organic powder of carbon containing; Contain carbon pastes and can be any one or the two or more mixtures in coal liquefaction residue, liquefied residue slip, coal oil mixture, methyl alcohol coal slurry, biomass slip, light oil and the heavy oil of coal water slurry, fusion; The carbon containing inflammable gas is that Sweet natural gas, coking dry gas, catalytic cracked dry gas, catalytic pyrolysis dry gas, flammable chemical industry discharge any one or the two or more mixtures in the gas.The vaporized chemical that adds from the vaporized chemical nozzle 10 of vapourizing furnace bottom sides setting or duff and vaporized chemical burner 7 is one or more mixture of oxygen, air or oxygen-rich air, carbonic acid gas or steam.
Classification gasification moving-bed gasification device 100 of the present invention, the purpose that vaporized chemical nozzle 10 is set are with a part of vaporized chemical such as oxygen and water vapour or oxygen and CO
2Add in the vapourizing furnace, in order to participate in burning and gasification reaction with coal or semicoke.It is dry coal powder or water (oil) coal slurry can be sprayed into the stove confidential reference items with vaporized chemical oxygen, carbonic acid gas or water vapour to add the gasification reaction with the purpose of vaporized chemical burner 7 that duff is set.So, then can reduce traditional moving-bed gasification technology to the dependence of lump coal with fine coal as the partial gasification raw material.Wherein vaporized chemical nozzle 10 is two and also is two with duff and vaporized chemical burner 7, alternately evenly distributes mutually.
Duff and vaporized chemical burner 7 as the charging of use dry coal powder, preferably use oxygen (or adding a small amount of water vapor) to be vaporized chemical, can select to use nitrogen or carbonic acid gas to make the delivery medium of dry coal powder according to the purposes of product gas, as the synthetic gas that will generate for the synthesis of ammonia, then can use nitrogen to carry the dry coal powder as delivery medium, otherwise generally use CO
2As delivery medium.If use coal water slurry or coal oil mixture as the partial gasification raw material, be vaporized chemical with oxygen preferably then, also can mix part of O
2, coal water slurry or coal oil mixture are then directly by being pumped in the system.
Main purpose of the present invention is by using a part of fine coal to be gasified raw material, thereby reduces traditional moving-bed gasification technology to the dependence of lump coal, and the fine coal price often is lower than the lump coal price, therefore also can reduce raw materials cost to a certain extent.Therefore consider the singularity of moving-bed gasification device, the duff amount that sprays into vapourizing furnace by duff and vaporized chemical burner 7 accounts for the 10%-50% of total furnace coal weight (lump coal+fine coal).The amount of burner vaporized chemical then determined according to duff amount and coal characteristic, but for reducing the medium amount of carrying, and need use for the dry coal powder and closely carry mutually, and every cubic metre of conveying solid substance amount of general requirement is greater than 400kg; For the coal water slurry charging, then require its concentration greater than 60wt%.
Compare with the strange gasification technology in existing Shandong, classification gasification moving-bed gasification device of the present invention has increased vaporized chemical and fine coal burner in the bottom of vapourizing furnace, and its steam oxygen ratio reduces greatly, can be down at present below 2 by the 5-8 of prior art, has reduced water vapour consumption and follow-up waste water output.Compare with the BGL gasification technology that the Shandong is strange, classification gasification moving-bed gasification device of the present invention has increased fine breeze and vaporized chemical, thereby has realized the gasification simultaneously in same vapourizing furnace of lump coal and fine coal.In addition because the specific surface area of fine breeze is greater than the specific surface area of lump coal, so the reaction times of fine breeze less than the reaction times of lump coal, under identical vapourizing furnace and gasification pressure condition, gas deliverability that can corresponding raising vapourizing furnace.And the coal gas that fine breeze reaction back generates can continue to participate in reaction in up process, has increased the growing amount of methane to a certain extent.
The working pressure scope of classification gasification moving-bed gasification device of the present invention is 0.1-10MPa, base burning district temperature is 1300-1600 ℃, the vapourizing furnace temperature out is 400-600 ℃, and the vapourizing furnace internal diameter can be 3-5m, and the ability of vapourizing furnace gasification of coal is 1000-3000t/d.
