CN103740409B - 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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- CN103740409B CN103740409B CN201410030040.0A CN201410030040A CN103740409B CN 103740409 B CN103740409 B CN 103740409B CN 201410030040 A CN201410030040 A CN 201410030040A CN 103740409 B CN103740409 B CN 103740409B
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- 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
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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 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, namely with the Lurgi technology fixed bed gasification technology that is representative, with the HTW technology fluidized-bed gasification technology that is representative and the entrained flow bed gasification technology that is representative with Texaco, Shell, multi-products production gasification technology.It is the GE(Texaco of raw material that external industrialized gasification air-flow bed coal-gasification technology mainly contains with coal water slurry) gasification technology, Global E-Gas gasification technology, take dried coal powder as the Shell gasification technology of raw material, Prenflo gasification technology, GSP gasification technology etc.These gasifying process all also 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, Grin-ding energ7 is high, and coal dust can not preheating, and oxygen depletion amount is large.
For traditional gasifying process Problems existing, scientific research institution of various countries have developed some new gasifying process.Wherein, the dense phase transporting bed gasification technique that U.S. KBR proposes, relative to traditional circulating fluidized bed, solids circulation rate and the gas velocity of this technique are fast, riser densities wants high, therefore has higher throughput and efficiency of carbon conversion, heat transfer and rate of mass transfer higher.The bed bioreactor that transports of U.S. KBR obtains remarkable break-throughs, and the coal gasification apparatus of certain IGCC transformation project adopts TRIG Coal Gasification Technology at home, and the first industry becoming the whole world should adopt the project of TRIG Coal Gasification Technology.Similar circulating fluidized bed pilot plant is also all had in HRL company of Australia and BHEL company of India.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 the 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, " 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 achieves greater advance, but still there is 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) be heated in reactor inequality, 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 current domestic industry Coal Gasification Technology mostly is to absorb and introduces, 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 existing large-scale coal gasifying process and existing dense-phase conveying coal gasifying process Problems existing, 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 kind of multistage distribution coal gas of high temperature gasifying device, comprise gasifying reactor and air compartment, 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 is upwards shunk and transitted to gasification intensification section, and gasification intensification section is upwards shunk and transitted to gasification raising section;
Described air compartment is 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;
In the middle part of described gasification intensification section, side is provided with four three grades of gasification agent inlets;
In the middle part of described gasification raising section, side 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, is highly H, and the distance bottom one-level gasification agent inlet distance oxygen-enriched combusting section is H/5, and the distance bottom one-level opening for feed and one-level returning charge mouth distance oxygen-enriched combusting section is H/2; The diameter of described mixing gasifying section is D
2=4D/5, be highly H
2=3H, the distance bottom secondary opening for feed distance mixing gasifying section is H
2/ 5, secondary gasification agent inlet and secondary returning charge mouth are H apart from the distance bottom mixing gasifying section
2/ 3; The diameter of described gasification intensification section is D
3=3D/5, be highly H
3=4H/3, the distance bottom three grades of gasification agent inlet distance gasification intensification sections is H
3/ 4; The diameter of described gasification raising section is D
4=D/2, be highly H
4=2H, the distance bottom level Four gasification agent inlet distance gasification raising section is H
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 access three grades of gasification agent inlets is the 3rd inclined tube, and the angle of described 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 4th inclined tube and horizontal plane is β
4, β
4it is 15 ~ 20 °.
This device is respectively oxygen-enriched combusting section, mixing gasifying section, gasification intensification section and gasification four sections, raising section from the bottom to top 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 the most of heat needed for gasification reaction by fuel oxygen enrichment combustion heat release, and mixing gasifying section, gasification intensification section and gasification raising section carry out burning in various degree, gasification reaction respectively.Multistage distribution carries out distribution according to the reaction characteristics of gasifying reactor different heights, greatly reduce the consumption of oxygen, realize being uniformly distributed of temperature while temperature of reaction higher in maintenance gasifying reactor, realize high gasification efficiency, high carbon conversions, oligosaprobic gasification.
