CN103740409A - Multi-stage gas distribution high-temperature coal gasification device and method - Google Patents
Multi-stage gas distribution high-temperature coal gasification device and method Download PDFInfo
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- CN103740409A CN103740409A CN201410030040.0A CN201410030040A CN103740409A CN 103740409 A CN103740409 A CN 103740409A CN 201410030040 A CN201410030040 A CN 201410030040A CN 103740409 A CN103740409 A CN 103740409A
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Abstract
The invention discloses a multi-stage gas distribution high-temperature coal gasification device and a multi-stage gas distribution high-temperature coal gasification method. According to the device, an oxygen-enriched combustion section, a mixed gasification section, a gasification temperature-rise section and a gasification lifting section are arranged in a gasification reactor from bottom to top and are respectively provided with an independent gasifying agent, so that different reaction conditions of coal in each section are realized, the oxygen-enriched combustion section performs oxygen-enriched combustion on fuel to release heat so as to provide most of the heat needed by a gasification reaction, and the mixed gasification section, the gasification temperature-rise section and the gasification lifting section respectively perform different degrees of combustion and gasification reactions. During multi-stage gas distribution, gas is distributed according to the reaction characteristics of each section, the consumption of oxygen is greatly reduced, and high reaction temperature is kept in the gasification reactor; meanwhile, the temperature is uniformly distributed in the gasification reactor, and gasification with high gasification efficiency, high carbon conversion rate and low pollution is realized.
Description
Technical field
The present invention relates to a kind of multistage distribution high-temperature coal gasification device and method, belong to Coal Gasification Technology.
Background technology
Gasification is the important channel of coal high-efficiency and clean utilization, and it is that primary energy source is converted into clean secondary energy, and its gas product can be used as the multiple gases sources such as combustion gas (coal gas), synthetic gas, hydrogen, carbon monoxide.Coal Gasification Technology is widely used in the fields such as synthetic ammonia, synthesizing methanol, sponge iron production, and its potential biggest market is integrated gasification combined cycle plants (1GCC) power field.
Industrialized Coal Gasification Technology can be divided into 3 classes, the fluidized-bed gasification technology that the fixed bed gasification technology that the Lurgi technology of take is representative, the HTW technology of take are representative and the entrained flow bed gasification technology that Texaco, Shell, the opposed gasification technology of multi-nozzle be representative of take.External industrialized gasification air-flow bed coal-gasification technology mainly contains take the GE(Texaco that coal water slurry is raw material) gasification technology, Global E-Gas gasification technology, the Shell gasification technology that the dried coal powder of take is raw material, Prenflo gasification technology, GSP gasification technology etc.These gasifying process all exist some problems, and the coal adaptability of fixed bed is poor, high to ingredient requirement, in coal ash, carbon content rate is high, and the coal adaptability of fluidized-bed is better, and gasification efficiency is high, but lower at gasification temperature, in flying dust, remaining carbon is higher, the carbon content in deslagging is higher, the coal adaptability of air flow bed is good, and gasification efficiency is high, and environmental pollution is little, but require high to fineness of pulverized coal, pulverizing energy consumption is high, and coal dust can not preheating, and oxygen depletion amount is large.
The problem existing for traditional gasifying process, various countries scientific research institution has developed some new gasifying process.Wherein, the dense phase transporting bed gasification technique that U.S. KBR proposes, with respect to traditional circulating fluidized bed, solid circulation speed and the gas velocity of this technique are fast, it is high that riser densities is wanted, and therefore has higher throughput and efficiency of carbon conversion, and heat transfer and rate of mass transfer are higher.The bed bioreactor that transports of U.S. KBR has been obtained remarkable break-throughs, and the coal gasification apparatus of certain IGCC transformation project adopts TRIG Coal Gasification Technology at home, and the first industry that becomes the whole world should adopt the project of TRIG Coal Gasification Technology.Similar circulating fluidized bed pilot plant is also all had in Australia HRL company and India BHEL company.The domestic research major part for dense phase transporting bed gasification technique is still under test, " dense-phase conveying-bed coal pressurizing gasifying apparatus and method (CN101024782A) " that Southeast China University proposes, Shaanxi extends " a kind of transporting bed gasification and thermoelectric integrated device (CN202912920U) " that oil (group) proposes, " fine coal pressurization dense phase transporting bed gasification method and device (CN101240196A) " that Institute of Engineering Thernophysics, Academia Sinica provides.In addition, " the fine coal combined cyclic fluidized bed classification pyrolytic gasification technique (CN102965157A) " that China University Of Petroleum Beijing proposes, " a kind of staged high-temperature combustion circulating fluidized bed system and combustion method (CN101806451A) " that Inst. of Mechanics, CAS proposes.
New type coal gasification research has obtained greater advance, but still exists following problem: (1) reactor temperature is lower, and gasification reaction efficiency is not high, and efficiency of carbon conversion is not high, and easily generates objectionable impurities; (2) in reactor, flow velocity is too fast, and gasification reaction does not carry out completely, and carbon residue is more, and in flying dust, carbon residue is more; (3) inequality of being heated in reactor, temperatures at localized regions is higher, causes avoiding the lining life-span partially short; (4) consume a large amount of oxygen, gasification cost is high.Dense-phase conveying coal gasifying process has a broad prospect of the use at China's tool, and domestic industry Coal Gasification Technology mostly is to absorb and introduces at present, significant to the independent research of its technique.