As traditional moving-bed gasification technology, the bed of material in the gasification hearth of classification gasification moving-bed gasification device of the present invention can be divided into drying layer, destructive distillation layer, methanation layer, first responding layer (reducing zone), second responding layer (oxidation gasification layer) and molten slag layer from top to bottom roughly, and layering may be so unobvious in actual procedure certainly.
As traditional moving-bed gasification technology, the reaction of coal gasification course can be divided into two types in the classification gasification moving-bed gasification device of the present invention: (1) heterogeneous gas-solid reaction, gas phase may be the vaporized chemical of initial charging, also may be the product in the gasification, solid phase refers to the carbon in the coal.Though coal has very complicated molecular structure, other elements such as hydrogen, oxygen in addition that are connected with carbon atom are because gasification reaction occurs in after the coal cracking, so only consider that the principal element carbon in the coal is rational.(2) gas-phase reaction of homogeneous phase, reactant may be the vaporized chemicals of initial charging, also may be the reaction product in the gasification.
The bed of material in the gasification hearth of classification gasification moving-bed gasification device of the present invention reaction conditions and/or the related reaction of each layer from top to bottom is as follows:
Drying layer: drying process also is the coal dehydration, after raw material lump coal adds vapourizing furnace from furnace roof, owing between the hot gas flow of coal and rising or the red-hot semicoke heat exchange takes place, makes moisture evaporation in the coal become water vapour and enters gas phase.Usually the thickness of drying layer is about 500-1000mm.
The destructive distillation layer: destructive distillation is the process that removes volatile matter, and along with coal moves down, the temperature of dry coal further improves, and this moment, volatile matter was overflowed from coal.Remove the pyrolysis that volatile matter generally is also referred to as coal, it is one of common primitive reaction of all gasifying process.The destructive distillation layer thickness is generally 500-600mm.
The methanation layer: the methanation layer is the principal reaction layer that generates methane in the gasification, also is the difference place of pressurized gasification and atmospheric gasification.The methane formation reaction that this layer carries out is the reaction between carbon and hydrogen, carbon monoxide and the hydrogen, speed of response will be slowly than the gasification reaction speed in first responding layer (reducing zone) and second responding layer (oxidation gasification layer) many, therefore, can fully carry out for making reaction, generate methane as much as possible, general requirement methane layer thickness is bigger, guarantees that raw material is at about 0.5-1h of the residence time of this layer.Because the heat that other reaction absorbs in methane formation reaction liberated heat and this layer is almost equal, therefore the temperature variation of this layer is less.The methanation layer thickness is generally 900-1200mm.The reaction that generates methane all is thermopositive reaction.
First responding layer: also claim reducing zone, the semicoke that after destructive distillation, obtains and the H in the air-flow
2O, CO
2, H
2Deng reaction, generate products such as inflammable gas, reducing zone thickness is about 400-600mm, and principal reaction comprises:
(1) reaction of carbon and water vapour
At a certain temperature, following inhomogeneous reaction takes place between carbon and the water vapour:
This is the principal reaction of making water-gas, is also referred to as the water vapour decomposition reaction sometimes, and last reaction formula is also referred to as water-gas reaction, and these two reactions all are thermo-negative reaction.
(2) reaction of carbon and carbonic acid gas
Second important inhomogeneous reaction of carrying out at gasifying stage is the producer gas reaction, i.e. the reaction of carbon and carbonic acid gas:
This is very strong thermo-negative reaction, must just can react under hot conditions.
(3) transformationreation
This reaction is called the carbon monodixe conversion reaction, or claims the water-gas balanced reaction.It is homogeneous reaction, by the CO of gasifying stage generation and the reaction between the water vapour.In order to produce H
2, need utilize this reaction.Because this reaction is easy to reach balance, under gasifier gas temperature out condition, reaction reaches balance substantially usually, thereby this reaction has determined the composition of outlet coal gas.
Second responding layer (oxidation gasification layer): this layer is different from traditional moving-bed slag tap layer, except combustion reactions, owing to spray into coal dust, quick destructive distillation also can take place, reach redox reaction, and this reaction layer thickness is about 300-500mm.Residual semicoke and the oxygen in the vaporized chemical burn after top gasification, for other reactions and coal drying provide heat:
Jiao ξ+O
2→ 2 (ξ-1) CO+ (2-ξ) CO
2+ ash
Wherein ξ is statistical constant, depends on CO and CO in the products of combustion
2Ratio, its scope is between 1～2.