A kind of multistage distribution high-temperature coal gasification method, maintains the middle high temperature of 800 ~ 1300 DEG C, comprises the steps: in gasifying reactor
(1) by one-level opening for feed by primary mixes material b
1add oxygen-enriched combusting section, by air compartment gasification agent inlet, air compartment vaporized chemical a is added air compartment simultaneously, by one-level gasification agent inlet by one-level vaporized chemical a
1add oxygen-enriched combusting section; Primary mixes material b
1carry out oxygen-enriched combusting in oxygen-enriched combusting section, release 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) by 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
2thered is provided by oxygen-enriched combusting section heat heating, with oxygen generation combustion reactions, and with water vapour generating portion gasification reaction, the burning of oxygen and combustiblematerials enables mixing gasifying section continue to keep higher gasification temperature 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) by three grades of gasification agent inlets by three grades of vaporized chemical a
3add gasification intensification section; Burn away a small amount of coal gas generated, 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) by level Four gasification agent inlet by level Four vaporized chemical a
4add gasification raising section, make to account for the difficult vaporising fuel of fuel 10 ~ 20% small particle size and fully gasify, to improve gasification efficiency in gasification raising section;
(5) the heating gas d generated 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 is controlled by one-level returning charge valve, sends into oxygen-enriched combusting section carry 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 is controlled by secondary returning charge valve, enters mixing gasifying section and propellant combination carries out combustion gasification jointly by secondary returning charge mouth.
Preferably, described primary mixes material b
1account for less than 30 ~ 50% of whole propellant combination, 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 vaporized chemical cumulative volume needed for device, one-level vaporized chemical a
1account for 15% of vaporized chemical cumulative volume needed for device; Secondary vaporized chemical a
2for the gas mixture of oxygen and superheated vapour, secondary vaporized chemical a
2account for 35% of vaporized chemical cumulative volume needed for 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 vaporized chemical cumulative volume needed for device; Level Four vaporized chemical a
4for the gas mixture of oxygen and superheated vapour, level Four vaporized chemical a
4account for 10% of vaporized chemical cumulative volume needed for device, wherein the volume fraction of oxygen is 10 ~ 30%.The vaporized chemical tolerance passed 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 DEG C, and the service temperature of mixing gasifying section is 800-1000 DEG C, and the service temperature of gasification intensification section is 900-1000 DEG C, and the service temperature of gasification raising section is 800-900 DEG C.
Beneficial effect: multistage distribution high-temperature coal gasification device and method provided by the invention, to compare prior art, below existing a little: 1, gasifying reactor adopts oxygen-enriched combusting section, mixing gasifying section, gasification intensification section and gasification four sections, raising section design, for the speed of reaction in differential responses stage, adopt different diameters, highly design, add the gas-solid mixing in gasifying reactor, ensure that the residence time in propellant combination gasifying reactor, propellant combination is fully gasified in gasifying reactor, improve carbon turnover ratio, outlet flying dust is few; 2, classification charging is adopted, the fresh fuel of 30 ~ 50% carries 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, maintain the middle hot conditions in gasifying reactor, avoid excessive fresh fuel at oxygen-enriched burner advanced combustion, improve thermo-efficiency and the efficiency of carbon conversion of system; 3, adopt multistage distribution, to make in gasifying reactor each section to have comparatively stable heat supply, gasification reaction temperature is carried out under remaining on the high temperature of 800 ~ 1300 DEG C, substantially increases the gasification efficiency of system, improves the efficiency of carbon conversion of system; 4, adopt multistage distribution, the mode of many vaporized chemicals mouth air inlet adds vaporized chemical, make the uniformity of temperature profile in whole gasifying reactor, pass into the vaporized chemical of different components in different pipe sections, ensure that the gasification demand needed for each section, greatly reduce the consumption of oxygen, reduce gasification cost; 5, level Four vaporized chemical adopts different angles air inlet respectively, one secondary vaporized chemical horizontal access enters and ensure that the residence time of propellant combination in oxygen-enriched combusting section, mixed lifting section and travelling speed, three level Four vaporized chemicals have angle entrance to make being added in stove of vaporized chemical cause certain disturbance, strengthening Mass and heat transfer, extend gas-solid mixture in gasification intensification section and the residence time of gasification raising section, improve 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, first mixing tank 120, 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, primary mixes material 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 returns 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 is upwards shunk and is transitted to mixing gasifying section 102, and mixing gasifying section 102 is upwards shunk and transitted to gasification intensification section 103, and gasification intensification section 103 is upwards shunk and transitted to gasification raising section 104;
Described air compartment 100 is 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 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 is 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;
In the middle part of described gasification intensification section 103, side is provided with four three grades of gasification agent inlets 131; Described four three grades of gasification agent inlets 131 are placed in sustained height, and be evenly arranged in all sides of gasification intensification section 103, the pipeline of access three grades of gasification agent inlets 131 is the 3rd inclined tube;
In the middle part of described gasification raising section 104, side is 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 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, and described one-level returning charge inclined tube 81 accesses 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, and described secondary returning charge inclined tube 91 accesses secondary returning charge mouth 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, is highly H, and one-level gasification agent inlet 111 is H/5 apart from the distance bottom oxygen-enriched combusting section 101, and one-level opening for feed 151 and one-level returning charge mouth 10 are H/2 apart from the distance bottom oxygen-enriched combusting section 101;
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 bottom secondary opening for feed dip distance mixing gasifying section 102 is H
2/ 5, secondary gasification agent inlet 121 and secondary returning charge mouth 11 are H apart from the distance bottom mixing gasifying section 102
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, three grades of gasification agent inlets 131 are H apart from the distance bottom gasification intensification section 103
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, level Four gasification agent inlet 141 is H apart from the distance bottom gasification raising section 104
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 3rd inclined tube and horizontal plane is β
3, β
3it is 15 ~ 20 °; The angle of described 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 DEG C, the vaporized chemical of different components is added by level Four gasification agent inlet, make gasifying reactor 1 be 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.
