CN103265976A - 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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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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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
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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 the 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 present large and medium-sized chemical enterprise device, all bigger with thermal load, general enterprise adopts the supporting extraction condensing type generating set of middle and high pressure steam boiler to reach with vapour balance and electricity consumption requirement, namely adopt coal firing boiler to produce steam, utilize steam turbine generating, and the steam of extracting the different pressures grade out satisfy the chemical enterprise device use the vapour requirement.But the problem that this method exists is the unit small scale, efficient is low, on the other hand because sulfur dioxide in flue gas, the content of nitrogen oxide height of coal firing boiler, adopt present desulfurization, denitride technology can't take off level to lower aq again, cause topsoil serious.
Summary of the invention
Based on this, be necessary the irrationality that exists at prior art, provide a kind of new, can satisfy power load and with normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method and the equipment of thermal load, economy.
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 produce original raw gas, then original raw gas is carried out dedusting and lower the temperature to handle obtaining just handling coal gas;
S200: coal gas desulfurization: first processing coal gas is carried out the desulfurization processing obtain desulfurization coal gas;
S300: power generation and heat supply: will obtain high-temperature flue gas after desulfurization coal gas and the air feeding burner combustion, then high-temperature flue gas is handled back feeding internal combustion turbine startup turbine through hybrid cooling and do work to drive generator for electricity generation, finishing high-temperature flue gas after the merit presses in entering waste heat boiler to press superheated vapour in producing, pressing superheated vapour to enter steam turbine in described is used for being back to vapourizing furnace after the generating, the high-temperature flue gas of therefrom pressing waste heat boiler to come out enters the low pressure waste heat boiler and produces low-pressure steam, saturation steam in the described low-pressure steam is used for boiler supply water deaerating, and the low-temperature flue gas of discharging from the low pressure waste heat boiler directly enters atmosphere.
Among embodiment, described step S100 comprises the steps: therein
S101: fuel is delivered into vapourizing furnace by fuel delivery system;
S102: the configuration oxygen concentration is 70% to 99.5% oxygen-rich air, and make oxygen-rich air enter the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank respectively, an oxygen-rich air that enters the first oxygen enrichment mixing tank enters vapourizing furnace by first nozzle, and the secondary oxygen-rich air that enters 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 burn in vapourizing furnace and form original raw gas; Then original raw gas is drawn by top of gasification furnace and enter tornado dust collector; This moment, the temperature of original raw gas was 950 ± 20 ℃;
S105: isolate flying dust in the original raw gas by tornado dust collector, obtain first raw gas through the dust removal process first time, and flying dust is returned vapourizing furnace further carry out second gasification; Wherein the temperature of first raw gas is 850 ± 20 ℃, and dustiness is 180 to 210g/m
3
S106: first raw gas is carried out waste heat recovery processing, obtain second raw gas, press superheated vapour in obtaining simultaneously; This moment, the temperature of second raw gas was 150 ± 10 ℃, and dustiness is 12 to 18g/m
3
S107: second raw gas is carried out handling coal gas at the beginning of the second time, dust removal process obtained, and just handling temperature of gas is 150 ℃, and dustiness is 75mg/m
3
Among embodiment, described step S200 comprises the steps: therein
S201: to the processing that is hydrolyzed of first processing coal gas, the organic sulfide in the coal gas is converted into hydrogen sulfide, obtains the 3rd coal gas;
S202: the 3rd coal gas is carried out obtaining the 4th coal gas after dedusting cooling and gas-water separation are handled, and the 4th temperature of gas is 35 ± 5 ℃, and dustiness is 8 to 12mg/m
3, hydrogen sulfide content is 1400 to 1600mg/Nm
3
S203: the 4th coal gas is carried out wet desulphurization handle and to obtain once desulfurization coal gas, the equipment that wet desulphurization is adopted is thionizer, and the hydrogen sulfide content of once desulfurization coal gas is 40 to 60mg/Nm
3, temperature is 40 ± 5 ℃;
S204: adopt sweetening agent and sorbent material that once desulfurization coal gas is carried out the dry desulfurization processing and obtain secondary desulfurization coal gas, the hydrogen sulfide content of secondary desulfurization coal gas is less than 1mg/Nm
3
Among embodiment, described step S203 comprises the steps: therein
S2031: the 4th coal gas is carried out dust removal process obtain the 5th coal gas, the dustiness of described the 5th coal gas is lower than 1mg/m
3
S2032: the 5th coal gas boosted to handle obtains the 6th coal gas, and the pressure of described the 6th coal gas is about 10KPa, and temperature is 50 ± 5 ℃;
S2033: the 6th coal gas is carried out cooling process, obtain the 7th coal gas, described the 7th temperature of gas is 35 ℃;
S2034: adopt thionizer to carry out the wet desulphurization processing to the 7th coal gas and obtain the 8th coal gas, thionizer has absorbed the hydrogen sulfide in the 7th coal gas.