Summary of the invention
Goal of the invention: in order to overcome the deficiencies in the prior art, the invention provides a kind of multistage distribution high-temperature coal gasification device and method, solve the problem that existing large-scale coal gasifying process and existing dense-phase conveying coal gasifying process exist, have that coal adaptability is good, temperature distribution is reasonable, gasification efficiency is high, efficiency of carbon conversion is high, pollute the advantages such as low.
Technical scheme: for achieving the above object, the technical solution used in the present invention is:
A multistage distribution coal gas of high temperature gasifying device, comprises gasifying reactor and air compartment, and described air compartment is arranged on the bottom of gasifying reactor, and described gasifying reactor is divided into oxygen-enriched combusting section, mixing gasifying section, gasification intensification section and gasification raising section from the bottom to top; Described oxygen-enriched combusting section is upwards shunk and is transitted to mixing gasifying section, and mixing gasifying section upwards contraction transits to the section that heats up that gasifies, and gasification intensification section is upwards shunk and transitted to gasification raising section;
On described air compartment, be provided with air compartment gasification agent inlet and air compartment scum pipe;
Described oxygen-enriched combusting pars infrasegmentalis side is provided with one-level opening for feed, one-level returning charge mouth and two one-level gasification agent inlets;
Described mixing gasifying pars infrasegmentalis side is provided with secondary opening for feed, secondary returning charge mouth and two secondary gasification agent inlets;
A side, described gasification intensification section middle part is provided with four three grades of gasification agent inlets;
Side, middle part, described gasification raising section is provided with four level Four gasification agent inlets;
Described gasification raising section top exit connects primary cyclone and secondary cyclone successively; Described primary cyclone bottom is connected with one-level downtake, one-level returning charge valve and downward-sloping one-level returning charge inclined tube in turn, described one-level returning charge inclined tube access one-level returning charge mouth; Described secondary cyclone bottom is connected with secondary downtake, secondary returning charge valve and downward-sloping secondary returning charge inclined tube in turn, described secondary returning charge inclined tube access secondary returning charge mouth.
Preferably, the diameter of described oxygen-enriched combusting section is D, highly for H, and one-level gasification agent inlet is H/5 apart from the distance of oxygen-enriched combusting section bottom, and one-level opening for feed and one-level returning charge mouth are H/2 apart from the distance of oxygen-enriched combusting section bottom; The diameter of described mixing gasifying section is D
2=4D/5, be highly H
2=3H, secondary opening for feed is H apart from the distance of mixing gasifying section bottom
2/ 5, secondary gasification agent inlet and secondary returning charge mouth are H apart from the distance of mixing gasifying section bottom
2/ 3; The diameter of described gasification intensification section is D
3=3D/5, be highly H
3=4H/3, three grades of gasification agent inlets are H apart from the heat up distance of section bottom of gasification
3/ 4; The diameter of described gasification raising section is D
4=D/2, be highly H
4=2H, level Four gasification agent inlet is H apart from the distance of bottom, gasification raising section
4/ 6.
Preferably, the angle of described one-level returning charge inclined tube and horizontal plane is α
1, α
1it is 35～45 °; The angle of described secondary returning charge inclined tube and horizontal plane is α
2, α
2it is 35～45 °.
Preferably, described two one-level gasification agent inlets are placed in sustained height, are evenly arranged in all sides of oxygen-enriched combusting section, and the pipeline of access one-level gasification agent inlet is the first level pipe; Described two secondary gasification agent inlets are placed in sustained height, are evenly arranged in all sides of mixing gasifying section, and the pipeline of access secondary gasification agent inlet is the second level pipe; Described four three grades of gasification agent inlets are placed in sustained height, are evenly arranged in all sides of gasification intensification section, and the pipeline of three grades of gasification agent inlets of access is the 3rd inclined tube, and the angle of described the 3rd inclined tube and horizontal plane is β
3, β
3it is 15～20 °; Described four level Four gasification agent inlets are placed in sustained height, are evenly arranged in all sides of gasification raising section, and the pipeline of access level Four gasification agent inlet is the 4th inclined tube, and the angle of described the 4th inclined tube and horizontal plane is β
4, β
4it is 15～20 °.
This device is respectively from the bottom to top oxygen-enriched combusting section, mixing gasifying section, gasification heat up four sections of section and gasification raising sections in gasifying reactor, and every section is respectively equipped with independently vaporized chemical import, realizes the differential responses condition of each section of coal; Oxygen-enriched combusting section provides gasification reaction required most of heat by the heat release of fuel oxygen-enriched combusting, and burning, gasification reaction in various degree carried out respectively in mixing gasifying section, gasification intensification section and gasification raising section.Multistage distribution is carried out distribution according to the reaction characteristics of gasifying reactor different heights, greatly reduced the consumption of oxygen, when keeping temperature of reaction higher in gasifying reactor, realize being uniformly distributed of temperature, realize high gasification efficiency, high carbon conversions, oligosaprobic gasification.