Primary mixes material b is added to oxygen-enriched combusting section 101 by one-level opening for feed 151
1comprise coal and quartz sand, vaporized chemical oxygen is passed into respectively from air compartment gasification agent inlet 2, two one-level gasification agent inlets 111, wherein, the oxygen that air compartment gasification agent inlet 2 passes into accounts for vaporized chemical volume 25% needed for device, it is equal that the oxygen that one-level gasification agent inlet 111 passes into accounts for 15%, two amount of oxygen that one-level gasification agent inlet 111 passes into of vaporized chemical volume needed for device, makes primary mixes material b
1carry out oxygen-enriched combusting rapidly in oxygen-enriched combusting section 101, 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 to be in the service temperature of 1000-1300 DEG C higher, for mixing gasifying section 102 provides the heat needed for gasification reaction.
Two-stage mixture material b is added to mixed firing section 102 by secondary opening for feed 161
2, comprise coal dust and Wingdale.Primary mixes material b
1account for the 30-50% of whole propellant combination, two-stage mixture material accounts for the 50-70% of whole propellant combination.The secondary vaporized chemical a of equivalent is passed into respectively to two secondary gasification agent inlets 121
2, secondary vaporized chemical a
2for oxygen n
0with superheated vapour m
0gas mixture, cumulative volume accounts for 35% of vaporized chemical volume needed for device, and wherein, the volume fraction of oxygen is 20-40%, and the volume fraction of superheated vapour is 60-80%.Two-stage mixture material b
2heated by the heat that oxygen-enriched combusting section 101 reacts generation in mixing gasifying section 121, pyrolysis and combustion reaction occurs, after oxygen depletion, carbon residue and steam generation gasification reaction, the hydrogen sulfide that limestone slurry gasification reaction generates removes, and generates sulfurated lime.This gasification absorbs amount of heat in stage, to be burnt two-stage mixture material b in the heat of release and mixing gasifying section 102 by oxygen-enriched combusting section 101
2the heat of generating portion combustion reactions release provides, and the service temperature of mixing gasifying section 102 is 800-1000 DEG C.The speed that the speed that combustion reactions occurs oxygen-enriched combusting section 101 is reacted much larger than mixing gasifying section 102 generating gasification, 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 temp is lower, temperature continues to reduce will make gasification reaction incomplete, therefore in gasification intensification section 103, pass into three grades of vaporized chemical a
3make continue generating portion combustion reactions in gasification intensification section 103, for gasification reaction provides heat, three grades of vaporized chemical a
3volume accounts for 15% of vaporized chemical volume needed for device.Because the gas-solid mixture entering gasification intensification section 103 has certain temperature, therefore select air as three grades of vaporized chemical a
3, reduce oxygen depletion amount, and the temperature of gasification reaction in gasification raising section 103 can be kept at 900-1000 DEG C.
