CN102604683A - Method for co-production of synthetic gas and coal tar - Google Patents
Method for co-production of synthetic gas and coal tar Download PDFInfo
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- CN102604683A CN102604683A CN2011104306421A CN201110430642A CN102604683A CN 102604683 A CN102604683 A CN 102604683A CN 2011104306421 A CN2011104306421 A CN 2011104306421A CN 201110430642 A CN201110430642 A CN 201110430642A CN 102604683 A CN102604683 A CN 102604683A
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Abstract
The invention discloses a method for the co-production of a synthetic gas and coal tar. The method comprises the following steps of: (a), adding coal dust into a coal pyrolysis area of a gasification furnace comprising the coal pyrolysis area and a coke gasification area, and making the coal dust contact with a coke gasification product material flow from the coke gasification area to at least partially pyrolyze the coal dust to generate a gas material flow containing the coal tar and the synthetic gas and coke; and (b) feeding the coke into the coke gasification area, making the coke contact with a gasification agent which is introduced into the coke gasification area and contains water vapor and oxygen to generate a coke gasification product material flow containing the synthetic gas and coke gasification residues, enabling the coke gasification product material to upwards flow to enter the coal pyrolysis area, and discharging the coke gasification residues out of the coke gasification area.
Description
Technical field
The invention belongs to the method for a kind of co-production synthesis gas and coal tar, relate in particular to a kind of with the coal raw material method of co-production synthesis gas and coal tar efficiently.
Background technology
Along with the scarcity day by day of oil and natural gas resource, the price of coal tar becomes increase trend.Mostly current Coal Gasification Technology is single process; As realized Texaco Water-coal-mud Gasification Technology and shell dried coal powder gasification technology of industrialization etc., under higher temperature and pressure, coal is become synthetic gas; The constructional feature of ignoring coal itself; Pressure all transforms all carbon, and this technological process has also been wasted the hydro carbons resource that is comprised in the coal except the material of reactor drum is had relatively high expectations.Along with the appearance of energy dilemma and the enhancing of people's environmental consciousness; Coal grading, clean transformation technology have been put on the research schedule; Like the Poly-generation technology of extensively being paid attention to by countries in the world, its principal feature is to start with from the structure of coal, takes to transform accordingly means according to coal characteristics.Based on this, the present invention proposes the method for a kind of co-production synthesis gas and coal tar, and main purpose is to realize that coal grading transforms, and has both utilized the hydro carbons resource of preciousness in the coal, improves the economy of process simultaneously.
Summary of the invention
The present invention relates to a kind of method, comprise the following steps: by coal co-production synthesis gas and coal tar
A. coal dust is joined the coal cracking district of the vapourizing furnace that comprises coal cracking district and char gasification district; And this coal dust is contacted with char gasification product materials flow from the char gasification district with the said coal dust of pyrolysis at least in part, generate the gas streams and the coal tar that comprise coal tar and synthetic gas;
B. said coal tar is sent into the char gasification district and contact with the vaporized chemical that comprises water vapour and oxygen that feeds said char gasification district; The materials flow of char gasification product and the char gasification residue that comprise synthetic gas with generation; This char gasification product materials flow upwards gets into said coal cracking district, and this char gasification residue is discharged this char gasification district.
Description of drawings
Fig. 1 is the schematic process flow diagram of method of the present invention.
It is understandable that accompanying drawing only is illustrative, do not plan to limit by any way scope of the present invention.Scope of the present invention should be confirmed by the content of claim.
