CN103265976B - Method and device for ordinary-pressure oxygen-enriched continuous gasification-gas-steam combined cycle power-generation heat supply - Google Patents
Method and device for ordinary-pressure oxygen-enriched continuous gasification-gas-steam combined cycle power-generation heat supply Download PDFInfo
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention provides a method and a device for ordinary-pressure oxygen-enriched continuous gasification-gas-steam combined cycle power-generation heat supply. The method comprises gas preparation, gas desulfuration, and power-generation heat-supply. The device comprises a gas preparation part, a gas desulfuration part, a gas power-generation part and a gas heat supply part. Primarily-treated gas produced by the gas preparation part enters into the gas desulfuration part, and is subjected to desulphurization to form desulfurated gas. The desulfurated gas passes through the gas power-generation part, is used for power-generation, and is fed into the gas heat supply part for heat recovery and steam supply. The method for ordinary-pressure oxygen-enriched continuous gasification-gas-steam combined cycle power-generation heat supply has a low cost, produces effects fast, has large construction flexibility and small pollution, saves energy and has good environmental benefits. The device for ordinary-pressure oxygen-enriched continuous gasification-gas-steam combined cycle power-generation heat supply has high dedusting efficiency and stability, low environmental pollution, low operation energy consumption, and reduce an investment. Flue gas produced by the device has low dust content and low sulfur content and can be directly discharged into the atmosphere without other treatment.
Description
Technical field
The invention belongs to cogeneration field, particularly relate to a kind of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method and equipment.
Background technology
The power load of current large and medium-sized chemical enterprise device, all larger by thermal load, general enterprises adopts the supporting extraction condensing type generating set of middle high-pressure steam boiler to reach with vapour balance and electricity consumption requirement, namely coal firing boiler is adopted to produce steam, utilize steam turbine to generate electricity, and the steam extracting different pressures grade out meet chemical enterprise device use vapour requirement.But this method Problems existing is unit small scale, efficiency is low, on the other hand because the sulfur dioxide in flue gas of coal firing boiler, content of nitrogen oxide are high, adopt current desulfurization, denitride technology cannot take off again level to lower aq, cause topsoil serious.
Summary of the invention
Based on this, be necessary for prior art exist irrationality, provide a kind of newly, can meet power load and with thermal load, economy normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method and equipment.
Technical scheme of the present invention is as follows:
A kind of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method, described method comprises the steps:
S100: produce coal gas; Fuel, oxygen-rich air and steam are added vapourizing furnace respectively and produces original raw gas, then dedusting is carried out to original raw gas and obtain just gas treatment with cooling process;
S200: coal gas desulfurization: desulfurization process is carried out to first gas treatment and obtains desulfurization coal gas;
S300: power generation and heat supply: obtain high-temperature flue gas after desulfurization coal gas and air are passed into burner combustion, then high-temperature flue gas is passed into after hybrid cooling process the acting of internal combustion turbine startup turbine to generate electricity with drive electrical generators, finish the high-temperature flue gas after merit enter middle pressure waster heat boiler produce in press through hot steam, press through hot steam in described and enter steam turbine for being back to vapourizing furnace after generating, enter low pressure waste heat boiler from middle pressure waster heat boiler high-temperature flue gas out and produce low-pressure steam, saturation steam in described low-pressure steam is used for boiler supply water deaerating, the low-temperature flue gas of discharging from low pressure waste heat boiler directly enters air.
Wherein in an embodiment, described step S100 comprises the steps:
S101: fuel is delivered into vapourizing furnace by fuel delivery system;
S102: configuration oxygen concentration is the oxygen-rich air of 70% to 99.5%, and make oxygen-rich air enter the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank respectively, the oxygen-rich air entering the first oxygen enrichment mixing tank enters vapourizing furnace by first jet, and the secondary oxygen-rich air entering the second oxygen enrichment mixing tank enters vapourizing furnace by second nozzle;
S103: the opposing steam flow from steam turbine enters vapourizing furnace;
S104: fuel, oxygen-rich air and steam carry out burning and forms original raw gas in vapourizing furnace; Then original raw gas is drawn by top of gasification furnace and enter tornado dust collector; Now the temperature of original raw gas is 950 ± 20 DEG C;
S105: isolate the flying dust in original raw gas by tornado dust collector, obtains the first raw gas through first time dust removal process, and flying dust is returned vapourizing furnace and carry out second gasification further; Wherein the temperature of the first raw gas is 850 ± 20 DEG C, and dustiness is 180 to 210g/m
3;
S106: carry out waste heat recovery processing to the first raw gas, obtains the second raw gas, presses through hot steam in obtaining simultaneously; Now the temperature of the second raw gas is 150 ± 10 DEG C, and dustiness is 12 to 18g/m
3;
S107: carry out second time dust removal process to the second raw gas and obtain just gas treatment, the temperature of first gas treatment is 150 DEG C, and dustiness is 75mg/m
3.
Wherein in an embodiment, described step S200 comprises the steps:
S201: first gas treatment is hydrolyzed process, the organic sulfide in coal gas is converted into hydrogen sulfide, obtains the 3rd coal gas;
S202: obtain the 4th coal gas after carrying out dedusting cooling and gas-water separation process to the 3rd coal gas, the temperature of the 4th coal gas is 35 ± 5 DEG C, and dustiness is 8 to 12mg/m
3, hydrogen sulfide content is 1400 to 1600mg/Nm
3;
S203: carry out wet desulphurization process to the 4th coal gas and obtain once desulfurization coal gas, the equipment that wet desulphurization adopts is thionizer, and the hydrogen sulfide content of once desulfurization coal gas is 40 to 60mg/Nm
3, temperature is 40 ± 5 DEG C;
S204: adopt sweetening agent and sorbent material to carry out dry desulfurization process to once desulfurization coal gas and obtain secondary desulfuration coal gas, the hydrogen sulfide content of secondary desulfuration coal gas is less than 1mg/Nm
3.
Wherein in an embodiment, described step S203 comprises the steps:
S2031: carry out dust removal process to the 4th coal gas and obtain the 5th coal gas, the dustiness of described 5th coal gas is lower than 1mg/m
3;
S2032: boosting process is carried out to the 5th coal gas and obtains the 6th coal gas, the pressure of described 6th coal gas is about 10KPa, and temperature is 50 ± 5 DEG C;
S2033: carry out cooling process to the 6th coal gas, obtains the 7th coal gas, and the temperature of described 7th coal gas is 35 DEG C;
S2034: adopt thionizer to carry out wet desulphurization process to the 7th coal gas and obtain the 8th coal gas, thionizer absorbs the hydrogen sulfide in the 7th coal gas.
S2035: carry out purifying treatment to the 8th coal gas, removes fine dust, elaioleucite, the sulphur foam in coal gas, obtains once desulfurization coal gas.