In addition, new coal dust also can remove volatile matter and above-mentioned semicoke and water vapour, CO
2Reaction.And under the prerequisite that oxygen exists, also have gaseous fraction generation combustion reactions, as:
Molten slag layer: this layer is positioned under second responding layer, but the two boundary is not obvious.
Except above principal reaction, the reaction that also has heteroatomss such as S, N to take place in the time of gasification generates H
2S, COS, NH
3With HCN etc.
Very compare with the BGL gasification technology with existing Shandong, the present invention has increased the coal dust burner in the pressure shell bottom of classification gasification moving-bed gasification device, thereby realized the gasification simultaneously in same vapourizing furnace of lump coal and fine coal, reduce the strange and BGL gasification technology in existing Shandong to the dependence of lump coal, be conducive to the comprehensive utilization of coal.
In addition, the reaction times of fine breeze is less than the lump coal reaction times, gas deliverability that can corresponding raising vapourizing furnace.And the coal gas that fine breeze reaction back generates can continue to participate in reaction in up process, increases the growing amount of methane to a certain extent.And by regulating duff that bottom sides sprays into and the amount of vaporized chemical, also can adjust the ratio of lump coal and fine coal, thereby improve operating load and the turndown ratio of single stove, and can suitably regulate the composition of product gas according to the needs of back system.In addition, this gasification technology can use dry powder, coal water slurry or coal oil mixture charging, has enlarged the use range of coal to a certain extent.
The mode of operation of classification gasification moving-bed gasification device of the present invention is: with lump coal, moulded coal or the coke of 5-100mm by adding coal bunker 1 and coal sparger 2 joins in the vapourizing furnace, go into lump coal, moulded coal or the coke of stove at first by up heating gas heat drying, dried lump coal, moulded coal or coke enter the destructive distillation pull-up subsequently successively except volatile matter, at methanation layer generation methanation reaction, in reducing zone and water vapour or carbonic acid gas generation reduction reaction, enter the base burning district subsequently.In the bottom of vapourizing furnace, first vaporized chemical (being oxygen and the water vapour) participation that is sprayed into by vaporized chemical nozzle 10 and the reaction of coal dust or above-mentioned semicoke; And burning and gasification reaction can directly take place by duff (can be dry coal powder, coal water slurry or coal oil mixture) and second vaporized chemical (oxygen, carbonic acid gas or water) that duff and vaporized chemical burner 7 spray into, also can react with the vaporized chemical (as oxygen-rich air) of other types, last ash content forms slag and drains into slag shock chamber 8, slag shock chamber 8 comprises circulation chilled water entrance 81 and circulation chilled water outlet 83, and the slag after the Quench relies on gravity to enter the sealing slag bucket 9 that is arranged on 8 belows, slag shock chamber.And high-temperature gas had both reacted in uphill process, and also with heat transferred solid coal or semicoke, coal gas is discharged vapourizing furnace by the gas exit 4 of top of gasification furnace side at last.
In a preferred embodiment, the circulation chilled water entrance 81 of slag shock chamber 8 is in and is lower than the circulation chilled water and exports 83 places.
In another preferred embodiment, the circulation chilled water entrance 81 of slag shock chamber 8 is in a side of slag shock chamber 8, circulation chilled water outlet 83 opposite sides that are in away from the slag shock chamber 8 of circulation chilled water entrance 81.
Add coal bunker 1 upper end and be provided with feed coal import 15, the lower end that adds coal bunker 1 links to each other with first opening 31 at pressure shell top by flange.
With reference to Fig. 6 and Fig. 2, also be connected with volume tank 45 on the pipeline of first gas exit 4 of classification gasification moving-bed gasification device 100 of the present invention, this volume tank 45 further comprises:
At least one deck gas net 456 that looses is arranged on the below of volume tank 45, and is installed on the inwall of volume tank 45 and around second gas line 459, and
At least one deck foam-breaking strip 453, are arranged on the top of the gas net 456 that looses, and are installed on the inwall of volume tank 45 and are positioned at second gas line, 459 tops that second gas entry 452 connects.
Circulating condensing water is arranged in volume tank 45, be used for cooling off and the coal gas of discharging being washed.Splendid attire is used for grey water outlet 457 dischargings that the buck of gas washing can be by being arranged on volume tank 45 bottoms in volume tank.One more preferably in the embodiment, second gas line 459 near the place, bottom that extends into volume tank 45 further comprises the gas distributor (not shown), the dispersion of the synthetic gas that is beneficial to generate and washing.