Detailed Description Of The Invention
The core equipment for gasification that method of the present invention adopted is a vapourizing furnace.The general vertical placement of this vapourizing furnace or tilt to place, when tilting to place its angle of inclination be enough to make in the stove solid materials for example coal dust under himself gravity, move downward.Under the most general situation, can vapourizing furnace be divided into two districts or two sections from top to bottom, according to the function of each section, be followed successively by coal cracking district and char gasification district.Wherein, said coal cracking district has at least one coal opening for feed and at least one gas discharge port; Said char gasification district has at least one vaporized chemical opening for feed, at least one slag-drip opening, optional solid circle material opening for feed and vaporized chemical grid distributor; And also has the upflow tube that is used for the coal tar that behind coal cracking district partial thermal decomposition, is produced by coal is imported from said coal cracking district said char gasification district in the said vapourizing furnace.When this vapourizing furnace work, solid materials, for example coal; Get into the coal cracking district from said coal opening for feed, and motion from the top down, the char gasification residue finally generated; Leave vapourizing furnace from the slag-drip opening of vapourizing furnace bottom, and comprise the vaporized chemical of water vapour and oxygen, then get into said char gasification district from said vaporized chemical opening for feed; And motion from bottom to top, finally the gas discharge port from top of gasification furnace leaves vapourizing furnace.Solid materials and gas material are the form of counter current contact basically in vapourizing furnace.Vapourizing furnace of the present invention, high more the closer to bottom temp basically, low more the closer to head temperature.In addition, vapourizing furnace can separate with multihole distributor between two districts, has the hole that the supplied gas material passes through on this multihole distributor.Also connect on this multihole distributor and be provided with the upflow tube that is both ends open, this upflow tube is used to make solid materials, and for example coal, coal tar flow to the char gasification district of lower floor from top to bottom through upflow tube from the coal cracking district on upper strata.Each district at vapourizing furnace all can be provided with as required and is used for material; For example coal and vaporized chemical etc. feed the apparatus for feeding of vapourizing furnace; These apparatuss for feeding are well known to a person skilled in the art, for example feed bin, rotation feeding device and necessary connecting tube, or the like.In addition, also be provided with the conventional discharging equipment that supplied gas and char gasification residue leave vapourizing furnace in the top of vapourizing furnace and bottom.
In the method for the present invention, the feed entrance point of coal and gasifying agent can be selected or adjusts based on needs.For example, at least a portion coal can be from the coal cracking district of vapourizing furnace of the present invention and/or any one or a few place in char gasification district get into vapourizing furnace, but preferably with most of coal, more preferably will whole coals from the coal cracking district entering vapourizing furnace.Vaporized chemical then feeds the vapourizing furnace from the bottom and/or the side in char gasification district, and preferably bottom and the side from the char gasification district feeds jointly.
To the not restriction of using among the present invention of coal, it can be selected from bituminous coal, hard coal, brown coal etc., and preferably before getting into vapourizing furnace of the present invention, is ground into coal dust, and the granularity of coal dust generally can be below the 6mm.
Step a of the present invention occurs in the coal cracking district of vapourizing furnace; Joining coal dust in this district contacts with char gasification product materials flow from the char gasification district with the said coal dust of pyrolysis at least in part; Formation comprises the gas streams and the coal tar of the synthetic gas of coal tar; Wherein said synthetic gas is meant the gaseous mixture that comprises hydrogen and carbon monoxide, and said coal tar is meant the product that produces after coal dust is by partial thermal decomposition.It is wherein said that " partial thermal decomposition " comprises following several kinds of situation: make whole coal dust generation partial thermal decompositions, make the part coal dust that whole pyrolysis take place and make part coal dust generation partial thermal decomposition at least; In other words, " part at least " is to carry out degree in the amount of coal dust and pyrolytic reaction at least one is not completely in the two.All gas in this coal cracking district leaves vapourizing furnace from said gas discharge port, and said coal tar then moves downward along vapourizing furnace via said upflow tube, enters into said char gasification district.In this step a, will be at least part of coal feed vapourizing furnace from said coal cracking district, preferably with most coals in addition more preferably will whole coals from said coal cracking district the feeding vapourizing furnace.The benefit of doing like this is to have made full use of the gasification reaction institute liberated heat of coal tar in the char gasification district; This heat is along with the materials flow of char gasification product upwards gets into the coal cracking district; Contact with the coal that gets into vapourizing furnace from the coal cracking district; Make this coal preheating and fast pyrogenation, generate synthetic gas and coal tar, wherein coal tar is from fugitive constituent contained in the coal.Along with gaseous product leaves vapourizing furnace, the char gasification district that coal tar then enters into vapourizing furnace downwards continues reaction to tar under the condition in this district.Temperature in this coal cracking district mainly flow through the vaporized chemical that adds and the inlet amount that joins the coal dust in this district is regulated, and generally is 500-700 ℃.The pressure in coal cracking district is 0.1～4.0MPa (all pressure is absolute pressure among this paper).
Step b of the present invention occurs in the char gasification district of vapourizing furnace.In this step; Said coal tar is sent into the char gasification district and contacted with the vaporized chemical that comprises water vapour and oxygen that feeds said char gasification district; The materials flow of char gasification product and the char gasification residue that comprise synthetic gas with generation; This char gasification product materials flow upwards gets into said coal cracking district, and this char gasification residue is discharged this char gasification district.The principal reaction that in this char gasification district, takes place is following:
2C+2H
2O→2H
2+2CO (1)
C+O
2→CO
2 (2)
2C+O
2→2CO (3)
CO+H
2O→CO
2+H
2 (4)
The temperature of reaction in said char gasification district is 900～1100 ℃, and pressure is 0.1～4.0MPa.In the char gasification district, reaction institute heat requirement is mainly from the combustion reactions that takes place between carbon in the coal and the oxygen in the vaporized chemical.