In gasification raising section 104, level Four vaporized chemical a is passed into by level Four gasification agent inlet 141
4, level Four vaporized chemical a
4volume accounts for 10% of vaporized chemical volume needed for 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%.Be difficult to the small size particle gasified containing 10-20% in gas-solid mixture in gasification raising section 104, pass into oxygen carry out combustion reactions be conducive to improve gasification raising section 104 in temperature, gasification reaction is fully carried out, level Four gasification agent inlet 141 is inclined tube, the height of gasification riser tube 104 is higher simultaneously, be conducive to the gas-solid mixing mass transfer gasified in raising section 104, thus improve the residence time of solid in gasification raising section 104, ensure the carrying out of gasification reaction, the service temperature of gasification raising section is 800-900 DEG C.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, send into oxygen-enriched combusting section 101, carry out oxygen-enriched combusting through one-level returning charge mouth 10.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 and 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 homogeneous temperature distribution in gasifying reactor 1 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 is 200mm.Add primary mixes material b1 by one-level opening for feed 151, for granularity is coal and the quartz sand of 5-10mm, pass into oxygen by air compartment gasification agent inlet 2, device is cleaned, make to be full of oxygen in device.The high-temperature fuel gas passing into 1000 DEG C by air compartment gasification agent inlet 2 lights the primary mixes material b in oxygen-enriched combusting section 101
1after, stop passing into of high-temperature fuel gas.Vaporized chemical oxygen is passed into respectively from air compartment gasification agent inlet 2, two one-level gasification agent inlets 111, oxygen volume accounts for 40% of vaporized chemical volume needed for 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 is equal, makes primary mixes material b
1carry out oxygen-enriched combusting rapidly in oxygen-enriched combusting section 101, 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 to be in the service temperature of 1000-1300 DEG C higher, for mixing gasifying section 102 provides the heat needed for gasification reaction.
The coal and Wingdale that granularity is below 5mm is added, primary mixes material b by secondary opening for feed 161
1account for 40% of whole propellant combination, two-stage mixture material accounts for 60% of whole propellant combination.Pass into secondary vaporized chemical a
2, secondary vaporized chemical a
2volume accounts for 35% of vaporized chemical volume needed for device, secondary vaporized chemical a
2be the oxygen of 35% and the superheated vapour gas mixture of 65%.Oxygen-enriched combusting section 101 is reacted the gas-solid mixture generated and is risen, two-stage mixture material b
2heated by the heat that oxygen-enriched combusting section 101 reacts generation in mixing gasifying section 121, generation pyrolysis and combustion reacts, 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 DEG C, and the temperature of mixing gasifying section 102 reduces vertically from bottom to top.
Gas-solid mixture enters gasification intensification section 103, in gasification intensification section 103, pass into three grades of vaporized chemical a
3make continue generating portion combustion reactions in gasification raising section, for gasification reaction provides heat, volume of air accounts for 15% of vaporized chemical volume needed for device.And the temperature of gasification reaction in gasification raising section 103 can be kept at 900-1000 DEG C.Three grades of gasification agent inlets 131 are inclined tube, are conducive to the gas-solid mixing mass transfer gasified in intensification section 103, thus improve the residence time of solid in gasification intensification section 103, make most of fuel gasification complete.
Gasification intensification section 103 reacted CO, H
2deng coal gas and be difficult on a small quantity gasify small size particle enter gasification raising section 104.In gasification raising section 104, level Four vaporized chemical a is passed into by level Four gasification agent inlet 141
4, level Four vaporized chemical a
4volume accounts for 10% of vaporized chemical volume needed for 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, isolate the one-level carbon residue g that particle diameter is greater than 1mm to be controlled by one-level returning charge valve 8, oxygen-enriched combusting section 101 is sent into through one-level returning charge mouth 10, 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, send into mixing gasifying section 102 through secondary returning charge mouth 11 to 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 and heats 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
0vaporized chemical a is formed respectively after the first mixing tank 120, second mixing tank 130 is with certain proportion mixing
2, a
4.Low temperature coal gas l
1the purified gas l generated after gas cleaning device 15
2enter circulation combined generating system 16 to utilize
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 (7)
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), gasification intensification section (103) and gasification raising section (104) from the bottom to top; Described oxygen-enriched combusting section (101) is upwards shunk and is transitted to mixing gasifying section (102), mixing gasifying section (102) is upwards shunk and is transitted to gasification intensification section (103), and gasification intensification section (103) is upwards shunk and transitted to gasification raising section (104);
Described air compartment (100) is 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);
Side, described gasification intensification section (103) middle part is provided with four three grades gasification agent inlets (131);
Side, described gasification raising section (104) middle part 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);
The diameter of described oxygen-enriched combusting section (101) is D, is highly H, the distance of one-level gasification agent inlet (111) distance oxygen-enriched combusting section (101) bottom is H/5, and the distance of one-level opening for feed (151) and one-level returning charge mouth (10) distance oxygen-enriched combusting section (101) bottom is H/2;
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 (161) distance mixing gasifying section (102) bottom is H
2/ 5, the distance of secondary gasification agent inlet (121) and secondary returning charge mouth (11) distance mixing gasifying section (102) bottom is H
2/ 3;
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;
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 raising section (104) bottom is H
4/ 6.
2. 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 °.
