CN105441131A - Method for preparing ash and steam by oxidation and decarbonization of coal gasification ash residues - Google Patents
Method for preparing ash and steam by oxidation and decarbonization of coal gasification ash residues Download PDFInfo
- Publication number
- CN105441131A CN105441131A CN201510759757.3A CN201510759757A CN105441131A CN 105441131 A CN105441131 A CN 105441131A CN 201510759757 A CN201510759757 A CN 201510759757A CN 105441131 A CN105441131 A CN 105441131A
- Authority
- CN
- China
- Prior art keywords
- ash
- bed
- fluidized
- gas
- decarbonization
- 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
-
- 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
- C10J3/72—Other features
- C10J3/725—Redox processes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
- F22B1/1838—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines the hot gas being under a high pressure, e.g. in chemical installations
- F22B1/1846—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines the hot gas being under a high pressure, e.g. in chemical installations the hot gas being loaded with particles, e.g. waste heat boilers after a coal gasification plant
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention provides a method for preparing ash and steam by oxidation and decarbonization of coal gasification ash residues. The method comprises an oxidation and decarbonization process, an energy utilization process and a flue gas purification process. The coal gasification ash residues are taken as raw materials and produce an oxidation and decarbonization reaction with an oxidant by adopting a combined rapid bed-dense bed circulation reactor to prepare the ash and the steam, so that the utilization rate of the raw materials is high; and the energy utilization process mainly comprises the steps that medium-pressure steam is produced by heat transfer in the combined bed circulation reactor, low-pressure steam is produced by recovering high-temperature waste heat flue gas through a waste heat boiler, and ash residue cooling and fluidizing gas preheating are realized while high-temperature ash exchanges heat with the fluidizing gas. According to the method, resource utilization of inorganic ash and chemical energy contained in the gasification ash residues is simply and effectively realized, the reaction efficiency is high, the technological process is simple, the production cost is low, and the whole production process is basically free of wastes.
Description
Technical field
The invention belongs to gasification lime-ash and reclaim field, particularly a kind of method of gasification lime-ash oxidation and decarbonization ash content coproduction steam.
Background technology
China Economic development is faced with the dual-pressure of energy shortage and the environmental pollution day by day highlighted.Energy shortage, especially petroleum resources shortage propose severe challenge to economy of energy development and national energy security." the BP world energy sources statistical yearbook " of 2014 is pointed out, China's primary energy source total quantity consumed occupies first place in the world, but primary energy source consumption is still only 1/3 of the developed countries such as the U.S. per capita.China's total energy consumption within the following long term can be predicted and will keep quick growth.The endowment of resources that China's fossil energy presents " the oil-poor weak breath of rich coal " is that the New Coal Chemical Industry of raw material petrochemical complex substitute products is able to fast development with coal.
Coal petrochemical industry substitute products mainly with synthetic gas-methyl alcohol for Key Platform raw material.Gasification is the source of Chemical Industry, and correlation technique development rapidly.The various kinds of coal gas stoves such as Lurgi stove, BGL stove, GE vapourizing furnace, multi-nozzle stove, Tsing-Hua University's stove, space flight stove, Shell stove, GSP stove achieve abundant industrialization achievement.Typical Coal Gasification Technology is mainly with coal dust or the charging of coal water slurry form.Coal rank all can be gasified in a large number lime-ash after the gasification of different Coal Gasification Technology.Gasification lime-ash is primarily of vapourizing furnace furnace bottom lime-ash and furnace roof flying dust two portions composition.The a large amount of lime-ash produced in coal gasification course, not only will take a large amount of soil and store, and its percolate can pollute soil and water.Gasification ash content carbon, generally higher than 20%, can not be directly used in and produce material of construction, backfill or make fertilizer.The recycling of gasification lime-ash becomes the key subject that Chemical Industry needs solution badly.
Summary of the invention
In various Coal Gasification Technology, the by-product of gasification lime-ash is a ubiquitous problem.The resource utilization of gasification lime-ash recycles the economic worth that can improve lime-ash, can solve again lime-ash and store the environmental problem brought.CN104759249A proposes gasification lime-ash to reclaim soluble potassium, and obtains the method for active residue.CN103991898A proposes the method base metal catalysts in gasification lime-ash and rare metal Ga simultaneously reclaimed.CN102980195A proposes will gasify lime-ash and coal slime evenly blending by a certain percentage, then adds clay wash, is recycled in fluidized-bed combustion boiler combustion.