Oxygen in the wherein said vaporized chemical is 0.2-1.0Nm with the ratio of said coal dust
3Oxygen/kg coal, the water vapour in the said vaporized chemical is 0.1-0.8kg water vapour/kg coal with the ratio of said coal dust.Nm wherein
3Be meant and be converted to standard state (298K, the volume of the gas under 101.325kPa).
In embodiment preferred of the present invention, can said vaporized chemical be divided into two strands and get into said char gasification districts, first plume through the vaporized chemical grid distributor that is arranged in said char gasification district with distributed entering; Concentrate from the centre hole that is positioned at the vaporized chemical grid distributor for second strand to get into, and control the deslagging in char gasification district through the gas speed of controlling second strand.More than throughput ratio between first strand and second strand can confirm according to concrete processing condition by those skilled in the art, for example, be 5: 1 to 30: 1.
In preferred embodiment of the present invention, can said vaporized chemical be divided into three strands and get into said char gasification districts, first plume through the vaporized chemical grid distributor that is arranged in said char gasification district with distributed entering; Second strand from the concentrated entering of the centre hole that is positioned at the vaporized chemical grid distributor; The 3rd strand through being arranged on the jet pipe entering of said vaporized chemical grid distributor top.The benefit of doing like this is to avoid pipe core to stop up because of slagging scorification effectively.More than first strand: second strand: the 3rd strand throughput ratio can be confirmed according to concrete processing condition by those skilled in the art, for example, is 5-30: 1: 0.5-10.
In a preferred embodiment of the invention, further comprising the steps of: as the said gas streams that comprises coal tar and synthetic gas through optional dedusting, to be carried out gas-liquid separation then, obtain comprising the gas streams and the liquid coal tar of synthetic gas.
Wherein dust removal operation can be carried out through the conventional dedusting technology in this area, for example carries out through cyclonic separator.This dust removal operation can not exist, but preferred the existence.Solid fine particle that can dust removal operation is collected is back to the char gasification district of said vapourizing furnace, so that make wherein contained carbon be able to again the generating gasification reaction, puies forward the high-carbon utilization ratio.
Wherein, carry out said gas-liquid separation through the said gas streams that comprises coal tar and synthetic gas of cooling in the indirect type water cooler, and/or carry out said gas-liquid separation through other gas-liquid separator (being preferably non-cooled gas-liquid separator).Wherein said indirect type water cooler is cooled to the temperature that wherein most of coal tar can become liquid with the temperature of said gas streams, for example is cooled to preferably be cooled to normal temperature below the boiling temperature of coal tar.This indirect type water cooler can use liquid water, preferred normal temperature water coolant as heat-eliminating medium.
Embodiment
Provide following examples to illustrate the present invention, these embodiment are also nonrestrictive.
Referring to Fig. 1, show to this illustrated property the process flow sheet of a preferred embodiment of the present invention.
Bituminous coal with from Shenmu County, Shaanxi is gasified raw material, is crushed to below the 6mm, joins in the feed bin 1 that has whipping appts for use.Vapourizing furnace 4 comprises the coal cracking district 19 that is in its epimere and 20 two districts, char gasification district that are in its hypomere at least; Separate with multihole distributor 6 between two districts, and make the solid materials in coal cracking district overflow get into the char gasification district through at least one upflow tube 5.When technology started, the hypomere at vapourizing furnace added extra coal tar particle earlier, is piled into bed; And the lower end of upflow tube 5 imbedded in this bed, about 1000 ℃ hot flue gases are got into vapourizing furnaces 4 from inlet mouth 7, be heated to 700-800 ℃ to vapourizing furnace 4; Stop heating; Open buncher 2, join feed coal in the coal cracking district 19 that is in vapourizing furnace 4 epimeres through screw feeder 3, treat that the overflow of upflow tube 5 is stable after; Stop to feed hot flue gas; And will be in the char gasification district 20 of vapourizing furnace 4 hypomeres through the entering of vaporized chemical grid distributor again from the air chamber of oxygen below inlet mouth 7 entering vaporized chemical grid distributors 9 of air separation facility, the ratio of oxygen and coal is 0.4Nm