S2035: the 8th coal gas is carried out purifying treatment, remove fine dust, elaioleucite, sulphur foam in the coal gas, obtain once desulfurization coal gas.
Among embodiment, described step S300 comprises the steps: therein
S301: secondary desulfurization coal gas is carried out processed compressed obtain the 9th coal gas, and the 9th coal gas is fed burner; The pressure of the 9th coal gas is 1.5 to 2.4MPa, and temperature is 350 ± 10 ℃;
S302: air is carried out obtaining pressurized air after dust removal process and the processed compressed, and part pressurized air is fed burner; Compressed-air actuated dustiness is lower than 1mg/m
3, pressure is 1.5 to 2.4MPa;
S303: the 9th coal gas and pressurized air burn in burner and produce high-temperature flue gas; The temperature of high-temperature flue gas is 1600 ± 50 ℃;
S304: high-temperature flue gas mixed obtaining second flue gas with rest part pressurized air, the temperature of second flue gas is 1100 ± 50 ℃, and pressure is 1.4 to 2.3MPa;
S305: make second flue gas enter internal combustion turbine and start the turbine acting and drive generator for electricity generation; The temperature of finishing the 3rd flue gas of discharging from internal combustion turbine after the merit is 500 to 600 ℃, and pressure is 5000 to 6000Pa;
S306: make the 3rd flue gas enter first waste heat boiler and press superheated vapour in obtaining, press superheated vapour to enter steam turbine in described and generate electricity, the opposing steam flow that comes out from steam turbine is to vapourizing furnace;
S307: the 4th flue gas that comes out from first waste heat boiler enters second waste heat boiler and obtains low-pressure steam, and the saturated low-pressure steam in the described low-pressure steam is supplied with deoxygenator and is used for boiler supply water deaerating;
S308: discharge from the 5th flue gas that second waste heat boiler comes out.
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 that coal gas produces part, coal gas desulfurization part, gas to generate electricity part and gas heating part:
Described coal gas is produced the first processing coal gas that makes of part and is entered and carry out desulfurization after the coal gas desulfurization part and obtain desulfurization coal gas, and desulfurization coal gas enters and enters the gas heating part after gas to generate electricity partly generates electricity and further reclaim heat and steam is provided.
Among embodiment, described coal gas is produced part and is comprised gazogene, cleaning apparatus and heat reclamation device therein;
Described gazogene comprises fuel delivery system, oxygen enriched air system, vapourizing furnace and dreg removing system; Described fuel delivery system communicates with described vapourizing furnace by the fuel inlet that is arranged on the described vapourizing furnace, and described oxygen enriched air system communicates with described vapourizing furnace by the nozzle that is arranged on the vapourizing furnace, and described dreg removing system is arranged on the bottom of described vapourizing furnace; Fuel, oxygen-rich air and in vapourizing furnace, produce original raw gas from the steam of gas heating part;
Described cleaning apparatus comprises tornado dust collector and first cleaning apparatus; Described tornado dust collector communicate with described vapourizing furnace by return line;
Described heat reclamation device comprises first heat reclamation device;
Described original raw gas is undertaken obtaining first raw gas after the dedusting by tornado dust collector, and first raw gas obtains second raw gas and middle pressure superheated vapour after entering first heat reclamation device, and second raw gas obtains just handling coal gas after entering first cleaning apparatus.