Not enough for prior art, the invention provides a kind of method of gasification lime-ash oxidation and decarbonization ash content coproduction steam.Present method can realize gasifying resource utilization of lime-ash is recycled, and gained ash content can make material of construction, and the carbon burning release heat energy and coproduction steam in lime-ash.
A method for gasification lime-ash oxidation and decarbonization ash content coproduction steam, it is characterized in that, the method comprises:
(1) oxidation and decarbonization process: the carbon in lime-ash and oxygenant generation oxidation and decarbonization reacts Formed oxide compound and release reaction is warm, obtains ash content after decarburization;
(2) Energy harvesting process: mainly comprise in Combined Cycle fluidized-bed and move hot coproduction middle pressure steam, waste heat boiler reclaims high-temperature flue gas waste heat coproduction low-pressure steam, and high temperature ash content and fluidized gas heat exchange realize lime-ash simultaneously and cool and fluidized gas preheating.
(3) gas cleaning process: flue gas discharge after water dust scrubber purification of heat boiler outlet.
In one example, described gasification lime-ash is one or more mixtures of various ature of coal coal dust or coal water slurry gasification gained lime-ash.
In one example, described decarburizing reaction process adopts fast bed-Mi bed Combined Cycle fluidized-bed.
In one example, described fast bed system fast fluidized bed, close bed system dense phase fluidized bed.
In one example, described fast bed-Mi bed Combined Cycle fluidized-bed adopts air or oxygen to be fluidized gas.
In one example, adopt in described Combined Cycle fluidized-bed and use water as heat transferring medium and move hot coproduction middle pressure steam by heat-exchanging tube bundle.
In one example, the pressure of the middle pressure steam of described coproduction is 1 ~ 3MPa.
In one example, described oxygenant is air or oxygen.
In one example, described waste heat boiler is adopted and is used water as heat transferring medium by heat-exchanging tube bundle recovery high-temperature flue gas waste heat, co-production low-pressure steam.
In one example, the pressure of the low-pressure steam of described coproduction is 0.3 ~ 0.8MPa, and flue gas is cooled to 100 ~ 200 DEG C.
In one example, described high temperature ash content and fluidized gas heat exchange in gas-solid heat exchange device.
In one example, described gas-solid heat exchange device system fluid-bed heat exchanger, fluidized gas is preheating to 500 ~ 750 DEG C, and lime-ash is cooled to 100 ~ 200 DEG C.
In one example, oxidation and decarbonization temperature of reaction is 550 ~ 850 DEG C.
According to a further aspect in the invention, provide a kind of gasification lime-ash treatment process, comprising: (1) utilizes fluidized-bed to carry out oxidation and decarbonization process to gasification lime-ash, obtains ash content and high-temperature flue gas; And (2) are while carrying out oxidation and decarbonization, the interchanger that fluidized-bed is arranged is utilized to reclaim the reaction heat of oxidation and decarbonization reaction release.
In one example, gasification lime-ash treatment process also comprises: utilize waste heat boiler to reclaim high-temperature flue gas waste heat coproduction low-pressure steam.
In one example, gasification lime-ash treatment process also comprises: utilize gas-solid heat exchange device cool the ash content that described fluidized-bed exports and carry out preheating to fluidized gas simultaneously, the fluidized gas wherein after preheating is input to described fluidized-bed.
In one example, described gas-solid heat exchange device is fluid-bed heat exchanger, and fluidized gas is preheating to 500 ~ 750 DEG C, and ash content is cooled to 100 ~ 200 DEG C.
In one example, gasification lime-ash treatment process also comprises: purify rear discharge by water dust scrubber to the flue gas that waste heat boiler is discharged.
In one example, the described reaction heat utilizing the interchanger that fluidized-bed is arranged to reclaim oxidation and decarbonization reaction release comprises: move hot coproduction middle pressure steam using water as heat transferring medium by interchanger.