On each root foam-breaking strip of each layer of two-layer foam-breaking strip 456, all evenly be provided with metal prong 458 (referring to Fig. 3).The structure of diffusing gas net 453 as shown in Figure 4.
Wherein one deck gas net 453 that looses is arranged in the buck of gas washing at least, evenly distributes in the buck of gas washing being used for to be conducive to synthetic gas, is beneficial to flush away solid entrainment wherein, as the coal dust of trace etc.And two-layer foam-breaking strip 456 is positioned at the buck top of gas washing, so that the air pocket of the synthetic gas through washing is smashed, to be conducive to remove the buck of sweeping along in the synthetic gas bubble, further purifies synthetic gas.Be conducive to the small bubbles of the synthetic gas through washing are smashed, to be conducive to remove the buck of sweeping along in the synthetic gas small bubbles, further purify synthetic gas again.
By the coal gas of volume tank 45 and since loose gas net 453 and foam-breaking strip 456 with and go up the metal prong 458 that arranges and reduced steam and a spot of ash content and the coal dust of carrying secretly in the coal gas, purified coal gas.
In a preferred embodiment, at least two vaporized chemical nozzles 10 of classification gasification moving-bed gasification device 100 of the present invention removably evenly are crisscross arranged on pressure shell 3 with at least two duffs and vaporized chemical burner 7.
With reference to Fig. 5 a and 5b, in order to improve the mixed aerosol effect of duff and vaporized chemical, classification gasification moving-bed gasification device 100 of the present invention, wherein each of duff and vaporized chemical burner 7 is provided with swirler 75 in spout.This swirler 75 can be axial screw slot type (referring to Fig. 5 a and 5b), also can be axial rotary vane type.Be arranged at the swirler 75 in duff and the vaporized chemical burner 7, have axial screw groove 752 on it, its external diameter equates with the internal diameter of duff and vaporized chemical burner 7, and cooperation is installed in duff and the vaporized chemical burner 7; The center of swirler is cylindrical cavity, and axle pivot internal diameter is 0.6-0.8 with the ratio of external diameter.Be arranged at the swirler 75 in duff and the vaporized chemical burner 7, has axial screw groove 752 on it, its thickness equates substantially with the diameter of the circular ring pipe of duff and vaporized chemical burner 7, be arranged at swirlers 75 in duff and the vaporized chemical burner 7 and further improved the mixed aerosol effect of duff and vaporized chemical burner 7 spout place oxygen, coal water slurry and/or carbonic acid gas, improve speed of response and gas producing efficiency.
Adopt classification gasification moving-bed gasification device 100 of the present invention to carry out gasification test, by the coal bunker 1 that adds that is positioned at top of gasification furnace lump coal or type coal gasification raw material are added stove, simultaneously with first vaporized chemical by sending into vapourizing furnace inside at two vaporized chemical nozzles 10, second gasified raw material and second vaporized chemical of the setting of vapourizing furnace bottom sides by two duffs that constituted by two-layer at least circulating line and vaporized chemical burner 7 in the setting of vapourizing furnace bottom sides.
Particularly, duff and vaporized chemical burner 7 can be to be constituted or be made of shellring shape pipeline by two-layer circulating line.
For example, duff and vaporized chemical burner 7 are made of two-layer circulating line, then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by outer field circulating line, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct, and vice versa.
If duff and vaporized chemical burner 7 are made of shellring shape pipeline then second gasified raw material such as fine breeze, coal water slurry or coal oil mixture can be sent into vapourizing furnace inside by the internal layer circulating line around central duct, second vaporized chemical such as oxygen or oxygen-rich air are then sent into vapourizing furnace inside by central duct and outermost circulating line, and vice versa.
Wherein first vaporized chemical can be oxygen, and second vaporized chemical also is oxygen.
Second gasified raw material is coal water slurry, is directly carried by pump.
Second gasified raw material and second vaporized chemical be the pipe-line transportation of the different layers by duff and vaporized chemical burner 7 respectively.The working pressure scope of vapourizing furnace is 0.1-10MPa, and base burning district temperature is 1300-1600 ℃, and temperature out is 400-600 ℃, and obtains following result.