3/ kg, treat material burn to furnace temperature stable after, the steam from vapour generator feeds vapourizing furnaces 4 through grid distributor 9 and pipe core 10 respectively again, 300 ℃ of vapor temperatures, steam in the boiler total amount and feed coal are than being 0.4kg/kg.The oxygen through regulating stove and the temperature of reaction in steam flow may command char gasification district are between 900-1100 degree centigrade.Behind the vapourizing furnace stable operation, the coal tar in the char gasification district then mainly leans on from the coal tar overflow in the coal cracking district of vapourizing furnace epimere and supplies, and can realize stable overflow through the pressure drop relation of regulating between upflow tube 5 and the multihole distributor 6.The char gasification residue that reaction produces enters slag bucket 11 by pipe core 10, can be regularly through valve 12 dischargings.The tar and the coal gas that leave vapourizing furnace get into gas cooler 15 through primary cyclone 13 and secondary cyclone 14 backs; This gas cooler 15 adopts indirect refrigerative method; Coal gas is cooled and is water-cooled to below 40 ℃, and most of tar gas is condensed into liquid tar in gas cooler 15 simultaneously.Cooled synthetic gas gets into gas-liquid separator 17, there still remaining some coal tar and synthetic gas is separated.Liquid tar from gas cooler 15 and gas-liquid separator 17 enters crude tar oil storage tank 16, obtains the crude tar oil product after the dehydration, and the synthetic gas that leaves gas-liquid separator 17 gets into gas holder 18, obtains the finished product synthetic gas.Flying dust (being mainly solid granule) in the primary cyclone 13 returns vapourizing furnace through material-returning device, and the lime-ash in the secondary cyclone 14 enters another slag bucket 11, but regular discharge.
Table 1 shows with reference to three groups of exemplary concrete processing condition and experimental results that adopted in the industrial experiment of above embodiment:
Advantage of the present invention is following:
(1) two district's coupled gasification, the fine coal that the coal cracking district of vapourizing furnace of the present invention utilizes the surplus temperature heating of char gasification district gaseous product just to get into carries out partial thermal decomposition; Produce synthetic gas and coal tar wet goods product, vapourizing furnace overall thermal efficient is higher, and efficiency of carbon conversion is high; Equipment is simplified, and is easy to operate.
(2) process is good through economy, and with respect to single gasification, coal tar can reduce the cost of unit synthetic gas greatly as one of product; Adopt two section fluidized-bed gasification furnaces that pyrolysis reactor and gasifying reactor are coupled, reduced investment of devices, improved the economy of process.
(3) coal adaptability is strong, and bituminous coal and brown coal all can be used as the raw material of method of the present invention.
Claims (8)
1. the method by coal co-production synthesis gas and coal tar comprises the following steps:
A. coal dust is joined the coal cracking district of the vapourizing furnace that comprises coal cracking district and char gasification district; And this coal dust is contacted with char gasification product materials flow from the char gasification district with the said coal dust of pyrolysis at least in part, generate the gas streams and the coal tar that comprise coal tar and synthetic gas;
B. said coal tar is sent into the char gasification district and contact with the vaporized chemical that comprises water vapour and oxygen that feeds said char gasification district; The materials flow of char gasification product and the char gasification residue that comprise synthetic gas with generation; This char gasification product materials flow upwards gets into said coal cracking district, and this char gasification residue is discharged this char gasification district.
2. the process of claim 1 wherein the temperature in coal cracking district in 500-700 ℃ of scope, char gasification district temperature is in 900-1100 ℃ of scope, and the absolute pressure in the vapourizing furnace is in the 0.1-4.0MPa scope.
3. according to the process of claim 1 wherein that the ratio of oxygen and said coal dust in the said vaporized chemical is 0.2-1.0Nm
3Oxygen/kg coal, the water vapour in the said vaporized chemical is 0.1-0.8kg water vapour/kg coal with the ratio of said coal dust.
4. according to the method for claim 1, further comprising the steps of: as the said gas streams that comprises coal tar and synthetic gas through optional dedusting, to be carried out gas-liquid separation then, obtain comprising the gas streams and the liquid coal tar of synthetic gas.
5. the method for claim 4 is wherein carried out said gas-liquid separation through the said gas streams that comprises coal tar and synthetic gas of cooling in the indirect type water cooler, and/or is carried out said gas-liquid separation through gas-liquid separator.
6. the process of claim 1 wherein that said vaporized chemical is divided into two strands and gets into said char gasification districts, first plume through the vaporized chemical grid distributor that is arranged in said char gasification district with distributed entering; Second strand from the concentrated entering of the centre hole that is positioned at the vaporized chemical grid distributor; And control the deslagging in char gasification district through the gas speed of controlling second strand.
7. the process of claim 1 wherein that said coal tar gets into said char gasification district downwards through upflow tube.