In one example, described fluidized-bed is the one in following items: dense phase fluidized bed; The Combined Cycle fluidized-bed of fast fluidized bed and dense phase fluidized bed series combination.
In one example, described fluidized-bed adopts air or oxygen to double as fluidized gas and oxygenant.
In one example, gasification lime-ash treatment process also comprises: in the ash content export fluidized-bed, a part is input to fluidized-bed as circulating ash.
The beneficial effect of the embodiment of the present invention is:
Gasification lime-ash is obtained ash content by oxidation and decarbonization by the method technical process of the embodiment of the present invention, simultaneously by energy recovery byproduct steam, achieve the recycling of inorganic ash content and chemical energy contained by gasification lime-ash simply and effectively, reaction efficiency is high, technical process is simple, production cost is low, and whole production process produces without waste substantially.
Accompanying drawing explanation
Fig. 1 is the technological process schematic diagram of the gasification lime-ash oxidation and decarbonization ash content coproduction steam of the embodiment of the present invention;
Fig. 2 is the example arrangement of a kind of gasification lime-ash oxidation and decarbonization Combined Cycle fluidizer according to the embodiment of the present invention according to the embodiment of the present invention.
The fast bed bioreactor of number in the figure: 1-; The close bed bioreactor of 2-; 3-gas-solid heat exchange device; 4-waste heat boiler; 5-water dust scrubber;
101-lime-ash entrance; 102,115-fluidized gas entrance; 103,112-gas distributor; 104-circulating ash entrance; 105,116-heat transferring medium entrance; 106,111-heat-exchanging tube bundle; 107,110-heat transferring medium outlet; 108-fluid outlet; 109-fluid intake; 113-circulating ash entrance; 114-ash outlet; 117-air cement separator; 118-exhanst gas outlet.
Embodiment
Embodiments provide a kind of method of the lime-ash oxidation and decarbonization ash content coproduction steam that gasifies, below in conjunction with the drawings and specific embodiments, embodiments of the present invention is further illustrated.
It should be noted that, " gasification lime-ash " herein refers to various coal with coal water slurry or coal dust form through various vapourizing furnace gained gasification lime-ash, but is not limited to above-mentioned gasification lime-ash, is also applicable to the lime-ash of the certain carbon content rate of other process by-product.
In this article, " fast bed " refers to fast fluidized bed, and " close bed " refers to dense phase fluidized bed.
Before introducing the gasification lime-ash treatment process of the embodiment of the present invention, illustrate according to the embodiment of the present invention propose the fluidised bed system that oxidation and decarbonization reclaims heat is simultaneously carried out to gasification lime-ash.
Fig. 1 shows a kind of gasification lime-ash oxidation and decarbonization Combined Cycle fluidised bed system according to the embodiment of the present invention.
The Combined Cycle fluidised bed system of the present embodiment comprises the Combined Cycle fluidized-bed 10, gas-solid heat exchange device 3, waste heat boiler 4, the water dust scrubber 5 that are made up of fast fluidized bed 1 and dense phase fluidized bed 2.
According to the gasification ash residue treatment technology of the present embodiment, utilize Combined Cycle fluidized-bed 10 pairs of gasification lime-ash to carry out oxidation and decarbonization process, obtain ash content and high-temperature flue gas; And while carrying out oxidation and decarbonization, utilize the interchanger that fluidized-bed is arranged to reclaim the reaction heat of oxidation and decarbonization reaction release.
According to the gasification ash residue treatment technology of the present embodiment, waste heat boiler 4 is utilized to reclaim high-temperature flue gas waste heat coproduction low-pressure steam; Utilize gas-solid heat exchange device 3 cool the ash content that described fluidized-bed exports and carry out preheating to fluidized gas simultaneously, the fluidized gas wherein after preheating is input to described fluidized-bed.In one example, gas-solid heat exchange device is fluid-bed heat exchanger, and fluidized gas is preheating to 500 ~ 750 DEG C, ash content is cooled to 100 ~ 200 DEG C, and cooled ash content like this can use as material of construction, such as, be used for brickmaking, also directly can bury, and can not pollute.The flue gas of being discharged by water dust scrubber 5 pairs of waste heat boilers purifies rear discharge.The interchanger that fluidized-bed is arranged can be heat-exchanging tube bundle, can move hot coproduction middle pressure steam using water as heat transferring medium by interchanger.