Wherein in an embodiment, described step S300 comprises the steps:
S301: secondary desulfuration coal gas is carried out processed compressed and obtain the 9th coal gas, and the 9th coal gas is passed into burner; The pressure of the 9th coal gas is 1.5 to 2.4MPa, and temperature is 350 ± 10 DEG C;
S302: obtain pressurized air after dust removal process and processed compressed are carried out to air, and Partial shrinkage air is passed into burner; Compressed-air actuated dustiness is lower than 1mg/m
3, pressure is 1.5 to 2.4MPa;
S303: the nine coal gas and pressurized air burn generation high-temperature flue gas in the burner; The temperature of high-temperature flue gas is 1600 ± 50 DEG C;
S304: high-temperature flue gas and rest part pressurized air are mixed to get the second flue gas, the temperature of the second flue gas is 1100 ± 50 DEG C, and pressure is 1.4 to 2.3MPa;
S305: make the second flue gas enter internal combustion turbine and start turbine acting and drive electrical generators generating; The temperature finishing the 3rd flue gas from internal combustion turbine discharge after merit is 500 to 600 DEG C, and pressure is 5000 to 6000Pa;
S306: the 3rd flue gas is entered during the first waste heat boiler obtains and press through hot steam, presses through hot steam and enters steam turbine and generate electricity in described, from steam turbine opposing steam flow out to vapourizing furnace;
S307: enter the second waste heat boiler from the first waste heat boiler the 4th flue gas out and obtain low-pressure steam, the saturated low-pressure steam supply deoxygenator in described low-pressure steam is used for boiler supply water deaerating;
S308: from the second waste heat boiler out the 5th flue gas discharge.
The present invention also provides a kind of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment, and described equipment comprises coal gas and produces part, coal gas desulfurization part, gas to generate electricity part and gas heating part:
Described coal gas is produced and is carried out desulfurization after the obtained first gas treatment of part enters coal gas desulfurization part and obtain desulfurization coal gas, and desulfurization coal gas enters and enters gas heating part after gas to generate electricity part generates electricity and reclaim heat further and provide steam.
Wherein in an embodiment, described coal gas is produced part and is comprised gazogene, cleaning apparatus and heat reclamation device;
Described gazogene comprises fuel delivery system, oxygen enriched air system, vapourizing furnace and dreg removing system; Described fuel delivery system is communicated with described vapourizing furnace by the fuel inlet be arranged on described vapourizing furnace, and described oxygen enriched air system is communicated with described vapourizing furnace by the nozzle be arranged on vapourizing furnace, and described dreg removing system is arranged on the bottom of described vapourizing furnace; Fuel, oxygen-rich air and the steam from gas heating part produce original raw gas in vapourizing furnace;
Described cleaning apparatus comprises tornado dust collector and the first cleaning apparatus; Described tornado dust collector are communicated with described vapourizing furnace by return line;
Described heat reclamation device comprises the first heat reclamation device;
Described original raw gas obtains the first raw gas after carrying out dedusting by tornado dust collector, the first raw gas obtain after entering the first heat reclamation device the second raw gas and in press through hot steam, the second raw gas obtains just gas treatment after entering the first cleaning apparatus.
Wherein in an embodiment, described oxygen enriched air system comprises the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank, the nozzle of described vapourizing furnace comprises first jet and second nozzle, described first oxygen enrichment mixing tank is connected with the first jet of described vapourizing furnace, described second oxygen enrichment mixing tank is connected with the second nozzle of described vapourizing furnace, and described first jet is arranged on the centrum portion of described vapourizing furnace; Described second nozzle is arranged on the top of described vapourizing furnace.
Wherein in an embodiment, described first jet is arranged on the below of described fuel inlet, the distance of described first jet and described fuel inlet is 1.0 to 2.0 meters, and the angle between the central axis of described first jet and the central axis of described vapourizing furnace is 10 to 25 to spend.
Wherein in an embodiment, the central axis of described second nozzle and the central axis upright of described vapourizing furnace.
Wherein in an embodiment, described coal gas desulfurization part comprises hydrolysis device, the first refrigerating unit, the second cleaning apparatus, increasing apparatus, the second refrigerating unit, thionizer, refining plant, dry desulfurization device and circulating water device;
Hydrolysis device, the first refrigerating unit, the second cleaning apparatus, increasing apparatus, the second refrigerating unit, thionizer, refining plant, dry desulfurization device connect successively; Wherein be provided with sweetening agent and sorbent material in dry desulfurization device;
Described just gas treatment obtains the 3rd coal gas by the hydrolysis device process that is hydrolyzed, described 3rd coal gas carries out dedusting cooling by the first refrigerating unit and gas-water separation process obtains the 4th coal gas, described 4th coal gas enters after the second cleaning apparatus carries out dust removal process and obtains the 5th coal gas, the 6th coal gas is obtained after described 5th coal gas enters increasing apparatus, the 7th coal gas is obtained after described 6th coal gas enters the second refrigerating unit, the 8th coal gas is obtained after described 7th coal gas enters thionizer, described 8th coal gas enters after refining plant purifies and obtains once desulfurization coal gas, secondary desulfuration coal gas is obtained after described once desulfurization coal gas enters dry desulfurization device,
Described circulating water device is connected with described first refrigerating unit and the second refrigerating unit respectively, and described recirculated water is back to circulating water device after circulating water device enters the first refrigerating unit and the second refrigerating unit respectively.
Wherein in an embodiment, described gas to generate electricity part comprises gas compressor, air filter, air compressor, burner and internal combustion turbine;
Described air filter is communicated with described air compressor, described gas compressor is all communicated with described burner with described air compressor, the exhanst gas outlet of described burner is communicated with described internal combustion turbine by high temp. flue, and described air compressor is communicated with described high temp. flue;
Secondary desulfuration coal gas obtains the 9th coal gas after gas compressor, enter burner, air carries out entering after dust removal process after air compressor carries out processed compressed through air filter and obtains pressurized air, 9th coal gas and Partial shrinkage air pass into burner and burning produces high-temperature flue gas in the burner, described high-temperature flue gas obtains the second flue gas in high temp. flue with after Partial shrinkage air mixed, and described second flue gas enters internal combustion turbine and starts turbine acting and drive electrical generators generating.
Wherein in an embodiment, described gas heating part comprises the first waste heat boiler, the second waste heat boiler, steam turbine and exhaust system;
Wherein the first waste heat boiler is communicated with steam turbine, and the second waste heat boiler is communicated with deoxygenator, and the first waste heat boiler is communicated with the second waste heat boiler, and the second waste heat boiler is communicated with exhaust system; Described steam turbine is connected with described vapourizing furnace;
Being discharged by exhaust system after the 3rd flue gas of internal combustion turbine discharge enters the first waste heat boiler and the second waste heat boiler successively after generating, wherein the first waste heat boiler presses through hot steam in producing, second waste heat boiler produces low-pressure steam, press through hot steam in producing and enter steam turbine, the low-pressure saturated steam produced enters deoxygenator.
Wherein in an embodiment, described first heat reclamation device is also communicated with described steam turbine.