The gasification furnace structure that adopts of test as shown in Figure 1, its processing power is 1000t/d.The gasified raw material that test is adopted is typical long-flame coal, its technical analysis and ultimate analysis such as following table:
In the last table, M
tBe full water-content, A
Ar, V
Ar, FC
ArBe respectively the content of as received basis ash content, as received basis volatile matter and as received basis fixed carbon, C
Ar, H
Ar, N
Ar, O
ArAnd S
Ar, tBe respectively as received basis carbon content, as received basis hydrogen richness, as received basis nitrogen content, as received basis oxygen level and as received basis total sulphur content.
Calculate through theory, under the condition of 80% lump coal and 20% fine coal charging, coal gas consists of:
H
2?24.10％，CO?57.78％，CH
4?8.34％，C
2H
6?0.52％，C
2H
4?0.21％，CO
2?4.83％，N
2?2.24％，H
2S0.12％，NH
3?0.02％。
The usage quantity of carbonic acid gas and coal water slurry is that the ratio of carbonic acid gas volumetric flow rate and coal water slurry flow changes between 1/200 to 10/50, and visual particular case is adjusted.
Ratio for the usage quantity of oxygen and carbonic acid gas does not have particular requirement, as long as control the ratio of carbonic acid gas volumetric flow rate and coal water slurry flow well, visual particular case is adjusted.
The pressure of carbonic acid gas pipeline changes between oxygen pipeline and coal water slurry line pressure, and the pressure of carbonic acid gas pipeline is good a little less than oxygen pipeline pressure, because the pressure rating difference of different vapourizing furnaces, the visual particular case of its pressure is adjusted.
Very compare with the BGL gasification technology with existing Shandong, classification gasification moving-bed gasification device of the present invention, increased the coal dust burner in the pressure shell bottom, thereby realized the gasification simultaneously in same vapourizing furnace of lump coal and fine coal, reduce the strange and BGL gasification technology in existing Shandong to the dependence of lump coal, be conducive to the comprehensive utilization of coal.
In addition, the reaction times of fine breeze is less than the lump coal reaction times, gas deliverability that can corresponding raising vapourizing furnace.And the coal gas that fine breeze reaction back generates can continue to participate in reaction in up process, increases the growing amount of methane to a certain extent.And by regulating duff that bottom sides sprays into and the amount of vaporized chemical, also can adjust the ratio of lump coal and fine coal, thereby improve operating load and the turndown ratio of single stove, and can suitably regulate the composition of product gas according to the needs of back system.In addition, this gasification technology can use dry powder, coal water slurry or coal oil mixture charging, has enlarged the use range of coal to a certain extent.
Be arranged at swirlers 75 in duff and the vaporized chemical burner 7 and further improved the mixed aerosol effect of duff and vaporized chemical burner 7 spout place oxygen, coal water slurry and/or carbonic acid gas, further improve speed of response and gas producing efficiency.
Circulating condensing water is arranged in volume tank 45, be used for cooling off and the coal gas of discharging being washed.Splendid attire is used for grey water outlet 457 dischargings that the buck of gas washing can be by being arranged on volume tank 45 bottoms in volume tank.
By the coal gas of volume tank 45 and since loose gas net 453 and foam-breaking strip 456 with and go up the metal prong 458 that arranges and reduced steam and a spot of ash content and the coal dust of carrying secretly in the coal gas, further purified coal gas.
Wherein one deck gas net 453 that looses is arranged in the buck of gas washing at least, evenly distributes in the buck of gas washing being used for to be conducive to synthetic gas, is beneficial to flush away solid entrainment wherein, as the coal dust of trace etc.And two-layer foam-breaking strip 456 is positioned at the buck top of gas washing, so that the air pocket of the synthetic gas through washing is smashed, to be conducive to remove the buck of sweeping along in the synthetic gas bubble, further purifies synthetic gas.Be conducive to the small bubbles of the synthetic gas through washing are smashed, to be conducive to remove the buck of sweeping along in the synthetic gas small bubbles, further purify synthetic gas again.
Although various embodiment of the present invention is described in context by embodiment, the present invention is not limited to this.Therefore, it is the restriction of the scope of the invention that above description should be used as, and scope of the present invention is limited by appended claim.It will be appreciated by those skilled in the art that under the situation that does not deviate from spirit of the present invention and can make various changes and change to the present invention, it all will fall within protection scope of the present invention.