It should be noted that, the system in combination circulating fluidized bed system shown in Fig. 1 is only example, can change component wherein, replace or remove as required.
In one example, Combined Cycle fluidized-bed 10 can adopt air or oxygen to double as fluidized gas and oxygenant.In one example, in the ash content that fluidized-bed can be exported, a part is input to fluidized-bed as circulating ash.
For clearly the present invention being described, below in conjunction with Fig. 2, example arrangement according to the gasification lime-ash oxidation and decarbonization Combined Cycle fluidizer 10 of the embodiment of the present invention and operation are described.
Fig. 2 shows the example arrangement of a kind of gasification lime-ash oxidation and decarbonization Combined Cycle fluidizer according to the embodiment of the present invention, and described Combined Cycle fluidizer comprises a fast fluidized bed 1 and a dense phase fluidized bed 2; Described fast fluidized bed 1 is the lifting tubular type bed body that diameter is unified; Described dense phase fluidized bed 2 comprises bed sections, taper connection section and expanding reach; Described fast fluidized bed lower end arranges gasification lime-ash entrance 101, fluidized gas entrance 102, circulating ash entrance 104 and heat transferring medium entrance 105, upper end arranges heat transferring medium outlet 107 and fluid outlet 108, and inside arranges panel-type air sparger 103 and heat-exchanging tube bundle 106; Described dense phase fluidized bed lower end arranges circulating ash outlet 113, ash outlet 114 and fluidized gas entrance 115, bed sections arranges heat transferring medium entrance 116 and heat transferring medium outlet 110, upper end arranges fluid intake 109 and exhanst gas outlet 118, and inside arranges annular tube type gas distributor 112, heat-exchanging tube bundle 111 and air cement separator 117; Fluid outlet 108 set by fast fluidized bed upper end is connected with fluid intake set by dense phase fluidized bed upper end by pipeline; Circulating ash outlet 113 set by dense phase fluidized bed lower end connects with circulating ash entrance 104 set by fast fluidized bed lower end.
The invention theory of the circulating fluidized bed of fast fluidized bed and dense phase fluidized bed combination is adopted to be in the present embodiment, (1) in fast fluidized bed, the gasification lime-ash entered, circulating ash form fast bed flow state under the effect of fluidizing agent, fluidizing agent comprises air or oxygen, doublely make oxygenant, react with the gasification lime-ash of charging and/or the part generation oxidation and decarbonization of the non-complete oxidation of circulating ash, then gas carry solid composition mixed stream leave fast fluidized bed, enter dense phase fluidized bed; (2) in dense phase fluidized bed, fluidizing gas velocity is comparatively slow, is adapted so that the part that oxidation and decarbonization does not occur in lime-ash fully contacts with fluidized gas, fully carries out oxidation and decarbonization reaction; (3) part in dense phase fluidized bed gained ash content turns back to fast fluidized bed as circulating ash, and the heat entrained by circulating ash passes to the gasification lime-ash of charging, thus makes, when steady-state operation, can not need additional thermal source.
In example above, fast fluidized bed is illustrated as the unified lifting tubular type fluidized-bed of diameter, but this is only example, the present invention is not limited thereto, fast fluidized bed can be the lifting tubular type fluidized-bed of non-diameter Unified Form, also can be the fast fluidized bed of other form being different from riser tube, such as taper riser tube.
In the above example, after fast fluidized bed, be connected to dense phase fluidized bed, such as turbulent fluidized bed.In alternate embodiments, the dense phase fluidized bed of other types can also be connected after fast fluidized bed, such as bubbling fluidized bed.
In the above example, dense phase fluidized bed is exemplified as and comprises bed sections, taper connection section and expanding reach.But this is preferred exemplary, and dense phase fluidized bed can be other forms, such as, have more section or less section.