Therein among 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 nozzle and second nozzle, first nozzle of the described first oxygen enrichment mixing tank and described vapourizing furnace is connected, second nozzle of the described second oxygen enrichment mixing tank and described vapourizing furnace is connected, and described first nozzle is arranged on the centrum portion of described vapourizing furnace; Described second nozzle is arranged on the top of described vapourizing furnace.
Therein among embodiment, described first nozzle is arranged on the below of described fuel inlet, the distance of described first nozzle and described fuel inlet is 1.0 to 2.0 meters, and the angle between the central axis of described first nozzle and the central axis of described vapourizing furnace is 10 to 25 degree.
Among embodiment, the central axis of described second nozzle is vertical with the central axis of described vapourizing furnace therein.
Among embodiment, described coal gas desulfurization partly comprises hydrolysis device, first refrigerating unit, second cleaning apparatus, increasing apparatus, second refrigerating unit, thionizer, refining plant, dry desulfurization device and circulating water device therein;
Hydrolysis device, first refrigerating unit, second cleaning apparatus, increasing apparatus, second refrigerating unit, thionizer, refining plant, dry desulfurization device connect successively; Wherein be provided with sweetening agent and sorbent material in the dry desulfurization device;
The described coal gas of processing just is hydrolyzed to handle by hydrolysis device and obtains the 3rd coal gas, described the 3rd coal gas carries out the dedusting cooling by first refrigerating unit and the gas-water separation processing obtains the 4th coal gas, described the 4th coal gas enters second cleaning apparatus to carry out obtaining the 5th coal gas after the dust removal process, described the 5th coal gas obtains the 6th coal gas after entering increasing apparatus, described the 6th coal gas obtains the 7th coal gas after entering second refrigerating unit, described the 7th coal gas obtains the 8th coal gas after entering thionizer, described the 8th coal gas enters and obtains once desulfurization coal gas after refining plant purifies, and described once desulfurization coal gas obtains secondary desulfurization coal gas after entering dry desulfurization device;
Described circulating water device is connected with second refrigerating unit with described first refrigerating unit respectively, and described recirculated water is back to circulating water device after circulating water device enters first refrigerating unit and second refrigerating unit respectively.
Among embodiment, described gas to generate electricity partly comprises gas compressor, air filter, air compressor, burner and internal combustion turbine therein;
Described air filter is communicated with described air compressor, described gas compressor and described air compressor all are communicated with described burner, the exhanst gas outlet of described burner is communicated with described air compressor and described high-temperature flue gas channel connection by the high-temperature flue gas passage with described internal combustion turbine;
Secondary desulfurization coal gas obtains the 9th coal gas through behind the gas compressor, enter burner, air carries out entering air compressor after the dust removal process through air filter and carries out obtaining pressurized air after the processed compressed, the 9th coal gas and part pressurized air feed burner and burning generation high-temperature flue gas in burner, described high-temperature flue gas obtains second flue gas in the high-temperature flue gas passage with after part pressurized air mixes, described second flue gas enters internal combustion turbine and starts the turbine acting and drive generator for electricity generation.