8. the process of claim 1 wherein that said vaporized chemical is divided into three strands and gets into said char gasification districts, first plume through the vaporized chemical grid distributor that is arranged in said char gasification district with distributed entering; Second strand from the concentrated entering of the centre hole that is positioned at the vaporized chemical grid distributor; The 3rd strand through being arranged on the jet pipe entering of said grid distributor top.
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| CN103087778A (en) * | 2013-01-28 | 2013-05-08 | 新奥科技发展有限公司 | Jet pipe, fluidized bed reactor with jet pipe and coal catalyzing and gasifying method |
| CN103571541A (en) * | 2012-07-30 | 2014-02-12 | 新奥科技发展有限公司 | Catalytic gasification method for co-production of methane and tar |
| CN103756732A (en) * | 2014-01-23 | 2014-04-30 | 上海锅炉厂有限公司 | Dual-fluidized bed low-carbon combustion and gasified heat-electricity-gas poly-generation device and method |
| CN103773507A (en) * | 2014-01-23 | 2014-05-07 | 上海锅炉厂有限公司 | Dual-bed burning and gasification poly-generation device and method |
| WO2014134920A1 (en) * | 2013-03-07 | 2014-09-12 | General Electric Company | Integrated pyrolysis and entrained flow gasification systems and methods for low rank fuels |
| CN104593089A (en) * | 2014-12-18 | 2015-05-06 | 广东正鹏生物质能源科技有限公司 | Self-heat supply type biomass oil gas co-production process |
| CN105112082A (en) * | 2015-08-10 | 2015-12-02 | 航天长征化学工程股份有限公司 | Pyrolysis device and pyrolysis equipment of coal |
| CN106433736A (en) * | 2016-09-28 | 2017-02-22 | 中石化宁波工程有限公司 | Direct coal hydrogenation reaction device and method |
| CN106987281A (en) * | 2017-05-25 | 2017-07-28 | 北京神雾电力科技有限公司 | The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal |
| US9874142B2 (en) | 2013-03-07 | 2018-01-23 | General Electric Company | Integrated pyrolysis and entrained flow gasification systems and methods for low rank fuels |
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| CN103571541B (en) * | 2012-07-30 | 2016-08-10 | 新奥科技发展有限公司 | A kind of co-production of methane and the catalysis gasification method of tar |
| CN103087778A (en) * | 2013-01-28 | 2013-05-08 | 新奥科技发展有限公司 | Jet pipe, fluidized bed reactor with jet pipe and coal catalyzing and gasifying method |
| CN103087778B (en) * | 2013-01-28 | 2014-11-05 | 新奥科技发展有限公司 | Jet pipe, fluidized bed reactor with jet pipe and coal catalyzing and gasifying method |
| US9874142B2 (en) | 2013-03-07 | 2018-01-23 | General Electric Company | Integrated pyrolysis and entrained flow gasification systems and methods for low rank fuels |
| WO2014134920A1 (en) * | 2013-03-07 | 2014-09-12 | General Electric Company | Integrated pyrolysis and entrained flow gasification systems and methods for low rank fuels |
| CN105229122A (en) * | 2013-03-07 | 2016-01-06 | 通用电气公司 | For the monoblock type pyrolysis of low-grade fuel and entrained flow bed gasification system and method |
| CN103756732B (en) * | 2014-01-23 | 2015-09-23 | 上海锅炉厂有限公司 | Double-fluidized-bed low-carbon combustion and the electric multi-joint-production apparatus of heat of gasification and method |
| CN103773507B (en) * | 2014-01-23 | 2015-08-19 | 上海锅炉厂有限公司 | Double bed burning and Gasification Polygeneration System device and method |
| CN103773507A (en) * | 2014-01-23 | 2014-05-07 | 上海锅炉厂有限公司 | Dual-bed burning and gasification poly-generation device and method |
| CN103756732A (en) * | 2014-01-23 | 2014-04-30 | 上海锅炉厂有限公司 | Dual-fluidized bed low-carbon combustion and gasified heat-electricity-gas poly-generation device and method |
| CN104593089A (en) * | 2014-12-18 | 2015-05-06 | 广东正鹏生物质能源科技有限公司 | Self-heat supply type biomass oil gas co-production process |
| CN105112082A (en) * | 2015-08-10 | 2015-12-02 | 航天长征化学工程股份有限公司 | Pyrolysis device and pyrolysis equipment of coal |
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| CN106987281A (en) * | 2017-05-25 | 2017-07-28 | 北京神雾电力科技有限公司 | The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal |
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Application publication date: 20120725 |