The above-mentioned fluid left from fluid outlet is mixed stream, can comprise one or more in the lime-ash, circulating ash etc. of various gas, ash content, non-complete reaction.Here various gases can comprise unreacted fluidizing agent, flue gas.Gas in fast fluidized bed carries ash fast and grades from pneumatic outlet and leave, and enters dense phase fluidized bed through fluid intake 109.
In example above, have employed the Combined Cycle fluidized-bed of fast fluidized bed and dense phase fluidized bed, as the preferred version carrying out gasification lime-ash oxidation and decarbonization and carry out heat recuperation simultaneously.In alternate embodiments, can only adopt single dense phase fluidized bed to carry out above-mentioned oxidation and decarbonization reaction.
In example above, Combined Cycle fluidized-bed have employed a fast fluidized bed and a dense phase fluidized bed, as the preferred version carrying out gasification lime-ash oxidation and decarbonization and carry out heat recuperation simultaneously.In alternate embodiments, array mode can adopt more than one (namely multiple) fast fluidized bed and a dense phase fluidized bed, a fast fluidized bed and multiple dense phase fluidized bed, the form of multiple fast fluidized bed and multiple dense phase fluidized bed.
In the above example, fly-ash separator have employed water dust scrubber, but this is only example, can adopt other forms of cleaning apparatus.
The amount of circulating ash can regulate according to the amount of the gasification lime-ash of charging, makes it possible to sufficient heat to pass to gasification lime-ash.Preferably, the amount of circulating ash is greater than the amount of gasification lime-ash, and such as both ratios can be 40:1 ~ 120:1.
In example above, double as fluidizing agent and oxygenant with air or oxygen, this is preferred exemplary.In alternative embodiments, can using other gases as fluidized gas itself or fluidized gas, such as inert gas helium, Krypton etc. as a supplement, and using special pure oxygen or air as oxygenant.Fluidizing agent and oxygenant can enter from two entrances separated, also can upon mixing via a gas inlet input.
In the sufficient region of oxygen supply, oxygen is adopted to be that fluidized gas and oxygenant can reduce reactor size and corresponding reduction cost of equipment.
The panel-type air sparger 103 that described fast fluidized bed inside is arranged arranges multiple hole or multiple nozzle; The percentage of open area of described panel-type air sparger 103 accounts for 0.1% ~ 20% of grid distributor cross-sectional area.
The tubular gas sparger 112 that described dense phase fluidized bed inside is arranged is the ring structures of 1 ~ 5 ring for number of rings, each ring is arranged multiple hole or multiple nozzle: the perforated area of described tubular gas sparger 112 or jet area account for 0.1% ~ 20% of dense phase fluidized bed bed sections cross-sectional area.
Described heat-exchanging tube bundle is parallel to fluidized-bed axial array; In fast fluidized bed, heat-exchanging tube bundle cross-sectional area accounts for 0.1 ~ 25% of bed cross-sectional area; In dense phase fluidized bed, heat-exchanging tube bundle cross-sectional area accounts for 0.1 ~ 25% of bed sections cross-sectional area.
Described heat transferring medium is one or more of water coolant, hot water, steam or thermal oil;
Described air cement separator 117 is one or more of cyclonic separator, wire gauzee filter or sintered pipes strainer;
The material of described fluidizer is high temperature resistant carbon steel or stainless steel.
The bed temperature of described fluidizer is 550 DEG C ~ 850 DEG C.
The bed working pressure of described fluidizer is normal pressure ~ 0.5MPa.
Described fluidized gas is air or oxygen; Fluidized gas plays oxygenant effect simultaneously.
As one embodiment of the present of invention, provide a kind of method of gasification lime-ash oxidation and decarbonization ash content coproduction steam, it is characterized in that, the method comprises:
(1) oxidation and decarbonization process: the carbon in lime-ash and oxygenant generation oxidation and decarbonization reacts Formed oxide compound and release reaction is warm, obtains ash content after decarburization;
(2) Energy harvesting process: mainly comprise in Combined Cycle fluidized-bed and move hot coproduction middle pressure steam, waste heat boiler reclaims high-temperature flue gas waste heat coproduction low-pressure steam, and high temperature ash content and fluidized gas heat exchange realize lime-ash simultaneously and cool and fluidized gas preheating.