Among embodiment, described gas heating partly comprises first waste heat boiler, second waste heat boiler, steam turbine and exhaust system therein;
Wherein first waste heat boiler is communicated with steam turbine, and second waste heat boiler is communicated with deoxygenator, and first waste heat boiler is communicated with second waste heat boiler, and second waste heat boiler is communicated with exhaust system; Described steam turbine is connected with described vapourizing furnace;
After entering first waste heat boiler and second waste heat boiler successively, the 3rd flue gas from the internal combustion turbine discharge after the generating discharges by exhaust system, wherein first waste heat boiler is pressed superheated vapour in producing, second waste heat boiler produces low-pressure steam, the middle pressure superheated vapour that produces enters steam turbine, and the low-pressure saturated steam that produces enters deoxygenator.
Among embodiment, described first heat reclamation device also is communicated with described steam turbine therein.
Among embodiment, described coal gas desulfurization part also comprises the doctor solution compounding system therein, 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 tank, 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 the solution Preparation tank, and the doctor solution in the described solution Preparation tank enters described thionizer by desulfur pump; The top of described regeneration tank is communicated with described lean solution groove and sulphur foam chute; Described sulfur recovery unit is communicated with described lean solution groove;
According to the prescription of doctor solution the raw material adding doctor solution of doctor solution is prepared pump and make suitable doctor solution, make suitable doctor solution by doctor solution preparation pump, doctor solution is mended top and the middle part of by desulfur pump doctor solution being delivered to thionizer behind the lean solution groove, doctor solution sprays from top to bottom, contact with back flow of gas, the hydrogen sulfide that absorbs in the gas obtains the doctor solution rich solution, described doctor solution rich solution enters regenerative pump after being gone out by the tower bottom flow of thionizer then, the liquid inlet of the injector that is arranged on the regeneration tank top delivered to the doctor solution rich solution by described regenerative pump, described doctor solution rich solution enters the regeneration tank bottom after the air of self-priming sprays by injector, airborne oxygen and doctor solution reaction in injector and regeneration tank, to the sulphur foam chute, the doctor solution lean solution after the regeneration enters the lean solution groove and recycles the sulphur foam that generates by the top overflow of regeneration tank; Described sulphur foam filters to isolate sulphur foam and clear liquid by the pressurization of sulphur foam pump through filter, and the sulphur foam enters sulfur melting kettle and obtains Sulphur element slab 99.5, and described clear liquid flows into the lean solution groove.
The invention has the beneficial effects as follows:
(1) normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method cost is low, instant effect, it is bigger to build handiness, pollute little, and energy-conserving and environment-protective;
(2) dust removal process in normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method has efficient and stable purification function, is lower than 1mg/m through the dust content of gas after the dust removal process
3And the huge facility of fundamentally having got rid of gas mud and sewage disposal reaches the pollution to environment;
(3) dust removal installation in normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heating equipment 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 efficient height of normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method reaches as high as more than 58% at present.
(5) dust content that the normal pressure oxygen-enriched continuous gasification-the combined combustion and steam turbine power heating equipment obtains of the present invention is low, and sulphur content is low, need can directly not enter atmosphere through other processing.
Description of drawings
Below in conjunction with concrete drawings and the specific embodiments, the present invention is further elaborated.
Fig. 1 is the synoptic diagram that the coal gas of normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heating equipment is produced part.
Fig. 2 is the synoptic diagram of the coal gas desulfurization part of normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heating equipment.
Fig. 3 is the synoptic diagram of gas to generate electricity part and the gas heating part of normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heating equipment.