A multistage distribution high-temperature coal gasification method, maintains the middle high temperature of 800～1300 ℃ in gasifying reactor, comprise the steps:
(1) pass through one-level opening for feed by one-level mixture b
1add oxygen-enriched combusting section, by air compartment gasification agent inlet, air compartment vaporized chemical a added to air compartment simultaneously, by one-level gasification agent inlet by one-level vaporized chemical a
1add oxygen-enriched combusting section; One-level mixture b
1in oxygen-enriched combusting section, carry out oxygen-enriched combusting, discharge amount of heat, for the gasification of mixing gasifying section provides heat, the gas-solid mixture that burning generates enters mixing gasifying section; Described gas-solid mixture comprises coke, the CO of high temperature
2, H
2o etc.;
(2) pass through secondary opening for feed by two-stage mixture material b
2add mixing gasifying section, pass through secondary gasification agent inlet by secondary vaporized chemical a simultaneously
2add mixing gasifying section; Two-stage mixture material b
2the heat being provided by oxygen-enriched combusting section heats, with oxygen generation combustion reactions, and with water vapour generation part gasification reaction, the burning of oxygen and combustiblematerials makes gasification temperature that mixing gasifying section can continue to keep higher and higher gasification efficiency; Along with the carrying out of gasification reaction, the temperature of reaction of mixing gasifying section constantly declines from bottom to top, and gas-solid mixture continues rising and enters gasification intensification section;
(3) pass through three grades of gasification agent inlets by three grades of vaporized chemical a
3add gasification intensification section; The coal gas that burns away and generate on a small quantity, for gasification reaction continues to provide heat, and the heat of supplemental equipment heat radiation, improve gas-solid mixture temperature; The gas-solid mixture that reaction generates continues rising and enters gasification raising section;
(4) pass through level Four gasification agent inlet by level Four vaporized chemical a
4add gasification raising section, make to account for the fully gasification in gasification raising section of the difficult vaporising fuel of fuel 10～20% small particle size, to improve gasification efficiency;
(5) the heating gas d generating in gasifying reactor enters primary cyclone and carries out gas solid separation, isolates one-level carbon residue g and primary dust removing coal gas e; One-level carbon residue g controls by one-level returning charge valve, sends into oxygen-enriched combusting section and carries out oxygen-enriched combusting, for gasification installation provides heat by one-level returning charge mouth; Primary dust removing coal gas e enters secondary cyclone and enters secondary separation, and isolated secondary carbon residue h controls by secondary returning charge valve, by secondary returning charge mouth, enters mixing gasifying section and propellant combination carries out combustion gasification jointly.
Preferably, described one-level mixture b
1account for below 30～50% of whole propellant combinations, particle diameter is 5～10mm, two-stage mixture material b
2particle diameter be below 5mm.
Preferably, described air compartment vaporized chemical a and one-level vaporized chemical a
1be oxygen, wherein air compartment vaporized chemical a accounts for 25% of the required vaporized chemical cumulative volume of device, one-level vaporized chemical a
1account for 15% of the required vaporized chemical cumulative volume of device; Secondary vaporized chemical a
2for the gas mixture of oxygen and superheated vapour, secondary vaporized chemical a
2account for 35% of the required vaporized chemical cumulative volume of device, wherein the volume fraction of oxygen is 20～40%; Three grades of vaporized chemical a
3for air, three grades of vaporized chemical a
3account for 15% of the required vaporized chemical cumulative volume of device; Level Four vaporized chemical a
4for the gas mixture of oxygen and superheated vapour, level Four vaporized chemical a
4account for 10% of the required vaporized chemical cumulative volume of device, wherein the volume fraction of oxygen is 10～30%.The vaporized chemical tolerance passing into of every grade of gasification agent inlet is the decile that this grade passes into gasification dosage.
Preferably, the service temperature of oxygen-enriched combusting section is 1000-1300 ℃, and the service temperature of mixing gasifying section is 800-1000 ℃, and the service temperature of gasification intensification section is 900-1000 ℃, and the service temperature of gasification raising section is 800-900 ℃.
Beneficial effect: multistage distribution high-temperature coal gasification device and method provided by the invention, the prior art of comparing, exist following a little: 1, gasifying reactor adopts oxygen-enriched combusting section, mixing gasifying section, gasification heat up section and gasification four sections of raising sections design, speed of reaction for the differential responses stage, adopt different diameter, height design, increased the gas-solid mixing in gasifying reactor, guaranteed the residence time in propellant combination gasifying reactor, make propellant combination fully gasification in gasifying reactor, improve carbon turnover ratio, outlet flying dust is few; 2, adopt classification charging, 30～50% fresh fuel is carried out oxygen-enriched combusting in oxygen-enriched combusting section, produce high-temperature flue gas to gasifying reactor heat supply, remaining fresh fuel is added by mixing gasifying section, kept the middle hot conditions in gasifying reactor, avoid excessive fresh fuel to burn in advance at oxygen-enriched burner, improved thermo-efficiency and the efficiency of carbon conversion of system; 3, adopt multistage distribution, make the comparatively stable heat supply of each Duan Douyou in gasifying reactor, gasification reaction temperature remains under the high temperature of 800～1300 ℃ carries out, and has greatly improved the gasification efficiency of system, has improved the efficiency of carbon conversion of system; 4, adopt the mode of multistage distribution, the air inlet of many vaporized chemicals mouth to add vaporized chemical, make the uniformity of temperature profile in whole gasifying reactor, in different pipe sections, pass into the vaporized chemical of different components, guaranteed each section of required gasification demand, greatly reduce the consumption of oxygen, reduced gasification cost; 5, level Four vaporized chemical adopts respectively different angles air inlet, one secondary vaporized chemical horizontal access enters and has guaranteed the residence time and the travelling speed of propellant combination in oxygen-enriched combusting section, mixed lifting section, three level Four vaporized chemicals have angle entrance to make being added in of vaporized chemical in stove, cause certain disturbance, the transmission of strengthening caloic, extend the residence time of gas-solid mixture in gasification intensification section and gasification raising section, improved gasification efficiency.