Wherein in an embodiment, described coal gas desulfurization part also comprises doctor solution compounding system, and described doctor solution compounding system is communicated with described thionizer;
Described doctor solution compounding system comprises doctor solution device for formulating, desulfurization regeneration device and sulfur recovery unit, wherein said doctor solution device for formulating comprises solution preparation groove, doctor solution preparation pump, lean solution groove and desulfur pump, and described desulfurization regeneration device comprises regenerative pump, regeneration tank and injector; Described sulfur recovery unit comprises sulphur foam chute, sulphur foam pump, filter and sulfur melting kettle; Described solution preparation pump is arranged on outside solution preparation groove, and the doctor solution in described solution preparation groove enters described thionizer by desulfur pump; The top of described regeneration tank is communicated with sulphur foam chute with described lean solution groove; Described sulfur recovery unit is communicated with described lean solution groove;
According to the formula of doctor solution, the raw material of doctor solution is added doctor solution preparation pump and make suitable doctor solution, suitable doctor solution is made by doctor solution preparation pump, by desulfur pump, doctor solution is delivered to top and the middle part of thionizer after doctor solution fills into lean solution groove, doctor solution sprays from top to bottom, contact with back flow of gas, the hydrogen sulfide absorbed in gas obtains doctor solution rich solution, then described doctor solution rich solution enters regenerative pump after being gone out by the tower bottom flow of thionizer, the liquid inlet of the injector be arranged on above regeneration tank delivered to by doctor solution rich solution by described regenerative pump, enter bottom regeneration tank together with after described doctor solution rich solution is sprayed by injector with the air of self-priming, oxygen in injector and regeneration tank in air and doctor solution react, the sulphur foam generated by the top overflow of regeneration tank to sulphur foam chute, doctor solution lean solution after regeneration enters lean solution groove and recycles, described sulphur foam is pressurizeed by sulphur foam pump, filters to isolate sulphur foam and clear liquid through filter, and sulphur foam enters sulfur melting kettle and obtains Sulphur element slab 99.5, and described clear liquid flows into lean solution groove.
The invention has the beneficial effects as follows:
(1) normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method cost of the present invention is low, instant effect, builds handiness comparatively greatly, pollutes little, and energy-conserving and environment-protective;
(2) dust removal process in normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method of the present invention has efficient and stable purification function, and the dust content of gas after dust removal process is lower than 1mg/m
3; And fundamentally get rid of the huge facility of gas mud and sewage disposal and the pollution to environment;
(3) dust removal installation in normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment of the present invention saves land 30 ~ 60%, and water saving 70 ~ 93%, reduces investment outlay 25 ~ 45%, reduces operation energy consumption 55 ~ 75%;
(4) the gas to generate electricity efficiency of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method of the present invention is high, reaches as high as more than 58% at present.
(5) dust content that normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment obtains of the present invention is low, and sulphur content is low, does not need directly to enter air through other process.
Accompanying drawing explanation
Below in conjunction with concrete drawings and the specific embodiments, the present invention is further elaborated.
Fig. 1 is the schematic diagram that the coal gas of normal pressure of the present invention oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment produces part.
Fig. 2 is the schematic diagram of the coal gas desulfurization part of normal pressure of the present invention oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment.
Fig. 3 is the gas to generate electricity part of normal pressure of the present invention oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment and the schematic diagram of gas heating part.
Embodiment
In order to make the object of normal pressure of the present invention oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method and equipment, technical scheme and advantage clearly understand, below in conjunction with the drawings and specific embodiments, the present invention is further elaborated.
The invention provides a kind of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method, described method comprises the steps:
S100: produce coal gas; Fuel, oxygen-rich air and steam are added vapourizing furnace respectively and produces original raw gas, then dedusting is carried out to raw gas and obtain just gas treatment with cooling process; Wherein the ratio of weight and number of fuel, oxygen-rich air and steam is 100:89:54; This step adopts coal gas to produce part and obtains just gas treatment;
S200: coal gas desulfurization: desulfurization process is carried out to first gas treatment and obtains desulfurization coal gas; This step adopts coal gas desulfurization part to carry out desulfurization process to first gas treatment and obtains desulfurization coal gas;
S300: power generation and heat supply: obtain high-temperature flue gas after desulfurization coal gas and air are passed into burner combustion, then high-temperature flue gas is passed into after hybrid cooling process the acting of internal combustion turbine startup turbine to generate electricity with drive electrical generators, finish the high-temperature flue gas after merit enter middle pressure waster heat boiler produce in press through hot steam, press through hot steam in described and enter steam turbine for being back to vapourizing furnace after generating, enter low pressure waste heat boiler from middle pressure waster heat boiler high-temperature flue gas out and produce low-pressure saturated steam, described low-pressure saturated steam enters deoxygenator for boiler supply water deaerating, the low-temperature flue gas of discharging from low pressure waste heat boiler directly enters air.This step have employed gas to generate electricity part and generates electricity, and carries out waste heat recovery simultaneously make heat obtain Appropriate application to the high-temperature flue gas after generating (finishing merit) by gas heating part.
First the present embodiment is produced part producing by coal gas and is gone out just gas treatment, then utilize coal gas desulfurization part to carry out desulfurization process to first gas treatment and obtain desulfurization coal gas, afterwards desulfurized coal pneumatic transmission is entered gas to generate electricity part to carry out generating electricity to meet power load, the coal gas finishing merit is sent into gas heating part in producing, presses through hot steam and low-pressure steam, press through hot steam wherein and enter steam turbine, need the steam can extracting different grades out to meet industrial vapour requirement according to industry, low-pressure steam can meet the deoxygenation vapour requirement of boiler feed water.
Carry out dust removal process and desulfurization process to raw gas in the present embodiment, reduce the dustiness in raw gas and sulphur content, the waste gas that the present invention is discharged, without the need to namely meeting waste gas emission standard through off gas treatment, has saved facility investment.
Preferably, as a kind of embodiment, described step S100 comprises the steps:
S101: fuel is delivered into vapourizing furnace 113 by fuel delivery system 111; In the present embodiment, described fuel is coal; Fuel delivery system in the present embodiment comprises coal bunker and fuel area density machine, needs to add N when general coal is stored in coal bunker
2(P=0.015Pa) protect, described fuel area density machine is arranged on the bottom of coal bunker and coal is sent into vapourizing furnace 113 from the fuel inlet being arranged on vapourizing furnace side by described fuel area density machine; Described fuel area density machine can be multiple according to design flow;
S102: configuration oxygen-containing gas volume concentrations is the oxygen-rich air of 70% to 99.5%, the oxygen-rich air prepared is made to enter the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank respectively, the oxygen-rich air entering the first oxygen enrichment mixing tank enters vapourizing furnace 113 by first jet, and the secondary oxygen-rich air entering the second oxygen enrichment mixing tank enters vapourizing furnace 113 by second nozzle; Wherein oxygen-rich air is in oxygen enrichment mixing tank exterior arrangement, oxygen-rich air configuration by purity oxygen and air by ratio of weight and the number of copies 65 ~ 57:0 ~ 32 mixture obtain;
S103: the opposing steam flow from steam turbine enters vapourizing furnace 113;
S104: fuel, oxygen-rich air and steam carry out burning and forms raw gas in vapourizing furnace 113, then raw gas is entered tornado dust collector 121 by vapourizing furnace 113 Base top contact, now the temperature of raw gas is 950 ± 20 DEG C, is approximately 950 DEG C, close phase section is formed at the bottom of the larger coarse particles of major part in vapourizing furnace 113 of the coal in the present embodiment in vapourizing furnace 113, raw material becomes boiling state, gas in this region, react Gu violent mass transfer and heat transfer and combustion oxidation occur two-phase, temperature of reaction is 950 to 1000 DEG C, now enter the macrobead small-particle that cracking produces because being heated in vapourizing furnace, then enter the fine powder of the coal in vapourizing furnace 113 and small-particle to be carried by reactant gases and leave close phase section, in the formation freeboard of fluidized bed, top of vapourizing furnace 113, and react further in freeboard of fluidized bed and secondary oxygen-rich air, secondary oxygen-rich air in the present embodiment has two effects: one is stop ascending gas, reduce the flow velocity of ascending gas, increase the residence time of reactant gases so that the entrainment in further reaction and separation processes gas, two is promote reaction, and make the carbon in the fine particle carried secretly in gas continue gasification reaction, the methane produce close phase section and higher carbon compounds burn and cracking further, the raw gas that raw material in this step is formed is drawn by top of gasification furnace and is carried out subsequent disposal,
S105: isolated the flying dust in raw gas by tornado dust collector 121, obtains the first raw gas through first time dust removal process, and flying dust is returned vapourizing furnace 113 and carry out second gasification further; Wherein the temperature of the first raw gas is 850 ± 20 DEG C, is generally about 850 DEG C, and dustiness is 180 to 210g/m
3, be generally about 200g/m
3; In the present embodiment, flying dust can return vapourizing furnace 113 by return line;
S106: adopt the first heat reclamation device 131 to carry out (superheat section, evaporator section, economizer) waste heat recovery processing to the first raw gas, obtain the second raw gas, press through hot steam in obtaining simultaneously; Now the temperature of the second raw gas is 150 ± 10 DEG C, is generally about 150 DEG C, and dustiness is 12 to 18g/m
3, be generally about 15g/m3, particle diameter is less than 50 μm; The pressure pressing through hot steam in this step is approximately 3.82MPa to 6.5MPa, and temperature is about 450 DEG C to 520 DEG C; Press through hot steam in this step and enter steam turbine;
S107: adopt the first cleaning apparatus 122 to carry out second time dust removal process to the second raw gas and obtain just gas treatment, the dustiness of first gas treatment is 75mg/m
3.The second cleaning apparatus in the present embodiment can be sack cleaner or electric precipitator.