Embodiment
For the purpose, technical scheme and the advantage that make normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method and equipment is clearer, 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 produce original raw gas, then raw gas is carried out dedusting and lower the temperature to handle obtaining just handling coal gas; 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 handling coal gas;
S200: coal gas desulfurization: first processing coal gas is carried out the desulfurization processing obtain desulfurization coal gas; This step adopts the coal gas desulfurization part that first processing coal gas is carried out the desulfurization processing and obtains desulfurization coal gas;
S300: power generation and heat supply: will obtain high-temperature flue gas after desulfurization coal gas and the air feeding burner combustion, then high-temperature flue gas is handled back feeding internal combustion turbine startup turbine through hybrid cooling and do work to drive generator for electricity generation, finishing high-temperature flue gas after the merit presses in entering waste heat boiler to press superheated vapour in producing, pressing superheated vapour to enter steam turbine in described is used for being back to vapourizing furnace after the generating, the high-temperature flue gas of therefrom pressing waste heat boiler to come out enters the low pressure waste heat boiler and produces low-pressure saturated steam, described low-pressure saturated steam enters deoxygenator and is used for boiler supply water deaerating, and the low-temperature flue gas of discharging from the low pressure waste heat boiler directly enters atmosphere.This step has adopted gas to generate electricity partly to generate electricity, and simultaneously the high-temperature flue gas after the generating (finishing merit) is partly carried out waste heat recovery by gas heating and makes heat rationally be utilized.
Present embodiment is at first produced part producing by coal gas and is gone out just to handle coal gas, utilize the coal gas desulfurization part that first processing coal gas is carried out the desulfurization processing then and obtain desulfurization coal gas, afterwards the desulfurized coal pneumatic transmission is gone into gas to generate electricity and partly generate electricity to satisfy power load, the coal gas of finishing merit is sent into the gas heating part press superheated vapour and low-pressure steam with in producing, press superheated vapour to enter steam turbine wherein, can extract the steam of different grades out according to industrial needs to satisfy the industrial vapour requirement of using, low-pressure steam can satisfy the deoxygenation vapour requirement of boiler feed water.
In the present embodiment raw gas is carried out dust removal process and desulfurization processing, reduced dustiness and the sulphur content in the raw gas, make institute of the present invention exhaust gas discharged need not namely to meet waste gas emission standard through off gas treatment, saved facility investment.
Preferable, 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 transfer roller, need add N when general coal is stored in the coal bunker
2(P=0.015Pa) protection, described fuel transfer roller is arranged on bottom and the described fuel transfer roller of coal bunker coal is sent into vapourizing furnace 113 from the fuel inlet that is arranged on vapourizing furnace one side; Described fuel transfer roller can be for a plurality of according to design flow;
S102: configuration oxygen-containing gas volume concentrations is 70% to 99.5% oxygen-rich air, make the oxygen-rich air for preparing enter the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank respectively, an oxygen-rich air that enters the first oxygen enrichment mixing tank enters vapourizing furnace 113 by first nozzle, and the secondary oxygen-rich air that enters 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, and the oxygen-rich air configuration 65～57:0～32 is mixed purity oxygen and air to obtain by ratio of weight and the number of copies;
S103: the opposing steam flow from steam turbine enters vapourizing furnace 113;
S104: fuel, oxygen-rich air and the steam formation raw gas that in vapourizing furnace 113, burns; Then raw gas is drawn by vapourizing furnace 113 tops and enter tornado dust collector 121; This moment, the temperature of raw gas was 950 ± 20 ℃, was approximately 950 ℃; Close phase section is formed at the big bottom of coarse particles in vapourizing furnace 113 of the major part of the coal in the present embodiment in the vapourizing furnace 113, raw material becomes boiling state, gas in this zone, Gu violent mass transfer and heat transfer and combustion oxidation reaction take place in two-phase, temperature of reaction is 950 to 1000 ℃, enter the small-particle that macrobead produces because of the cracking of being heated in the vapourizing furnace this moment, the