Accompanying drawing explanation
Fig. 1 is apparatus of the present invention structural representation;
Fig. 2 is the scantlings of the structure schematic diagram of gasifying reactor;
Fig. 3 is the scantlings of the structure figure of oxygen-enriched combusting section, and wherein Fig. 3 (a) is front view, and Fig. 3 (b) is vertical view, and Fig. 3 (c) is left view;
Fig. 4 is the scantlings of the structure figure of mixing gasifying section, and wherein Fig. 4 (a) is front view, and Fig. 4 (b) is vertical view, and Fig. 4 (c) is left view;
Fig. 5 is the scantlings of the structure figure of gasification intensification section, and wherein Fig. 5 (a) is front view, and Fig. 5 (b) is vertical view;
Fig. 6 is the scantlings of the structure figure of gasification raising section, and wherein Fig. 6 (a) is front view, and Fig. 6 (b) is vertical view;
Fig. 7 is a kind of implementation system schematic diagram of the present invention;
Comprise: gasifying reactor 1, oxygen-enriched combusting section 101, mixing gasifying section 102, gasification intensification section 103, gasification raising section 104, one-level gasification agent inlet 111, secondary gasification agent inlet 121, three grades of gasification agent inlets 131, level Four gasification agent inlet 141, one-level opening for feed 151, secondary opening for feed 161, air compartment gasification agent inlet 2, air compartment 100, air compartment scum pipe 3, primary cyclone 4, secondary cyclone 5, one-level downtake 6, secondary downtake 7, one-level returning charge valve 8, one-level returning charge inclined tube 81, secondary returning charge valve 9, secondary returning charge inclined tube 91, one-level returning charge mouth 10, secondary returning charge mouth 11, waste heat boiler 12, vapor superheater 13, preheater 14, gas cleaning device 15, association circulating power generation system 16, deaerator 110, the first mixing tank 120, the second mixing tank 130, air compartment vaporized chemical a, one-level vaporized chemical a
1, secondary vaporized chemical a
2, three grades of vaporized chemical a
3, level Four vaporized chemical a
4, one-level mixture b
1, two-stage mixture material b
2, gas-solid mixture c, heating gas d, primary dust removing coal gas e, two-stage dust removal coal gas f, one-level carbon residue g, secondary carbon residue h, one-level is returned charcoal i, and secondary returns charcoal j, pure water k
0, Low Temperature Steam k, the first superheated vapour m
0, the second superheated vapour m
1, middle low temperature coal gas l, low temperature coal gas l
1, purified gas l
2, the first hot oxygen n
0, the second hot oxygen n
1, oxygen o
0, air o, other gas o
1.
Embodiment
Below in conjunction with accompanying drawing, the present invention is further described.
Be a kind of multistage distribution coal gas of high temperature gasifying device as shown in Figure 1 and Figure 2, comprise gasifying reactor 1 and air compartment 100, described air compartment 100 is arranged on the bottom of gasifying reactor 1, and described gasifying reactor 1 is divided into oxygen-enriched combusting section 101, mixing gasifying section 102, gasification intensification section 103 and gasification raising section 104 from the bottom to top; Described oxygen-enriched combusting section 101 makes progress to shrink and transits to mixing gasifying section 102, and mixing gasifying section 102 upwards contraction transitting to gasification intensification section 103, and gasification intensification section 103 makes progress to shrink and transits to gasification raising section 104;
On described air compartment 100, be provided with air compartment gasification agent inlet 2 and air compartment scum pipe 3;
Described oxygen-enriched combusting section 101 lower side are provided with one-level opening for feed 151, one-level returning charge mouth 10 and two one-level gasification agent inlets 111; Described two one-level gasification agent inlets 111 are placed in sustained height, are evenly arranged in all sides of oxygen-enriched combusting section 101, and the pipeline of access one-level gasification agent inlet 111 is the first level pipe;
Described mixing gasifying section 102 lower side are provided with secondary opening for feed 161, secondary returning charge mouth 11 and two secondary gasification agent inlets 121; Described two secondary gasification agent inlets 121 are placed in sustained height, are evenly arranged in all sides of mixing gasifying section 102, and the pipeline of access secondary gasification agent inlet 121 is the second level pipe;
Described gasification intensification section 103 sides, middle part are provided with four three grades of gasification agent inlets 131; Described four three grades of gasification agent inlets 131 are placed in sustained height, are evenly arranged in all sides of gasification intensification section 103, and the pipeline of three grades of gasification agent inlets 131 of access is the 3rd inclined tube;
104 sides, middle part, described gasification raising section are provided with four level Four gasification agent inlets 141; Described four level Four gasification agent inlets 141 are placed in sustained height, are evenly arranged in all sides of gasification raising section 104, and the pipeline of access level Four gasification agent inlet 141 is the 4th inclined tube;
Described gasification raising section 104 top exits connect primary cyclone 4 and secondary cyclone 5 successively; Described primary cyclone 4 bottoms are connected with one-level downtake 6, one-level returning charge valve 8 and downward-sloping one-level returning charge inclined tube 81 in turn, described one-level returning charge inclined tube 81 access one-level returning charge mouths 10; Described secondary cyclone 5 bottoms are connected with secondary downtake 7, secondary returning charge valve 9 and downward-sloping secondary returning charge inclined tube 91 in turn, described secondary returning charge inclined tube 91 access secondary returning charge mouths 11.