Preferably, as a kind of embodiment, described step S200 comprises the steps:
S201: adopt hydrolysis device 211 to be hydrolyzed process to first gas treatment, the organic sulfide in coal gas is converted into hydrogen sulfide, obtains the 3rd coal gas; Hydrolysis device in the present embodiment is hydrolytic tank, and the main purpose of this step makes the organic sulfide in first gas treatment be converted into hydrogen sulfide so that remove;
S202: obtain the 4th coal gas after adopting the first refrigerating unit 212 to carry out dedusting cooling and gas-water separation process to the 3rd coal gas, the temperature of the 4th coal gas is 35 ± 5 DEG C, and general temperature is about 35 DEG C, and dustiness is 8 to 12mg/m
3, dustiness is generally about 10mg/m
3, hydrogen sulfide content is 1400 to 1600mg/Nm
3, usual hydrogen sulfide content is about 1500mg/Nm
3; The first refrigerating unit in the present embodiment is filler cooling washing tower;
S203: wet desulphurization process is carried out to the 4th coal gas and obtains once desulfurization coal gas; The equipment that wet desulphurization adopts is thionizer, and the hydrogen sulfide content of once desulfurization coal gas is 40 to 60mg/Nm
3, temperature is 40 ± 5 DEG C, and typical temperature is 40 DEG C; Doctor solution wherein in thionizer is from doctor solution compounding system and desulfurization regeneration system; The 5th coal gas in this step enters the bottom of thionizer, the packing layer of coal gas from bottom to top by thionizer in thionizer, and with the doctor solution counter current contact of the top spray of thionizer, the hydrogen sulfide now in gas is desulfurized liquid and absorbs;
S204: adopt sweetening agent and sorbent material to carry out dry desulfurization process to cooling once desulfurization coal gas in dry desulfurization device 218 and obtain secondary desulfuration coal gas, the hydrogen sulfide content of secondary desulfuration coal gas is less than 1mg/Nm
3.In the present embodiment, described sweetening agent is adsorptivity.
In the present embodiment, the mode that dust removal process adopts dry method dust process and wet dedusting process to combine is carried out to coal gas, first the most of flying dust in dry method dust process removal coal gas is adopted, then wet dedusting is adopted to carry out dedusting further and lower the temperature simultaneously, not only solve the problem of the serious and water resource waste of the simple water pollutions adopting water washing dedust to cause like this, and dust removing effects is good, can also lower the temperature to coal gas simultaneously.
Further, the mode that desulfurization in the present embodiment adopts wet desulphurization and dry desulfurization to combine, first be hydrogen sulfide by the sulfide in coal gas by hydrolysis, then the hydrogen sulfide in wet desulphurization absorption coal gas is adopted, finally adopt sweetening agent and sorbent material etc. to adsorb again and reduce sulphur content further, sulfur method in the present embodiment acts synergistically together, and the sulphur content in coal gas is reduced.
Preferably, as a kind of embodiment, the step S203 in the present embodiment also comprises the steps:
S2031: adopt the second cleaning apparatus 213 to carry out dust removal process to the 4th coal gas and obtain the 5th coal gas, the dustiness of described 5th coal gas is lower than 1mg/m
3; In the present embodiment, the 3rd cleaning apparatus is preferably wet electrical dust precipitator;
S2032: adopt increasing apparatus 214 to carry out boosting process to the 5th coal gas and obtain the 6th coal gas, the pressure of described 6th coal gas is about 10kPa, and temperature is 50 ± 5 DEG C, and general temperature is about 50 DEG C; In the present embodiment, described increasing apparatus is gas fan;
S2033: adopt the second refrigerating unit 215 to carry out cooling process to the 6th coal gas and obtain the 7th coal gas; The second refrigerating unit in the present embodiment is cooling tower; In this step, the 6th coal gas enters the bottom of cooling tower, spray with the tower top of cooling tower and under water coolant counter current contact cool, then obtain the 7th coal gas by the top of cooling tower;
S2034: adopt thionizer 216 to carry out wet desulphurization process to the 7th coal gas and obtain the 8th coal gas, wherein thionizer absorbs the hydrogen sulfide in the 7th coal gas.
S2035: adopt refining plant 217 to carry out purifying treatment to the 8th coal gas, the fine dusts in removal the 8th coal gas, greasy dirt, sulphur foam obtain once desulfurization coal gas, and the temperature of described once desulfurization coal gas is 35 DEG C; Refining plant in the present embodiment is high pressure static electricity decoking tower;
In order to make wet desulphurization respond well, the present embodiment had carried out the process such as a series of boosting, dedusting, cooling before coal gas enters thionizer.Adopt sorbent material and sweetening agent to carry out dry desulfurization process afterwards, further can absorb the sulfide in coal gas on the one hand.The moisture etc. in coal gas can be absorbed on the other hand, make coal gas be applicable to follow-up generating acting.
The water coolant of the first refrigerating unit 212, second refrigerating unit 215 in the present embodiment all can recycle, and the doctor solution in thionizer in the present embodiment reuses after can carrying out manipulation of regeneration, can save process cost like this, saving resource.
Preferably, as a kind of embodiment, described step S300 comprises the steps:
S301: adopt gas compressor 311 pairs of secondary desulfuration coal gas to carry out processed compressed and obtain the 9th coal gas, and the 9th coal gas is passed into burner 314; The pressure of the 9th coal gas is 1.5 to 2.4MPa, and temperature is 350 ± 10 DEG C, is preferably 350 DEG C; In the present embodiment, the sulphur content≤1mg/m of the secondary desulfuration coal gas after desulfurization process
3, dustiness≤1mg/m
3.