(3) gas cleaning process: flue gas discharge after water dust scrubber purification of heat boiler outlet.
The method of the embodiment of the present invention achieves the recycling of inorganic ash content and chemical energy contained by gasification lime-ash simply and effectively only by oxidation and decarbonization combination cot reactor, reaction efficiency is high, technical process is simple, and production cost is low, and whole production process produces without waste substantially.
In one example, raw material is made with coal water slurry gasification gained lime-ash;
In one example, decarburizing reaction process adopts fast bed-Mi bed Combined Cycle fluidized-bed; Fast bed system fast fluidized bed, close bed system dense phase fluidized bed;
In one example, fast bed-Mi bed Combined Cycle fluidized-bed adopts air to be fluidized gas, is especially suitable in the area of the supporting deficiency of oxygen.
Adopt in Combined Cycle fluidized-bed and use water as heat transferring medium and move hot coproduction middle pressure steam by heat-exchanging tube bundle;
In one example, the pressure of the middle pressure steam of coproduction is 1 ~ 3MPa, preferably 1 ~ 1.5MPa.
In one example, oxygenant is air; Air not only makes fluidized gas but also make oxygenant.
In one example, waste heat boiler is adopted and is used water as heat transferring medium by heat-exchanging tube bundle recovery high-temperature flue gas waste heat, co-production low-pressure steam; The pressure of the low-pressure steam of coproduction is 0.3 ~ 0.8MPa, preferably 0.3 ~ 0.5MPa, and flue gas is cooled to 100 ~ 200 DEG C, preferred 100-150 DEG C.
In one example, high temperature ash content and fluidized gas heat exchange in gas-solid heat exchange device; Gas-solid heat exchange device system fluid-bed heat exchanger, fluidized gas is preheating to 500 ~ 750 DEG C, preferred 550-650 DEG C, and lime-ash is cooled to 100 ~ 200 DEG C, preferred 100-150 DEG C.
In one example, oxidation and decarbonization temperature of reaction is 550 ~ 850 DEG C, preferred 600-750 DEG C.
Example 1:
As shown in Figure 1, gasification lime-ash is fed intake and is entered in fast bed bioreactor 101, oxidation and decarbonization rate 80%.Lime-ash fluidisation after part decarburization is left fast bed bioreactor 101 and is entered in close bed bioreactor 102, and oxidation and decarbonization rate reaches 99%.Ash content part circulation bottom close bed bioreactor 102 enters in fast bed bioreactor 101, and another part enters in gas-solid heat exchange device 103.The oxidation and decarbonization temperature of fast bed-Mi bed Combined Cycle fluidized-bed is at 650 DEG C, but this is only example.Adopt in Combined Cycle fluidized-bed and use water as heat transferring medium and move hot coproduction 1.0MPa middle pressure steam by heat-exchanging tube bundle
The hot ash content of 650 DEG C is discharged after gas-solid heat exchange device 103 is cooled to 150 DEG C, and meanwhile, fluidized gas air is preheated to 550 DEG C.
650 DEG C of high-temperature flue gas pass through heat-exchanging tube bundle heat exchange with water in waste heat boiler 104, and coproduction 0.3MPa low-pressure steam, flue-gas temperature is cooled to 110 DEG C
Flue gas discharge after water dust scrubber 105 purifies of heat boiler outlet.
Be described above various embodiments of the present invention, above-mentioned explanation is exemplary, and non-exclusive, and be also not limited to disclosed each embodiment.When not departing from the scope and spirit of illustrated each embodiment, many modifications and changes are all apparent for those skilled in the art.Therefore, protection scope of the present invention should be as the criterion with the protection domain of claim.
Claims (12)
1. a method for gasification lime-ash oxidation and decarbonization ash content coproduction steam, it is characterized in that, the method comprises:
(1) oxidation and decarbonization process: the carbon in lime-ash and oxygenant oxidation and decarbonization occur in Combined Cycle fluidized-bed and react Formed oxide compound and release reaction is warm, obtain ash content after decarburization;
(2) Energy harvesting process: mainly comprise in Combined Cycle fluidized-bed and move hot coproduction middle pressure steam, waste heat boiler reclaims high-temperature flue gas waste heat coproduction low-pressure steam, and high temperature ash content and fluidized gas heat exchange realize lime-ash simultaneously and cool and fluidized gas preheating.