The size design of each several part is as follows:
As shown in Figure 3, the diameter of described oxygen-enriched combusting section 101 is D, highly for H, and one-level gasification agent inlet 111 is H/5 apart from the distance of oxygen-enriched combusting section 101 bottoms, and one-level opening for feed 151 and one-level returning charge mouth 10 are H/2 apart from the distance of oxygen-enriched combusting section 101 bottoms;
As shown in Figure 4, the diameter of described mixing gasifying section 102 is D
2=4D/5, be highly H
2=3H, the distance of secondary opening for feed dip distance mixing gasifying section 102 bottoms is H
2/ 5, secondary gasification agent inlet 121 and secondary returning charge mouth 11 are H apart from the distance of mixing gasifying section 102 bottoms
2/ 3;
As shown in Figure 5, the diameter of described gasification intensification section 103 is D
3=3D/5, be highly H
3=4H/3, the distance of three grades of gasification agent inlet 131 distance gasification intensification section 103 bottoms is H
3/ 4;
As shown in Figure 6, the diameter of described gasification raising section 104 is D
4=D/2, be highly H
4=2H, the distance of level Four gasification agent inlet 141 distance gasification 104 bottoms, raising section is H
4/ 6.
Described one-level returning charge inclined tube 81 is α with the angle of horizontal plane
1, α
1it is 35～45 °; Described secondary returning charge inclined tube 91 is α with the angle of horizontal plane
2, α
2it is 35～45 °; The angle of described the 3rd inclined tube and horizontal plane is β
3, β
3it is 15～20 °; The angle of described the 4th inclined tube and horizontal plane is β
4, β
4it is 15～20 °.
Coal gasification reaction carries out in gasifying reactor 1, adopt the middle high temperature of 800-1300 ℃, the vaporized chemical that is added different components by level Four gasification agent inlet, make gasifying reactor 1 in differing temps, atmosphere and reaction process, gasifying reactor 1 is divided into oxygen-enriched combusting section 101, mixing gasifying section 102, gasification intensification section 103, gasification raising section 104 from bottom to top.
By one-level opening for feed 151, to oxygen-enriched combusting section 101, add one-level mixture b
1comprise coal and quartz sand, from air compartment gasification agent inlet 2, two one-level gasification agent inlets 111, pass into vaporized chemical oxygen respectively, wherein, the oxygen that air compartment gasification agent inlet 2 passes into accounts for the required vaporized chemical volume 25% of device, the oxygen that one-level gasification agent inlet 111 passes into accounts for the amount of oxygen that 15%, two one-level gasification agent inlet 111 of the required vaporized chemical volume of device passes into and equates, makes one-level mixture b
1in oxygen-enriched combusting section 101, carry out rapidly oxygen-enriched combusting, produce coke, volatized hydrocarbon, CO
2, H
2the gas-solid mixtures such as O, the reaction that oxygen-enriched combusting section 101 occurs is thermopositive reaction, discharges amount of heat, keeps oxygen-enriched combusting section in 1000-1300 ℃ of higher service temperature, for mixing gasifying section 102 provides gasification reaction required heat.
By secondary opening for feed 161, to mixed firing section 102, add two-stage mixture material b
2, comprise coal dust and Wingdale.One-level mixture b
1account for the 30-50% of whole propellant combinations, two-stage mixture material accounts for the 50-70% of whole propellant combinations.To two secondary gasification agent inlets 121, pass into respectively the secondary vaporized chemical a of equivalent
2, secondary vaporized chemical a
2for oxygen n
0with superheated vapour m
0gas mixture, cumulative volume accounts for 35% of the required vaporized chemical volume of device, wherein, the volume fraction of oxygen is 20-40%, the volume fraction of superheated vapour is 60-80%.Two-stage mixture material b
2the heat being produced by 101 reactions of oxygen-enriched combusting section in mixing gasifying section 121 heats, and pyrolysis and combustion reaction occurs, after oxygen depletion, and carbon residue and steam generation gasification reaction, the hydrogen sulfide that limestone slurry gasification reaction generates removes, and generates sulfurated lime.This stage gasification absorbs amount of heat, the heat and the interior two-stage mixture material of mixing gasifying section 102 b that by 101 burnings of oxygen-enriched combusting section, are discharged
2the heat that the reaction of generating unit divided combustion discharges provides, and the service temperature of mixing gasifying section 102 is 800-1000 ℃.There is the speed of combustion reactions much larger than the speed of mixing gasifying section 102 generating gasification reactions in oxygen-enriched combusting section 101, mixing gasifying section 102 adopts 3 times of height to oxygen-enriched combusting section 101 that gasified reverse should be able to fully be carried out.
The reacted gas-solid mixture of mixing gasifying section 102 enters gasification intensification section 103, because gasification reaction is thermo-negative reaction, the oxygen concentration of mixing gasifying section 102 reduces vertically from bottom to top, gas-solid mixture combustion reactions weakens, mixing gasifying section 102 upper temps are lower, temperature continues to reduce will make gasification reaction incomplete, therefore in gasification heats up section 103, pass into three grades of vaporized chemical a
3the interior generating unit divided combustions that can continue of gasification intensification section 103 are reacted, for gasification reaction provides heat, three grades of vaporized chemical a
3volume accounts for 15% of the required vaporized chemical volume of device.Owing to entering the gas-solid mixture of gasification intensification section 103, there is certain temperature, therefore select air as three grades of vaporized chemical a
3, reduce oxygen depletion amount, and can keep the temperature of gasification raising section 103 interior gasification reactions at 900-1000 ℃.