S302: adopt air filter 312 pairs of air to carry out dust removal process, obtains pressurized air after adopting air compressor 313 pairs of air to carry out processed compressed afterwards, and Partial shrinkage air is passed into burner 314; Compressed-air actuated dustiness is lower than 1mg/m
3, pressure is 1.5 to 2.4MPa, and temperature is 300 DEG C;
S303: the nine coal gas and pressurized air burn and produce high-temperature flue gas in burner 314; The temperature of high-temperature flue gas is 1600 ± 50 DEG C, and typical temperature is about 1600 DEG C;
S304: the pressurized air of high-temperature flue gas and rest part is mixed to get the second flue gas, the temperature of the second flue gas is 1100 ± 50 DEG C, is generally 1100 DEG C, and pressure is 1.4 to 2.3MPa;
S305: make the second flue gas enter internal combustion turbine 316 and start turbine acting and drive electrical generators generating; The temperature finishing the 3rd flue gas from internal combustion turbine discharge after merit is 500 DEG C to 600 DEG C, and pressure is 5000Pa to 6000Pa;
S306: the 3rd flue gas is entered during the first waste heat boiler 411 obtains and press through hot steam, press through in described during hot steam and step S106 produce and press through hot steam mixing and enter steam turbine 413 in the lump and generate electricity, and from steam turbine opposing steam flow out to vapourizing furnace for generation of original raw gas; Steam turbine in this step may be used for extracting steam out with satisfied vapour load according to by vapour grade; Pressing through hot steam pressure in obtaining in this step is 3.82MPa to 6.5MPa, and temperature is 450 DEG C to 520 DEG C; Be 0.5MPa from the steam turbine pressure being back to the steam of vapourizing furnace out in this step, temperature is 210 DEG C; In the present embodiment, generally the oiler feed of the first waste heat boiler can be heated to 230 DEG C;
S307: enter the second waste heat boiler 412 from the first waste heat boiler 411 the 4th flue gas out and obtain low-pressure steam, the low-pressure saturated steam in described low-pressure steam enters deoxygenator for boiler water deaeration; The pressure of the low-pressure saturated steam produced in this step is 0.2MPa, and temperature is temperature of saturation 132 DEG C;
S308: discharged by exhaust system 414 from the second waste heat boiler 412 the 5th flue gas out; In this step, the temperature of the 5th flue gas is about 130 DEG C.
Normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method produces coal gas, coal gas is carried out in advance to carry out waste heat recovery after then effective dedusting and desulfurization process make gas to generate electricity do work makes it produce steam with satisfied vapour load, each technique in the present invention organically combines, synergy, can meet industrial power load and the requirement with vapour load simultaneously; Method of the present invention is all recycled the waste produced in each processing step on the other hand, has good economic benefit and social benefit; Moreover method of the present invention has carried out dust removal process and desulfurization process in advance to coal gas in use, the coal gas obtained so better can carry out generating acting on the one hand, follow-up needs carries out the waste gas emission standard that off gas treatment can reach country on the other hand, save off gas treatment expense, simultaneously can to waste rational and efficient use wherein, energy-conserving and environment-protective.
In order to realize aforesaid method, see Fig. 1 to Fig. 3, the present invention also provides a kind of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment adapted with aforesaid method, and described equipment comprises coal gas and produces part, coal gas desulfurization part, gas to generate electricity part and gas heating part; Wherein coal gas is produced and is partly carried out dust removal process for the preparation of coal gas and to coal gas, coal gas desulfurization part is used for carrying out desulfurization process to reduce the sulphur content in coal gas to coal gas, gas to generate electricity part carries out generating acting to meet industrial power load for using coal gas, and gas heating part is for using the generation of the high-temperature flue gas after generating steam with satisfied vapour load and carrying out waste heat recovery to high-temperature flue gas; Its working process is that described coal gas is produced and carried out desulfurization after the obtained first gas treatment of part enters coal gas desulfurization part and obtain desulfurization coal gas, and desulfurization coal gas enters and enters gas heating part after gas to generate electricity part generates electricity and reclaim heat further and provide steam.
Preferably, as a kind of embodiment, described coal gas is produced part and is comprised gazogene 11, cleaning apparatus and heat reclamation device;
Described gazogene comprises fuel delivery system 111, oxygen enriched air system 112, vapourizing furnace 113 and dreg removing system 114; Described fuel delivery system 111 is communicated with described vapourizing furnace 113 by the fuel inlet be arranged on described vapourizing furnace 113, described oxygen enriched air system 112 is communicated with described vapourizing furnace 113 by the nozzle be arranged on vapourizing furnace 113, and described dreg removing system 114 is arranged on the bottom of described vapourizing furnace 113; Fuel, oxygen-rich air and the steam from gas heating part produce original raw gas in vapourizing furnace 113, and the slag that vapourizing furnace 113 reacts rear generation is discharged by dreg removing system 114;
Described cleaning apparatus comprises tornado dust collector 121 and the first cleaning apparatus 122; Described tornado dust collector 121 are communicated with described vapourizing furnace 113 by return line; Described heat reclamation device is the first heat reclamation device 131;
Described original raw gas obtains the first raw gas after carrying out dedusting by tornado dust collector 121, first raw gas obtain after entering the first heat reclamation device 131 second raw gas and in press through hot steam, described second raw gas obtains just gas treatment after entering the first cleaning apparatus 122.
Wherein, preferably, the fuel delivery system 111 in the present embodiment comprises coal bunker and fuel area density machine, needs to add N when general coal is stored in coal bunker
2(P=0.015Pa) protect, described fuel area density machine is arranged on the bottom of coal bunker and coal is sent into vapourizing furnace from the fuel inlet being arranged on vapourizing furnace side by described fuel area density machine; Described fuel area density machine can be multiple according to design flow.
Wherein, preferably, the first heat reclamation device 131 can be waste heat boiler (superheat section, evaporator section, economizer), and the first cleaning apparatus 122 can be sack cleaner or electric precipitator.Vapourizing furnace can be Ender furnace.
Wherein, preferably, the dreg removing system 114 in the present embodiment comprises and is arranged on the ash ejector bottom vapourizing furnace and the ash bucket for storing slag, and described slag needs to adopt steam to cool after entering ash bucket, wherein ash ejector can be spiral ash discharger, and quantity can be multiple.Slag discharge process in the present embodiment continues to carry out, and the slag entering ash bucket regularly pulls away discharge.
Preferably, as a kind of embodiment, oxygen enriched air system in the present embodiment comprises the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank, the nozzle of described vapourizing furnace comprises first jet and second nozzle, described first oxygen enrichment mixing tank is connected with the first jet of described vapourizing furnace, described second oxygen enrichment mixing tank is connected with the second nozzle of described vapourizing furnace, and described first jet is arranged on the centrum portion of described vapourizing furnace; Described second nozzle is arranged on the top of described vapourizing furnace.Namely first jet is arranged on the close phase section of vapourizing furnace, and second nozzle is arranged on the dilute phase section of vapourizing furnace.The object arranging second nozzle adds secondary oxygen-rich air.
Preferably, as a kind of embodiment, first jet in the present embodiment is arranged on the below of fuel inlet, and the distance of first jet and described fuel inlet is 1.0 to 2.0 meters, and the angle between the central axis of described first jet and the central axis of described vapourizing furnace is 10 to 25 to spend.In the present embodiment, the elevation angle upwards of 15 degree to 17 degree can be formed between the central axis of first jet and the central axis of vapourizing furnace, also can form the downward oblique angle of about 21 degree, spray an oxygen-rich air entering so more easily and fuel mix, promote fuel combustion reaction.The number of the first jet in the present embodiment is 6, and these 6 first jet are evenly arranged on vapourizing furnace.