Claims (22)
1. a classification gasification moving-bed gasification device (100) comprising:
Pressure shell (3), has first opening (31) at the top of described pressure shell, has second opening (33) in the bottom of described pressure shell, upper side at described pressure shell arranges first gas exit (4), and the same horizontal plane in described pressure shell (3) bottom of described classification gasification moving-bed gasification device (100) evenly arranges at least two vaporized chemical nozzles (10);
Add coal bunker (1), be arranged on first opening (31) at described pressure shell top;
Coal sparger (2) is arranged at the top of described pressure shell inside, and described coal sparger (2) comprises agitator;
Axial symmetrical water jacket (5) is arranged on the inboard of described first gas exit (4) below of described pressure shell (3), and the inside of described axial symmetrical water jacket (5) constitutes vaporizer (6);
Slag shock chamber (8) is arranged under described second opening (33) of described pressure shell (3) bottom, and described slag shock chamber (8) comprises circulation chilled water entrance (81) and circulation chilled water outlet (83); And
Seal slag bucket (9), be arranged on the below of described slag shock chamber (8);
It is characterized in that, described pressure shell (3) bottom and the residing same horizontal plane of described at least two vaporized chemical nozzles (10) at described classification gasification moving-bed gasification device (100) also alternately evenly arrange at least two duffs and vaporized chemical burner (7), wherein said at least two vaporized chemical nozzles are evenly arranged in the vapourizing furnace bottom along vapourizing furnace shell (3) in same horizontal plane, and described at least two vaporized chemical nozzles and described at least two duffs and vaporized chemical burner symmetric arrangement in same horizontal plane.
2. classification gasification moving-bed gasification device according to claim 1 (100), the described circulation chilled water entrance (81) that it is characterized in that described slag shock chamber (8) are in and are lower than described circulation chilled water outlet (83) and locate.
3. classification gasification moving-bed gasification device according to claim 1 (100), it is characterized in that the described circulation chilled water entrance (81) of described slag shock chamber (8) is in a side of described slag shock chamber (8), described circulation chilled water outlet (83) is in the opposite side away from the described slag shock chamber (8) of described circulation chilled water entrance (81).
4. classification gasification moving-bed gasification device according to claim 1 (100) is characterized in that described at least two vaporized chemical nozzles (10) and described at least two duffs and vaporized chemical burner (7) are selected from two vaporized chemical nozzles (10) and two duffs and vaporized chemical burner (7) respectively, three vaporized chemical nozzles (10) and three duffs and vaporized chemical burner (7), four vaporized chemical nozzles (10) and four duffs and vaporized chemical burner (7), five vaporized chemical nozzles (10) and five duffs and vaporized chemical burner (7), or six vaporized chemical nozzles (10) and six duffs and vaporized chemical burner (7).
5. classification gasification moving-bed gasification device according to claim 1 (100), it is characterized in that described duff and vaporized chemical burner (7) are to be made of two-layer at least circulating line, wherein duff and vaporized chemical are by the pipe-line transportation of the different layers of described duff and vaporized chemical burner (7).
6. classification gasification moving-bed gasification device according to claim 1 (100), it is characterized in that described coal bunker (1) upper end that adds is provided with feed coal import (15), the described lower end that adds coal bunker (1) links to each other with first opening (31) at described pressure shell top by flange.
7. according to each described classification gasification moving-bed gasification device (100) of claim 1～6, it is characterized in that described first gas exit (4) is connected with volume tank (45), described volume tank (45) further comprises:
Second gas entry (452) is arranged on the sidewall of described volume tank (45) middle part and a little less than described first gas exit (4), and is connected with second gas line (459) and extends into locating near the bottom of described volume tank (45),
Second gas exit (454) is arranged on described volume tank (45) upper portion side wall or the top, and is higher than described second gas entry (452),
Ash water outlet (457) is arranged on described volume tank (45) bottom,
At least one deck gas net (453) that looses is arranged on the below of described volume tank (45), and is installed on the inwall of described volume tank (45) and around described second gas line (459), and
At least one deck foam-breaking strip (456) is arranged on the top of described diffusing gas net (453), and is installed on the inwall of described volume tank (45) and is positioned at described second gas line (459) top that described second gas entry (452) connects.
8. classification gasification moving-bed gasification device according to claim 7 (100) is characterized in that, evenly is provided with metal prong (458) on each root foam-breaking strip of the described foam-breaking strip of one deck at least (456).