By level Four gasification agent inlet 141, in gasification raising section 104, pass into level Four vaporized chemical a
4, level Four vaporized chemical a
4volume accounts for 10% of the required vaporized chemical volume of device, level Four vaporized chemical a
4for the gas mixture of superheated vapour and oxygen, wherein the gas fraction of oxygen is 10-30%, and the volume fraction of superheated vapour is 70-90%.In gas-solid mixture in gasification raising section 104, contain the small size particle that 10-20% is difficult to gasification, passing into oxygen carries out combustion reactions and is conducive to improve the temperature in gasification raising section 104, gasification reaction can fully be carried out, level Four gasification agent inlet 141 is inclined tube, the height of riser tube 104 of simultaneously gasifying is higher, the gas-solid mixing mass transfer that is conducive to gasify in raising section 104, thereby improve the residence time of solid in gasification raising section 104, guarantee the carrying out of gasification reaction, the service temperature of gasification raising section is 800-900 ℃.The heating gas d that reaction generates enters primary cyclone 6 and carries out gas solid separation, isolates the one-level carbon residue g that particle diameter is greater than 1mm and is controlled by one-level returning charge valve 8, through one-level returning charge mouth 10, sends into oxygen-enriched combusting section 101, carries out oxygen-enriched combusting.Primary dust removing coal gas e enters secondary cyclone 7 and carries out secondary gas solid separation, and sub-argument goes out the secondary carbon residue h that particle diameter is less than 1mm to be controlled by secondary returning charge valve 9, sends into mixing gasifying section 102 react through secondary returning charge mouth 11.The carbon residue of different-grain diameter enters different conversion zones and reacts, and is conducive to the abundant reaction of carbon residue, keeps the interior temperature of gasifying reactor 1 to be uniformly distributed simultaneously.The deslagging p of reaction is discharged by air compartment scum pipe 3.
Below in conjunction with embodiment, the present invention is made further instructions.
The schema of embodiments of the invention is as shown in Figure 7: gasifying reactor 1 height of bed H is 6m, and oxygen-enriched combusting section 101 diameter D are 200mm.By one-level opening for feed 151, add one-level mixture b1, coal and quartz sand for granularity is 5-10mm, pass into oxygen by air compartment gasification agent inlet 2, and device is cleaned, and makes to be full of in device oxygen.The high-temperature fuel gas that passes into 1000 ℃ by air compartment gasification agent inlet 2 is lighted the one-level mixture b in oxygen-enriched combusting section 101
1after, stop passing into of high-temperature fuel gas.From air compartment gasification agent inlet 2, two one-level gasification agent inlets 111, pass into vaporized chemical oxygen respectively, oxygen volume accounts for 40% of the required vaporized chemical volume of device, wherein, the oxygen that air compartment gasification agent inlet 2 passes into is 25%, the oxygen that one-level gasification agent inlet 111 passes into is 15%, the amount of oxygen that two one-level gasification agent inlets 111 pass into equates, makes one-level mixture b
1in oxygen-enriched combusting section 101, carry out rapidly oxygen-enriched combusting, produce coke, volatized hydrocarbon, CO
2, H
2the gas-solid mixtures such as O, the reaction that oxygen-enriched combusting section 101 occurs is thermopositive reaction, discharges amount of heat, keeps oxygen-enriched combusting section in 1000-1300 ℃ of higher service temperature, for mixing gasifying section 102 provides gasification reaction required heat.
By secondary opening for feed 161, adding granularity is coal and the Wingdale below 5mm, one-level mixture b
1account for 40% of whole propellant combinations, two-stage mixture material accounts for 60% of whole propellant combinations.Pass into secondary vaporized chemical a
2, secondary vaporized chemical a
2volume accounts for 35% of the required vaporized chemical volume of device, secondary vaporized chemical a
2be 35% oxygen and 65% superheated vapour gas mixture.The gas-solid mixture that 101 reactions of oxygen-enriched combusting section generate rises, two-stage mixture material b
2the heat being produced by 101 reactions of oxygen-enriched combusting section in mixing gasifying section 121 heats, the reaction of generation pyrolysis and combustion, after oxygen depletion, carbon residue and steam generation gasification reaction, the hydrogen sulfide that limestone slurry gasification reaction generates removes, generate sulfurated lime, the service temperature of mixing gasifying section 102 is 800-1000 ℃, and the temperature of mixing gasifying section 102 reduces vertically from bottom to top.
Gas-solid mixture enters gasification intensification section 103, in gasification heats up section 103, passes into three grades of vaporized chemical a
3make to gasify and can continue the reaction of generating unit divided combustion in raising section, for gasification reaction provides heat, volume of air accounts for 15% of the required vaporized chemical volume of device.And can keep the temperature of gasification raising section 103 interior gasification reactions at 900-1000 ℃.Three grades of gasification agent inlets 131 are inclined tube, are conducive to the gas-solid mixing mass transfer that gasification heats up in section 103, thereby improve the residence time of solid in gasification heats up section 103, make most of fuel gasification complete.