Preferably, as a kind of embodiment, the central axis of described second nozzle and the central axis upright of described vapourizing furnace.Namely secondary oxygen-rich air enters in vapourizing furnace from the horizontal direction of the body of heater of vapourizing furnace.The number of the second nozzle in the present embodiment is 24, and secondary oxygen-rich air out enters in vapourizing furnace from 24 second nozzles afterwards respectively from the second oxygen enrichment mixing tank.
Preferably, as a kind of embodiment, the coal gas desulfurization part in the present embodiment comprises hydrolysis device 211, first refrigerating unit 212, second cleaning apparatus 213, increasing apparatus 214, second refrigerating unit 215, thionizer 216, refining plant 217, dry desulfurization device 218 and circulating water device;
Hydrolysis device 211, first refrigerating unit 212, second cleaning apparatus 213, increasing apparatus 214, second refrigerating unit 215, thionizer 216, refining plant 217, dry desulfurization device 218 connect successively; Wherein be provided with sweetening agent and sorbent material in dry desulfurization device;
Described just gas treatment obtains the 3rd coal gas by hydrolysis device 211 process that is hydrolyzed, described 3rd coal gas carries out dedusting cooling by the first refrigerating unit 212 and gas-water separation process obtains the 4th coal gas, described 4th coal gas enters after the second cleaning apparatus 213 carries out dust removal process and obtains the 5th coal gas, the 6th coal gas is obtained after described 5th coal gas enters increasing apparatus 214, the 7th coal gas is obtained after described 6th coal gas enters the second refrigerating unit 215, the 8th coal gas is obtained after described 7th coal gas enters thionizer 216, described 8th coal gas enters after refining plant 217 purifies and obtains once desulfurization coal gas, secondary desulfuration coal gas is obtained after described once desulfurization coal gas enters dry desulfurization device 218,
Described circulating water device is connected with described first refrigerating unit 212 and the second refrigerating unit 215 respectively, and described recirculated water is back to circulating water device after circulating water device enters washing unit, the first refrigerating unit and the second refrigerating unit respectively.
In the present embodiment, hydrolysis device is hydrolytic tank, first refrigerating unit 212 is filler cooling washing tower, second cleaning apparatus 213 is wet electrical dust precipitator, increasing apparatus 214 is gas fan, second refrigerating unit 215 is cooling tower, and refining plant 217 is high pressure static electricity decoking tower, and circulating water device comprises circulation water station and circulating water treatment device.
Recirculated water described in the present embodiment enters filler cooling washing tower and cooling tower respectively from circulation water station, sprayed downwards by shower nozzle in tower or nozzle, with coal gas counter current contact, play the effect of cleaning and cooling respectively, then be out back to circulation water station by tower bottom, and use through circulating water treatment device process Posterior circle.
Preferably, as a kind of embodiment, the coal gas desulfurization part in the present embodiment also comprises doctor solution compounding system 219, and described doctor solution compounding system 219 is communicated with described thionizer 216;
Described doctor solution compounding system 219 comprises doctor solution device for formulating, desulfurization regeneration device and sulfur recovery unit, wherein said doctor solution device for formulating comprises solution preparation groove, doctor solution preparation pump, lean solution groove and desulfur pump, described desulfurization regeneration device comprises regenerative pump, regeneration tank and injector, and described sulfur recovery unit comprises sulphur foam chute, sulphur foam pump, filter and sulfur melting kettle; Described solution preparation pump is arranged on outside solution preparation groove, and the doctor solution in described solution allocation groove enters described thionizer by desulfur pump; The top of described regeneration tank is communicated with described lean solution groove; The top of described regeneration tank is communicated with sulphur foam chute, and described sulfur recovery unit is communicated with described lean solution groove;
According to the formula of doctor solution, the raw material of doctor solution is added doctor solution preparation pump and make suitable doctor solution, the doctor solution configured is kept in solution preparation groove, , by desulfur pump, doctor solution is delivered to top and the middle part of thionizer after doctor solution enters lean solution groove, doctor solution sprays from top to bottom, contact with back flow of gas, the hydrogen sulfide absorbed in gas obtains doctor solution rich solution, then described doctor solution rich solution enters regenerative pump after being gone out by the tower bottom flow of thionizer, the liquid inlet of the injector be arranged on above regeneration tank delivered to by doctor solution rich solution by described regenerative pump, enter bottom regeneration tank together with after described doctor solution rich solution is sprayed by injector with the air of self-priming, oxygen in injector and regeneration tank in air and doctor solution react, the sulphur foam generated carries out sulfur recovery by the top overflow of regeneration tank to sulfur recovery unit, doctor solution lean solution after regeneration enters lean solution groove and recycles, described sulphur foam is pressurizeed by sulphur foam pump, filters to isolate sulphur foam and clear liquid through filter, and sulphur foam enters sulfur melting kettle and obtains Sulphur element slab 99.5, and described clear liquid flows into lean solution groove and recycles.The raw material of doctor solution institute loss and water regular replenishment.Wherein the raw material of doctor solution comprises alkali and tannin extract.
Doctor solution after using, on the one hand in order to provide doctor solution to thionizer, can carry out regenerating and the sulphur of absorption be carried out extraction simultaneously and obtain sulphur product, achieve the Maxi-mize city value of product by doctor solution configuration-system that the present embodiment is arranged on the other hand.Doctor solution compounding system of the present invention will reuse the object reaching saving water resource after desulfurization regeneration, can obtain the waste that sulphur product makes to produce in the present invention simultaneously and have certain output value.
Further, the sulphur foam entering sulphur foam chute in the present embodiment squeezes into filter by sulphur foam pump, by filter separate sulfur foam and clear liquid; Clear liquid returns lean solution groove, and sulphur foam enters continuous sulfur melting kettle, is heated by jacket steam, melt as sulphur melt at 135 DEG C, enter sulphur disc molding by the lower part outlet of continuous sulfur melting kettle, top solution flows into solution collection groove, sends into lean solution groove recycle by solution pump.
Preferably, as a kind of embodiment, the described gas to generate electricity part in the present embodiment comprises gas compressor 311, air filter 312, air compressor 313, burner 314 and internal combustion turbine 316;
Described air filter 312 is communicated with described air compressor 313, described gas compressor 311 is all communicated with described burner 314 with described air compressor 313, the exhanst gas outlet of described burner is communicated with described internal combustion turbine 316 by high temp. flue 315, and described air compressor 313 is communicated with described high temp. flue 315;
Secondary desulfuration coal gas obtains the 9th coal gas after adopting gas compressor 311 to carry out processed compressed, described 9th coal gas enters burner 314, cooling air obtains filtrated air after air sucks after air filter 312 carries out filtration treatment, described filtrated air enters after air compressor 313 carries out processed compressed and obtains pressurized air, 9th coal gas and Partial shrinkage air pass into burner 314 and burning produces high-temperature flue gas in the burner, described high-temperature flue gas obtains the second flue gas in high temp. flue 315 with after Partial shrinkage air mixed, described second flue gas enters internal combustion turbine 316 and starts turbine acting and drive electrical generators generating.
The secondary desulfuration coal gas through processed compressed in the present embodiment enters in burner the high-temperature flue gas obtained that burns and enters internal combustion turbine acting generating to meet industrial power load together with the air through dedusting, processed compressed.Finish the flue gas after merit and enter gas heating part for generation of steam with carry out UTILIZATION OF VESIDUAL HEAT IN further.