(3) gas cleaning process: flue gas discharge after fly-ash separator purification of heat boiler outlet.
2. method according to claim 1, is characterized in that, one or more mixtures of the described gasification ash various ature of coal coal dust of slag system or coal water slurry gasification gained lime-ash.
3. method according to claim 1, is characterized in that, described decarburizing reaction process adopts fast bed-Mi bed Combined Cycle fluidized-bed.
4. method according to claim 3, is characterized in that, described fast bed-Mi bed Combined Cycle fluidized-bed adopts air or oxygen to be fluidized gas.
5. method according to claim 1, is characterized in that, adopts to use water as heat transferring medium and move hot coproduction middle pressure steam by heat-exchanging tube bundle in described Combined Cycle fluidized-bed.
6. according to the method for claim 1 or 5, it is characterized in that, the pressure of the middle pressure steam of described coproduction is 1 ~ 3MPa.
7. method according to claim 1, is characterized in that, described oxygenant is air or oxygen.
8. method according to claim 1, is characterized in that, described waste heat boiler is adopted and used water as heat transferring medium by heat-exchanging tube bundle recovery high-temperature flue gas waste heat, co-production low-pressure steam.
9. according to the method for claim 1 or 8, it is characterized in that, the pressure of the low-pressure steam of described coproduction is 0.3 ~ 0.8MPa, and flue gas is cooled to 100 ~ 200 DEG C.
10. method according to claim 1, is characterized in that, high temperature ash content and fluidized gas heat exchange in gas-solid heat exchange device.
11. according to the method for claim 1 or 10, and it is characterized in that, described gas-solid heat exchange device system fluid-bed heat exchanger, fluidized gas is preheating to 500 ~ 750 DEG C, and lime-ash is cooled to 100 ~ 200 DEG C.
12. methods according to claim 1, is characterized in that, oxidation and decarbonization temperature of reaction is 550 ~ 850 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510759757.3A CN105441131B (en) | 2015-11-10 | 2015-11-10 | A kind of method of coal gasification lime-ash oxidation and decarbonization ash content coproduction steam |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510759757.3A CN105441131B (en) | 2015-11-10 | 2015-11-10 | A kind of method of coal gasification lime-ash oxidation and decarbonization ash content coproduction steam |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105441131A true CN105441131A (en) | 2016-03-30 |
| CN105441131B CN105441131B (en) | 2018-04-20 |
Family
ID=55551781
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510759757.3A Active CN105441131B (en) | 2015-11-10 | 2015-11-10 | A kind of method of coal gasification lime-ash oxidation and decarbonization ash content coproduction steam |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105441131B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108620002A (en) * | 2018-06-15 | 2018-10-09 | 陕西化建工程有限责任公司 | A kind of temperature control fluidizes fast bed reactor and its technological process |
| CN110172362A (en) * | 2019-05-16 | 2019-08-27 | 新奥科技发展有限公司 | A kind of catalytic coal gasifaction method |
| CN113955757A (en) * | 2021-11-26 | 2022-01-21 | 内蒙古禹源机械有限公司 | Device and process for preparing carbon dioxide capture agent and co-producing hydrogen and alloy from carbon and gasified slag |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1065286A (en) * | 1992-05-25 | 1992-10-14 | 中国石油化工总公司洛阳石油化工工程公司 | Improved two-stage regeneration for fluid catalytic cracking catalyst |
| JP2000213709A (en) * | 1999-01-20 | 2000-08-02 | Idemitsu Kosan Co Ltd | Manufacture of low unburned carbon ash |
| CN101265008A (en) * | 2008-04-22 | 2008-09-17 | 东南大学 | Sludge drying burning combination treatment method |
| CN102506420A (en) * | 2011-10-26 | 2012-06-20 | 重庆大学 | Coal ash fluidized bed combustion decarburization device |
| CN102676231A (en) * | 2011-03-14 | 2012-09-19 | 美特索电力公司 | An method for processing ash, and an ash processing plant |
-
2015