Gasification intensification section 103 reacted CO, a H
2deng coal gas and be difficult on a small quantity gasification small size particle enter gasification raising section 104.By level Four gasification agent inlet 141, in gasification raising section 104, pass into level Four vaporized chemical a
4, level Four vaporized chemical a
4volume accounts for 10% of the required vaporized chemical volume of device, level Four vaporized chemical a
4for the gas mixture of superheated vapour and oxygen, wherein the gas fraction of oxygen is 20%, and the volume fraction of superheated vapour is 80%.Longer gasification riser tube 104 highly makes gasification reaction abundant, and carbon turnover ratio, more than 92%, generates CO+H in synthetic gas
2content>=90%.The heating gas d that reaction generates enters I and II cyclonic separator and carries out gas solid separation, isolating the one-level carbon residue g that particle diameter is greater than 1mm is controlled by one-level returning charge valve 8, through one-level returning charge mouth 10, send into oxygen-enriched combusting section 101, carry out oxygen-enriched combusting, the secondary carbon residue h that particle diameter is less than 1mm is controlled by secondary returning charge valve 9, through secondary returning charge mouth 11, send into mixing gasifying section 102 and react, the deslagging p of reaction is discharged by air compartment scum pipe 3.The secondary pyrolysis dedusting gas f that reaction generates enters waste heat boiler 12 heating pure water k
0, the middle low temperature coal gas l of generation enters preheater 14 preheated oxygen o
0, obtain low temperature coal gas l
1.The Low Temperature Steam k that waste heat boiler 12 generates enters vapor superheater 13, the superheated vapour m of generation
0, m
1.Air o is by the isolated oxygen o of deaerator 110
0enter preheater 14, generate the first hot oxygen n
0, the second hot oxygen n
1with superheated vapour m
0after mixing with certain proportion, the first mixing tank 120, the second mixing tank 130 form vaporized chemical a respectively
2, a
4.Low temperature coal gas l
1the purified gas l generating after gas cleaning device 15
2entering circulation combined generating system 16 utilizes
The above is only the preferred embodiment of the present invention; be noted that for those skilled in the art; under the premise without departing from the principles of the invention, can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (8)
1. a multistage distribution coal gas of high temperature gasifying device, it is characterized in that: comprise gasifying reactor (1) and air compartment (100), described air compartment (100) is arranged on the bottom of gasifying reactor (1), and described gasifying reactor (1) is divided into oxygen-enriched combusting section (101), mixing gasifying section (102) from the bottom to top, gasification heats up section (103) and gasification raising section (104); Described oxygen-enriched combusting section (101) is upwards shunk and is transitted to mixing gasifying section (102), and mixing gasifying section (102) upwards contraction transits to the section (103) that heats up that gasifies, and gasification intensification section (103) is upwards shunk and transitted to gasification raising section (104);
On described air compartment (100), be provided with air compartment gasification agent inlet (2) and air compartment scum pipe (3);
Described oxygen-enriched combusting section (101) lower side is provided with one-level opening for feed (151), one-level returning charge mouth (10) and two one-level gasification agent inlets (111);
Described mixing gasifying section (102) lower side is provided with secondary opening for feed (161), secondary returning charge mouth (11) and two secondary gasification agent inlets (121);
A side, described gasification intensification section (103) middle part is provided with four three grades gasification agent inlets (131);
Side, middle part, described gasification raising section (104) is provided with four level Four gasification agent inlets (141);
Described gasification raising section (104) top exit connects primary cyclone (4) and secondary cyclone (5) successively; Described primary cyclone (4) bottom is connected with one-level downtake (6), one-level returning charge valve (8) and downward-sloping one-level returning charge inclined tube (81) in turn, described one-level returning charge inclined tube (81) access one-level returning charge mouth (10); Described secondary cyclone (5) bottom is connected with secondary downtake (7), secondary returning charge valve (9) and downward-sloping secondary returning charge inclined tube (91) in turn, described secondary returning charge inclined tube (91) access secondary returning charge mouth (11).
2. multistage distribution coal gas of high temperature gasifying device according to claim 1, is characterized in that:
The diameter of described oxygen-enriched combusting section (101) is D, highly for H, one-level gasification agent inlet (111) is H/5 apart from the distance of oxygen-enriched combusting section (101) bottom, and one-level opening for feed (151) and one-level returning charge mouth (10) are H/2 apart from the distance of oxygen-enriched combusting section (101) bottom;
The diameter of described mixing gasifying section (102) is D
2=4D/5, be highly H
2=3H, secondary opening for feed (161) is H apart from the distance of mixing gasifying section (102) bottom
2/ 5, secondary gasification agent inlet (121) and secondary returning charge mouth (11) are H apart from the distance of mixing gasifying section (102) bottom
2/ 3;
The diameter of described gasification intensification section (103) is D
3=3D/5, be highly H
3=4H/3, a distance for three grades of gasification agent inlets (131) distance gasification intensification sections (103) bottom is H
3/ 4;
The diameter of described gasification raising section (104) is D
4=D/2, be highly H
4=2H, the distance of bottom, level Four gasification agent inlet (141) distance gasification raising section (104) is H
4/ 6.
3. multistage distribution coal gas of high temperature gasifying device according to claim 1, is characterized in that: described one-level returning charge inclined tube (81) is α with the angle of horizontal plane
1, α
1it is 35～45 °; Described secondary returning charge inclined tube (91) is α with the angle of horizontal plane
2, α
2it is 35～45 °.