3. 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, evenly be arranged in all sides of gasification intensification section (103), the pipeline accessing three grades of gasification agent inlets (131) is the 3rd inclined tube, and the angle of described 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, evenly be arranged in all sides of gasification raising section (104), the pipeline of access level Four gasification agent inlet (141) is the 4th inclined tube, and the angle of described 4th inclined tube and horizontal plane is β
4, β
4it is 15 ~ 20 °.
4. adopt the multistage distribution high-temperature coal gasification method based on multistage distribution coal gas of high temperature gasifying device according to claim 1, it is characterized in that: the middle high temperature maintaining 800 ~ 1300 DEG C in gasifying reactor (1), comprises the steps:
(1) by one-level opening for feed (151) by primary mixes material b
1add oxygen-enriched combusting section (101), by air compartment gasification agent inlet (2), air compartment vaporized chemical a is added air compartment (100) simultaneously, by one-level gasification agent inlet (111) by one-level vaporized chemical a
1add oxygen-enriched combusting section (101); Primary mixes material b
1carry out oxygen-enriched combusting in oxygen-enriched combusting section (101), release 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) by 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 provided by oxygen-enriched combusting section (101), with oxygen generation combustion reactions, and with water vapour generating portion gasification reaction, the burning of oxygen and combustiblematerials makes mixing gasifying section (102) can continue to keep higher gasification temperature 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) by three grades of gasification agent inlets (131) by three grades of vaporized chemical a
3add gasification intensification section (103); Burn away a small amount of coal gas generated, 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) by 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 generated 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 is controlled by one-level returning charge valve (8), sends into oxygen-enriched combusting section (101) carry 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, isolated secondary carbon residue h is controlled by secondary returning charge valve (9), enters mixing gasifying section (102) and propellant combination carries out combustion gasification jointly by secondary returning charge mouth (11).
5. multistage distribution high-temperature coal gasification method according to claim 4, is characterized in that: described primary mixes material b
1account for less than 30 ~ 50% of whole propellant combination, particle diameter is 5 ~ 10mm, two-stage mixture material b
2particle diameter be below 5mm.
6. multistage distribution high-temperature coal gasification method according to claim 4, 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 vaporized chemical cumulative volume needed for device, one-level vaporized chemical a
1account for 15% of vaporized chemical cumulative volume needed for device; Secondary vaporized chemical a
2for the gas mixture of oxygen and superheated vapour, secondary vaporized chemical a
2account for 35% of vaporized chemical cumulative volume needed for 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 vaporized chemical cumulative volume needed for device; Level Four vaporized chemical a
4for the gas mixture of oxygen and superheated vapour, level Four vaporized chemical a
4account for 10% of vaporized chemical cumulative volume needed for device, wherein the volume fraction of oxygen is 10 ~ 30%.
7. multistage distribution high-temperature coal gasification method according to claim 4, it is characterized in that: the service temperature of oxygen-enriched combusting section (101) is 1000-1300 DEG C, the service temperature of mixing gasifying section (102) is 800-1000 DEG C, the service temperature of gasification intensification section (103) is 900-1000 DEG C, and the service temperature of gasification raising section (104) is 800-900 DEG C.
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| CN106590757A (en) * | 2015-10-15 | 2017-04-26 | 中国石油化工股份有限公司 | Device and method for segmented-oxygen-blowing catalytic coal gasification |
| CH711812A1 (en) * | 2015-11-26 | 2017-05-31 | Carboforce Sàrl | Burner. |
| CN106675658B (en) * | 2016-12-15 | 2020-05-05 | 华北电力大学 | High-flux circulating fluidized bed low-order coal gasification device and method |
| CN108998098B (en) * | 2018-07-19 | 2020-11-10 | 山东大学 | Coal gasification process and device for liquid slag discharge and high-temperature coke return |
| CN109797012B (en) * | 2018-12-19 | 2021-01-15 | 中国科学院山西煤炭化学研究所 | High-temperature fluidized bed reaction device and method for gasifying carbon-containing material thereof |
| CN110500578B (en) * | 2019-08-21 | 2020-11-06 | 青岛科技大学 | Chemical chain conversion device and method for coupling reaction and separation of solid fuel |
| CN111780095A (en) * | 2020-06-24 | 2020-10-16 | 中国科学院工程热物理研究所 | Combustion system, control method thereof and preheating equipment |
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| CN101942344A (en) * | 2010-09-20 | 2011-01-12 | 中国科学院山西煤炭化学研究所 | Method and device for gasifying multi-segment staged converted fluidized bed |
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