- 2015-11-10 CN CN201510759757.3A patent/CN105441131B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1065286A (en) * | 1992-05-25 | 1992-10-14 | 中国石油化工总公司洛阳石油化工工程公司 | Improved two-stage regeneration for fluid catalytic cracking catalyst |
| JP2000213709A (en) * | 1999-01-20 | 2000-08-02 | Idemitsu Kosan Co Ltd | Manufacture of low unburned carbon ash |
| CN101265008A (en) * | 2008-04-22 | 2008-09-17 | 东南大学 | Sludge drying burning combination treatment method |
| CN102676231A (en) * | 2011-03-14 | 2012-09-19 | 美特索电力公司 | An method for processing ash, and an ash processing plant |
| CN102506420A (en) * | 2011-10-26 | 2012-06-20 | 重庆大学 | Coal ash fluidized bed combustion decarburization device |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108620002A (en) * | 2018-06-15 | 2018-10-09 | 陕西化建工程有限责任公司 | A kind of temperature control fluidizes fast bed reactor and its technological process |
| CN110172362A (en) * | 2019-05-16 | 2019-08-27 | 新奥科技发展有限公司 | A kind of catalytic coal gasifaction method |
| CN113955757A (en) * | 2021-11-26 | 2022-01-21 | 内蒙古禹源机械有限公司 | Device and process for preparing carbon dioxide capture agent and co-producing hydrogen and alloy from carbon and gasified slag |
| CN113955757B (en) * | 2021-11-26 | 2023-11-03 | 内蒙古禹源机械有限公司 | Device and process for preparing carbon dioxide capturing agent from gasified slag and combining hydrogen and alloy |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105441131B (en) | 2018-04-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10208948B2 (en) | Solid fuel grade gasification-combustion dual bed poly-generation system and method thereof | |
| CN101245264B (en) | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method | |
| CN107418634B (en) | Multistage cooling and dedusting process and device for circulating fluidized bed coal gasification | |
| CN202543155U (en) | Combined circulation system for gasified combustion and catalyst regeneration by adopting heat carrier as basis | |
| CN105062528B (en) | A kind of pyrolysis of coal multi-production process and its device suitable for coal-powder boiler | |
| CN103740409B (en) | Multi-stage gas distribution high-temperature coal gasification device and method | |
| CN101550361A (en) | Under nozzle-type entrained flow gasification shock chilling device and shock chilling technology | |
| CN102146301A (en) | Method for two-stage coal gasification on composite external heat fixed bed and gas furnace | |
| CN101892081B (en) | Process for chemical poly-generation of coal-based energy | |
| CN101665724A (en) | Water-coal-slurry gasification method and gasification furnace | |
| CN204058390U (en) | Solid fuel classification gasification-burning double bed polygenerations systeme | |
| CN105441131A (en) | Method for preparing ash and steam by oxidation and decarbonization of coal gasification ash residues | |
| CN107057768B (en) | Dry coal powder gasification furnace with air preheating and steam generation functions and method thereof | |
| CN100577774C (en) | Differential bed catalytic coal gasifaction stove and catalysis gasification method | |
| CN211227042U (en) | Device for catalytic hydrogen production and power generation of biomass | |
| CN105396518B (en) | A kind of combination circulating fluid bed reactor of coal gasification lime-ash oxidation and decarbonization | |
| CN108410509B (en) | Coke powder and coal gas environment-friendly production method based on pulverized coal pure oxygen semi-gasification | |
| CN107641528B (en) | Energy-saving water-gas/steam co-production gasification process | |
| CN111718757A (en) | Thermal power plant coal pyrolysis gas hydrogen production system and method | |
| CN111718756A (en) | Thermal power plant pyrolysis hydrogen production system and hydrogen production method | |
| CN210287240U (en) | Combined bed coal gasification system | |
| CN111676065A (en) | Biomass and coal co-gasification system and gasification method | |
| CN108517227B (en) | Industrial gas preparation system and industrial gas preparation method | |
| CN210122559U (en) | Thermal power plant pyrolysis hydrogen production system | |
| CN112646609A (en) | Device and method for producing hydrogen by gasifying biomass |
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 |