4. multistage distribution coal gas of high temperature gasifying device according to claim 1, it is characterized in that: described two one-level gasification agent inlets (111) are placed in sustained height, evenly be arranged in all sides of oxygen-enriched combusting section (101), the pipeline of access one-level gasification agent inlet (111) is the first level pipe; Described two secondary gasification agent inlets (121) are placed in sustained height, are evenly arranged in all sides of mixing gasifying section (102), and the pipeline of access secondary gasification agent inlet (121) is the second level pipe; Described four three grades gasification agent inlets (131) are placed in sustained height, are evenly arranged in all sides of gasification intensification section (103), and the pipeline that accesses three grades of gasification agent inlets (131) is the 3rd inclined tube, and the angle of described the 3rd inclined tube and horizontal plane is β
3, β
3it is 15～20 °; Described four level Four gasification agent inlets (141) are placed in sustained height, are evenly arranged in all sides of gasification raising section (104), and the pipeline of access level Four gasification agent inlet (141) is the 4th inclined tube, and the angle of described the 4th inclined tube and horizontal plane is β
4, β
4it is 15～20 °.
5. a multistage distribution high-temperature coal gasification method, is characterized in that: in gasifying reactor (1), maintain the middle high temperature of 800～1300 ℃, comprise the steps:
(1) pass through one-level opening for feed (151) by one-level mixture b
1add oxygen-enriched combusting section (101), by air compartment gasification agent inlet (2), air compartment vaporized chemical a added to air compartment (100) simultaneously, by one-level gasification agent inlet (111) by one-level vaporized chemical a
1add oxygen-enriched combusting section (101); One-level mixture b
1in oxygen-enriched combusting section (101), carry out oxygen-enriched combusting, discharge amount of heat, for the gasification of mixing gasifying section (102) provides heat, the gas-solid mixture that burning generates enters mixing gasifying section (102); Described gas-solid mixture comprises coke, the CO of high temperature
2, H
2o;
(2) pass through secondary opening for feed (161) by two-stage mixture material b
2add mixing gasifying section (102), pass through secondary gasification agent inlet (121) by secondary vaporized chemical a simultaneously
2add mixing gasifying section (102); Two-stage mixture material b
2the heat heating being provided by oxygen-enriched combusting section (101), with oxygen generation combustion reactions, and with water vapour generation part gasification reaction, the burning of oxygen and combustiblematerials makes gasification temperature that mixing gasifying section (102) can continue to keep higher and higher gasification efficiency; Along with the carrying out of gasification reaction, the temperature of reaction of mixing gasifying section (102) constantly declines from bottom to top, and gas-solid mixture continues rising and enters gasification intensification section (103);
(3) pass through three grades of gasification agent inlets (131) by three grades of vaporized chemical a
3add gasification intensification section (103); The coal gas that burns away and generate on a small quantity, for gasification reaction continues to provide heat, and the heat of supplemental equipment heat radiation, improve gas-solid mixture temperature; The gas-solid mixture that reaction generates continues rising and enters gasification raising section (104);
(4) pass through level Four gasification agent inlet (141) by level Four vaporized chemical a
4add gasification raising section (104), make to account for the fully gasification in gasification raising section (104) of the difficult vaporising fuel of fuel 10～20% small particle size;
(5) the heating gas d generating in gasifying reactor (1) enters primary cyclone (4) and carries out gas solid separation, isolates one-level carbon residue g and primary dust removing coal gas e; One-level carbon residue g controls by one-level returning charge valve (8), sends into oxygen-enriched combusting section (101) and carries out oxygen-enriched combusting, for gasification installation provides heat by one-level returning charge mouth (10); Primary dust removing coal gas e enters secondary cyclonic separation (5) device and enters secondary separation, and isolated secondary carbon residue h controls by secondary returning charge valve (9), by secondary returning charge mouth (11), enters mixing gasifying section (102) and propellant combination carries out combustion gasification jointly.
6. multistage distribution high-temperature coal gasification method according to claim 5, is characterized in that: described one-level mixture b
1account for below 30～50% of whole propellant combinations, particle diameter is 5～10mm, two-stage mixture material b
2particle diameter be below 5mm.
7. multistage distribution high-temperature coal gasification method according to claim 5, is characterized in that: described air compartment vaporized chemical a and one-level vaporized chemical a
1be oxygen, wherein air compartment vaporized chemical a accounts for 25% of the required vaporized chemical cumulative volume of device, one-level vaporized chemical a
1account for 15% of the required vaporized chemical cumulative volume of device; Secondary vaporized chemical a
2for the gas mixture of oxygen and superheated vapour, secondary vaporized chemical a
2account for 35% of the required vaporized chemical cumulative volume of device, wherein the volume fraction of oxygen is 20～40%; Three grades of vaporized chemical a
3for air, three grades of vaporized chemical a
3account for 15% of the required vaporized chemical cumulative volume of device; Level Four vaporized chemical a
4for the gas mixture of oxygen and superheated vapour, level Four vaporized chemical a
4account for 10% of the required vaporized chemical cumulative volume of device, wherein the volume fraction of oxygen is 10～30%.
8. multistage distribution high-temperature coal gasification method according to claim 5, it is characterized in that: the service temperature of oxygen-enriched combusting section (101) is 1000-1300 ℃, the service temperature of mixing gasifying section (102) is 800-1000 ℃, the service temperature of gasification intensification section (103) is 900-1000 ℃, and the service temperature of gasification raising section (104) is 800-900 ℃.
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