Preferably, as a kind of embodiment, the described gas heating part in the present embodiment comprises the first waste heat boiler 411, second waste heat boiler 412, steam turbine 413 and exhaust system 414;
Wherein the first waste heat boiler 411 is communicated with steam turbine 413, and the second waste heat boiler 412 is communicated with deoxygenator, and the first waste heat boiler 411 is communicated with the second waste heat boiler 412, and the second waste heat boiler 412 is communicated with exhaust system 414; Described steam turbine 413 is connected with described vapourizing furnace 113 and is used for delivering vapor;
Being discharged by exhaust system 414 after the 3rd flue gas of internal combustion turbine 316 discharge enters the first waste heat boiler 411 and the second waste heat boiler 412 successively after generating, wherein the first waste heat boiler 411 presses through hot steam in producing, second waste heat boiler 412 produces low-pressure steam, press through hot steam in producing and enter steam turbine 413, the low-pressure steam produced enters deoxygenator for boiler supply water deaerating.The first waste heat boiler in the present embodiment can be middle pressure waster heat boiler, and the second waste heat boiler is low pressure waste heat boiler.
Steam turbine in the present embodiment may be used for extracting steam out with satisfied vapour load according to by vapour grade.Low-pressure saturated steam in described low-pressure steam enters deoxygenator for boiler supply water deaerating, and what meet low-pressure steam uses vapour demand.
Preferably, as a kind of embodiment, the first heat reclamation device 131 that described coal gas produces part is also communicated with described steam turbine 413, and namely the first heat reclamation device presses through hot steam in producing and also enters steam turbine.
Normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment of the present invention can solve the pollution problem of flue gas to air, effectively can utilize low grade coal again simultaneously, heat utilization rate can be improved, and be well positioned to meet industrial electricity consumption and use vapour demand, and device maneuverability of the present invention, cost is low, instant effect, and energy consumption is lower than the circulating fluidized bed combustion coal boiler power generation assembly of same scale.
Adopt the acting in conjunction of wet method string dry method to remove inorganic sulfur, the organosulfur such as hydrogen sulfide, sulphur carbonoxide in coal gas in the present invention, the sulphur content in the coal gas after actual treatment is≤1mg/m
3.Coal gas burns in the gas turbine, SO in the flue gas of generation
2content≤1mg/m
3, dust content≤1mg/m
3, NOx content is 30mg/m
3, all much smaller than the national discharge index dust≤50mg/Nm of fire coal boiler fume discharge
3, SO
2≤ 400mg/Nm
3, NOx≤450mg/Nm
3.Therefore normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method of the present invention and equipment have absolute predominance in exhaust gas emission.
Dust removal process in the present invention have employed the mode that dry process and wet processing combine, and use dry process to have the decontamination effect improving of efficient stable on the one hand, after process, its dustiness is lower than 1mg/m
3; Save water resources on the other hand, be fundamentally separated out the pollution of facility to environment of gas mud and sewage disposal; Moreover equipment of the present invention takes up an area little, saving water resource, reduces investment outlay, and operation energy consumption is low, adopts dust removal installation of the present invention to save land 30 ~ 60% according to statistics, and water saving 70 ~ 93%, reduces investment outlay 25 ~ 45%, reduces operation energy consumption 55 ~ 75%; Dust removal process of the present invention is all carried out continuously at air-tight state, achieve environmental friendliness operation, and dust removal installation level of automation of the present invention is high, reduces labour intensity.
The gas to generate electricity efficiency of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method of the present invention is high, reaches as high as more than 58% at present.For Steel Plant 50MW scale unit; the generating efficiency of normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method of the present invention can reach 40 ~ 46%; and being only about 23 ~ 30% with the Boiler Steam generating efficiency of scale, thermo-efficiency of the present invention exceeds more than 80%.The method that present invention employs vapourizing furnace normal pressure oxygen-enriched continuous gasification produces coal gas; adopt 50MW scale unit cogeneration; for melanism Ender furnace; it is 80% that coal gas produces thermo-efficiency (thermo-efficiency=(coal gas lower heating value+useless pot producing steam enthalpy)/(as-fired coal lower calorific value+steam in the boiler enthalpy)); cogeneration efficiency is 32 ~ 37%; compared with same scale Boiler Steam generating efficiency 23 ~ 30%, the thermo-efficiency of gas maked coal cogeneration about exceeds 40%.In addition, outer coal consumption of power supply of the present invention is 395 ~ 480g/kwh, and the outer coal consumption of power supply of steam boiler is 430 ~ 500g/kwh.Save mark coal 20 ~ 35g/kwh.
The above embodiment only have expressed several embodiment of the present invention, and it describes comparatively concrete and detailed, but therefore can not be interpreted as the restriction to the scope of the claims of the present invention.It should be pointed out that for the person of ordinary skill of the art, without departing from the inventive concept of the premise, can also make some distortion and improvement, these all belong to protection scope of the present invention.Therefore, the protection domain of patent of the present invention should be as the criterion with claims.
Claims (8)
1. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method, is characterized in that: described method comprises the steps:
S100: produce coal gas; Fuel, oxygen-rich air and steam are added vapourizing furnace respectively and produces original raw gas, then dedusting is carried out to original raw gas and obtain just gas treatment with cooling process; The oxygen concentration of described oxygen-rich air is 70% to 99.5%;
S200: coal gas desulfurization: desulfurization process is carried out to first gas treatment and obtains desulfurization coal gas;
S300: power generation and heat supply: obtain high-temperature flue gas after desulfurization coal gas and air are passed into burner combustion, then high-temperature flue gas is passed into after hybrid cooling process the acting of internal combustion turbine startup turbine to generate electricity with drive electrical generators, finish the high-temperature flue gas after merit enter middle pressure waster heat boiler produce in press through hot steam, press through hot steam in described and enter steam turbine for being back to vapourizing furnace after generating, enter low pressure waste heat boiler from middle pressure waster heat boiler high-temperature flue gas out and produce low-pressure steam, described low-pressure steam is that saturation steam is for boiler supply water deaerating, the low-temperature flue gas of discharging from low pressure waste heat boiler directly enters air,
Described step S100 comprises the steps:
S101: fuel is delivered into vapourizing furnace by fuel delivery system;
S102: configuration oxygen-rich air, and make oxygen-rich air enter the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank respectively, the oxygen-rich air entering the first oxygen enrichment mixing tank enters vapourizing furnace by first jet, and the secondary oxygen-rich air entering the second oxygen enrichment mixing tank enters vapourizing furnace by second nozzle;
S103: the opposing steam flow from steam turbine enters vapourizing furnace;
S104: fuel, oxygen-rich air and steam carry out burning and forms original raw gas in vapourizing furnace; Then original raw gas is drawn by top of gasification furnace and enter tornado dust collector; Now the temperature of original raw gas is 950 ± 20 DEG C;
S105: isolate the flying dust in original raw gas by tornado dust collector, obtains the first raw gas through first time dust removal process, and flying dust is returned vapourizing furnace and carry out second gasification further; Wherein the temperature of the first raw gas is 850 ± 20 DEG C, and dustiness is 180 to 210g/m
3;
S106: carry out waste heat recovery processing to the first raw gas, obtains the second raw gas, presses through hot steam in obtaining simultaneously; Now the temperature of the second raw gas is 150 ± 10 DEG C, and dustiness is 12 to 18g/m
3;
S107: carry out second time dust removal process to the second raw gas and obtain just gas treatment, the temperature of first gas treatment is 150 DEG C, and dustiness is 75mg/m
3.
2. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method according to claim 1, is characterized in that: described step S200 comprises the steps:
S201: first gas treatment is hydrolyzed process, the organic sulfide in coal gas is converted into hydrogen sulfide, obtains the 3rd coal gas;
S202: obtain the 4th coal gas after carrying out dedusting cooling and gas-water separation process to the 3rd coal gas, the temperature of the 4th coal gas is 35 ± 5 DEG C, and dustiness is 8 to 12mg/m
3, hydrogen sulfide content is 1400 to 1600mg/Nm
3;
S203: carry out wet desulphurization process to the 4th coal gas and obtain once desulfurization coal gas, the equipment that wet desulphurization adopts is thionizer, and the hydrogen sulfide content of once desulfurization coal gas is 40 to 60mg/Nm
3, temperature is 40 ± 5 DEG C;
S204: adopt sweetening agent and sorbent material to carry out dry desulfurization process to once desulfurization coal gas and obtain secondary desulfuration coal gas, the hydrogen sulfide content of secondary desulfuration coal gas is less than 1mg/Nm
3.
3. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method according to claim 2, is characterized in that: described step S203 comprises the steps:
S2031: carry out dust removal process to the 4th coal gas and obtain the 5th coal gas, the dustiness of described 5th coal gas is lower than 1mg/m
3;
S2032: boosting process is carried out to the 5th coal gas and obtains the 6th coal gas, the pressure of described 6th coal gas is 10KPa, and temperature is 50 ± 5 DEG C;
S2033: carry out cooling process to the 6th coal gas, obtains the 7th coal gas, and the temperature of described 7th coal gas is 35 DEG C;
S2034: adopt thionizer to carry out wet desulphurization process to the 7th coal gas and obtain the 8th coal gas, thionizer absorbs the hydrogen sulfide in the 7th coal gas;
S2035: carry out purifying treatment to the 8th coal gas, removes fine dust, elaioleucite, the sulphur foam in coal gas, obtains once desulfurization coal gas.
4. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method according to claim 1, is characterized in that: described step S300 comprises the steps:
S301: secondary desulfuration coal gas is carried out processed compressed and obtain the 9th coal gas, and the 9th coal gas is passed into burner; The pressure of the 9th coal gas is 1.5 to 2.4MPa, and temperature is 350 ± 10 DEG C;
S302: obtain pressurized air after dust removal process and processed compressed are carried out to air, and Partial shrinkage air is passed into burner; Compressed-air actuated dustiness is lower than 1mg/m
3, pressure is 1.5 to 2.4MPa;
S303: the nine coal gas and pressurized air burn generation high-temperature flue gas in the burner; The temperature of high-temperature flue gas is 1600 ± 50 DEG C;
S304: high-temperature flue gas and rest part pressurized air are mixed to get the second flue gas, the temperature of the second flue gas is 1100 ± 50 DEG C, and pressure is 1.4 to 2.3MPa;
S305: make the second flue gas enter internal combustion turbine and start turbine acting and drive electrical generators generating; The temperature finishing the 3rd flue gas from internal combustion turbine discharge after merit is 500 to 600 DEG C, and pressure is 5000 to 6000Pa;
S306: the 3rd flue gas is entered during the first waste heat boiler obtains and press through hot steam, presses through hot steam and enters steam turbine and generate electricity in described, from steam turbine opposing steam flow out to vapourizing furnace;
S307: enter the second waste heat boiler from the first waste heat boiler the 4th flue gas out and obtain low-pressure steam, described low-pressure steam is that saturated low-pressure steam supply deoxygenator is for boiler supply water deaerating;
S308: from the second waste heat boiler out the 5th flue gas discharge.
5. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment, is characterized in that: described equipment comprises coal gas and produces part, coal gas desulfurization part, gas to generate electricity part and gas heating part:
Described coal gas is produced and is carried out desulfurization after the obtained first gas treatment of part enters coal gas desulfurization part and obtain desulfurization coal gas, and desulfurization coal gas enters and enters gas heating part after gas to generate electricity part generates electricity and reclaim heat further and provide steam;
Described coal gas is produced part and is comprised gazogene, cleaning apparatus and heat reclamation device;
Described gazogene comprises fuel delivery system, oxygen enriched air system, vapourizing furnace and dreg removing system; Described fuel delivery system is communicated with described vapourizing furnace by the fuel inlet be arranged on described vapourizing furnace, and described oxygen enriched air system is communicated with described vapourizing furnace by the nozzle be arranged on vapourizing furnace, and described dreg removing system is arranged on the bottom of described vapourizing furnace; Fuel, oxygen-rich air and the steam from gas heating part produce original raw gas in vapourizing furnace;
Described oxygen enriched air system comprises the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank, the nozzle of described vapourizing furnace comprises first jet and second nozzle, described first oxygen enrichment mixing tank is connected with the first jet of described vapourizing furnace, described second oxygen enrichment mixing tank is connected with the second nozzle of described vapourizing furnace, and described first jet is arranged on the centrum portion of described vapourizing furnace; Described second nozzle is arranged on the top of described vapourizing furnace;
The central axis of described second nozzle and the central axis upright of described vapourizing furnace.
6. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment according to claim 5, is characterized in that:
Described cleaning apparatus comprises tornado dust collector and the first cleaning apparatus; Described tornado dust collector are communicated with described vapourizing furnace by return line; Described first cleaning apparatus is sack cleaner or electric precipitator;
Described heat reclamation device comprises the first heat reclamation device;
Described original raw gas obtains the first raw gas after carrying out dedusting by tornado dust collector, the first raw gas obtain after entering the first heat reclamation device the second raw gas and in press through hot steam, the second raw gas obtains just gas treatment after entering the first cleaning apparatus.
7. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment according to claim 6, it is characterized in that: described first jet is arranged on the below of described fuel inlet, the distance of described first jet and described fuel inlet is 1.0 to 2.0 meters, and the angle between the central axis of described first jet and the central axis of described vapourizing furnace is 10 to 25 to spend.
8. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment according to claim 5, is characterized in that: described coal gas desulfurization part comprises hydrolysis device, the first refrigerating unit, the second cleaning apparatus, increasing apparatus, the second refrigerating unit, thionizer, refining plant, dry desulfurization device and circulating water device;
Hydrolysis device, the first refrigerating unit, the second cleaning apparatus, increasing apparatus, the second refrigerating unit, thionizer, refining plant, dry desulfurization device connect successively; Wherein be provided with sweetening agent and sorbent material in dry desulfurization device;
Described just gas treatment obtains the 3rd coal gas by the hydrolysis device process that is hydrolyzed, described 3rd coal gas carries out dedusting cooling by the first refrigerating unit and gas-water separation process obtains the 4th coal gas, described 4th coal gas enters after the second cleaning apparatus carries out dust removal process and obtains the 5th coal gas, the 6th coal gas is obtained after described 5th coal gas enters increasing apparatus, the 7th coal gas is obtained after described 6th coal gas enters the second refrigerating unit, the 8th coal gas is obtained after described 7th coal gas enters thionizer, described 8th coal gas enters after refining plant purifies and obtains once desulfurization coal gas, secondary desulfuration coal gas is obtained after described once desulfurization coal gas enters dry desulfurization device,
Described circulating water device is connected with described first refrigerating unit and the second refrigerating unit respectively, and described recirculated water is back to circulating water device after circulating water device enters the first refrigerating unit and the second refrigerating unit respectively.
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