9. according to each described classification gasification moving-bed gasification device (100) of claim 1～6, it is characterized in that described at least two vaporized chemical nozzles (10) and described at least two duffs and vaporized chemical burner (7) removably evenly are crisscross arranged on described pressure shell (3).
10. according to each described classification gasification moving-bed gasification device (100) of claim 1～6, each that it is characterized in that described at least two duffs and vaporized chemical burner (7) is provided with swirler (75) at the spout place.
11. according to each described classification gasification moving-bed gasification device (100) of claim 1～6, it is characterized in that the spout level of described at least two vaporized chemical nozzles and described at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-45 °.
12. classification gasification moving-bed gasification device according to claim 11 (100), it is characterized in that the spout level of described at least two vaporized chemical nozzles and described at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-30 °.
13. classification gasification moving-bed gasification device according to claim 12 (100), it is characterized in that the spout level of described at least two vaporized chemical nozzles and described at least two duffs and vaporized chemical burner or arrange downwards, with the angular range of horizontal direction be 0-20 °.
14. classification gasification moving-bed gasification device according to claim 7 (100) is characterized in that described second gas line (459) near the place, bottom that extends into described volume tank (45) further comprises gas distributor.
15. an application rights requires the coal grading gasification process of the described gasifying device for graded gasification moving bed of any one (100) in 1～14, comprise: by the coal bunker (1) that adds that is positioned at top of gasification furnace, lump coal or type coal gasification raw material are added stove, simultaneously the first gasifying agent is sent into described gasification furnace by at least two the gasifying agent nozzles (10), the second gasified raw material and the second gasifying agent that arrange in the gasification furnace bottom sides by at least two duffs that consist of two-layer at least circulating line in the setting of gasification furnace bottom sides and gasifying agent burner (7) inner
Wherein said first vaporized chemical is selected from oxygen and water vapour or oxygen and CO
2Described second vaporized chemical is selected from oxygen, air, oxygen-rich air, the mixture of one or more in carbonic acid gas or the water vapour, described second gasified raw material is selected from fine particles containing carbon, contain carbon pastes or carbon containing inflammable gas, described fine particles containing carbon is selected from coal dust, the mixture of one or more in the organic powder of coal liquefaction residue powder and carbon containing, the described carbon pastes that contains is selected from coal water slurry, the coal liquefaction residue of fusion, the liquefied residue slip, coal oil mixture, the methyl alcohol coal slurry, the biomass slip, the mixture of one or more in light oil and the heavy oil
Described second gasified raw material and described second vaporized chemical be the pipe-line transportation of the different layers by described duff and vaporized chemical burner (7) respectively, described second gasified raw material that is sprayed into vapourizing furnace by described duff and vaporized chemical burner (7) accounts for total furnace coal weight, namely (lump coal+second gasified raw material) amount 10%-50%, the working pressure scope of described vapourizing furnace is 0.1-10MPa, base burning district temperature is 1300-1600 ℃, and temperature out is 400-600 ℃.
16. coal grading gasification process according to claim 15 is characterized in that, described fine particles containing carbon is biomass material powder.
17. coal grading gasification process according to claim 15, it is characterized in that described second gasified raw material is selected from dry coal powder, coal water slurry or coal oil mixture, described second gasified raw material that is sprayed into vapourizing furnace by described duff and vaporized chemical burner (7) accounts for total furnace coal weight, i.e. the 10%-50% of the amount of (lump coal+duff).
18. coal grading gasification process according to claim 17 it is characterized in that described second gasified raw material is the dry coal powder, and every cubic metre of conveying solid substance amount is greater than 400kg.
19. coal grading gasification process according to claim 17 is characterized in that described second gasified raw material is coal water slurry or coal oil mixture, the concentration of described coal water slurry or coal oil mixture is greater than 60wt%.
20. according to claim 17 or 18 described coal grading gasification process, it is characterized in that using nitrogen or carbonic acid gas as the delivery medium of described dry coal powder.
21. according to each described classification gasification moving-bed gasification device of claim 1～14 and according to each described coal grading gasification process of claim 15～20 in the application of preparation aspect synthetic gas, reducing gas or the fuel gas.
22. according to each described classification gasification moving-bed gasification device of claim 1～14 and according to each described coal grading gasification process of claim 15～20 in the application aspect preparation water-gas, the semi-water gas.
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