fine powder that then enters the coal in the vapourizing furnace 113 is carried by reactant gases with small-particle and leaves close section mutually, freeboard of fluidized bed is formed at the top at vapourizing furnace 113, and further react at freeboard of fluidized bed and secondary oxygen-rich air, secondary oxygen-rich air in the present embodiment has two effects: the one, 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 the divided gas flow; The 2nd, promote reaction, make the carbon in the fine particle of carrying secretly in the gas continue gasification reaction, with methane and further burning and the cracking of higher carbon compounds of close phase section generation; The raw gas that raw material in this step forms is drawn by top of gasification furnace and is carried out subsequent disposal;
S105: isolate flying dust in the raw gas by tornado dust collector 121, obtain first raw gas through the dust removal process first time, and flying dust is returned vapourizing furnace 113 further carry out second gasification; Wherein the temperature of first raw gas is 850 ± 20 ℃, generally is about 850 ℃, and dustiness is 180 to 210g/m
3, generally be about 200g/m
3Flying dust can return vapourizing furnace 113 by return line in the present embodiment;
S106: adopt 131 pairs of first raw gass of first heat reclamation device to carry out (superheat section, evaporator section, economizer) waste heat recovery processing, obtain second raw gas, press superheated vapour in obtaining simultaneously; This moment, the temperature of second raw gas was 150 ± 10 ℃, generally was about 150 ℃, and dustiness is 12 to 18g/m
3, generally being about 15g/m3, particle diameter is less than 50 μ m; The pressure of the middle pressure superheated vapour in this step is approximately 3.82MPa to 6.5MPa, and temperature is about 450 ℃ to 520 ℃; Middle pressure superheated vapour in this step enters steam turbine;
S107: adopt 122 pairs of second raw gass of first cleaning apparatus to carry out handling coal gas at the beginning of the second time, dust removal process obtained, the dustiness of just handling coal gas is 75mg/m
3Second cleaning apparatus in the present embodiment can be sack cleaner or electric precipitator.
Preferable, as a kind of embodiment, described step S200 comprises the steps:
S201: adopt and to handle the coal gas processing that is hydrolyzed at the beginning of 211 pairs of the hydrolysis devices, the organic sulfide in the coal gas is converted into hydrogen sulfide, obtain the 3rd coal gas; Hydrolysis device in the present embodiment is hydrolytic tank, and the main purpose of this step is to make the organic sulfide of just handling in the coal gas be converted into hydrogen sulfide so that remove;
S202: adopt 212 pairs of the 3rd coal gas of first refrigerating unit to carry out obtaining the 4th coal gas after dedusting cooling and gas-water separation are handled, the 4th temperature of gas is 35 ± 5 ℃, and general temperature is about 35 ℃, and dustiness is 8 to 12mg/m
3, dustiness generally is about 10mg/m
3, hydrogen sulfide content is 1400 to 1600mg/Nm
3, hydrogen sulfide content is about 1500mg/Nm usually
3First refrigerating unit in the present embodiment is filler cooling washing tower;
S203: the 4th coal gas is carried out the wet desulphurization processing obtain once desulfurization coal gas; The equipment that wet desulphurization is adopted is thionizer, and the hydrogen sulfide content of once desulfurization coal gas is 40 to 60mg/Nm
3, temperature is 40 ± 5 ℃, typical temperature is 40 ℃; Wherein the doctor solution in the thionizer is from doctor solution compounding system and desulfurization regeneration system; The 5th coal gas in this step enters the bottom of thionizer, coal gas packing layer by thionizer from bottom to top in thionizer, and with the doctor solution counter current contact of the top spray of thionizer, the hydrogen sulfide in this moment gas is desulfurized liquid and absorbs;
S204: adopt sweetening agent and sorbent material that cooling once desulfurization coal gas is carried out the dry desulfurization processing in dry desulfurization device 218 and obtain secondary desulfurization coal gas, the hydrogen sulfide content of secondary desulfurization coal gas is less than 1mg/Nm
3In the present embodiment, described sweetening agent is adsorptivity.
In the present embodiment, coal gas is carried out dust removal process adopt the mode that dry method dust is handled and the wet dedusting processing combines, at first adopt dry method dust to handle most of flying dust of removing in the coal gas, adopt wet dedusting further to carry out dedusting and cooling simultaneously then, so not only solved the problem of the seriously polluted and water resource waste of water that simple employing water washing dedust causes, 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, at first the sulfide in the coal gas is converted into hydrogen sulfide by hydrolysis, adopt the hydrogen sulfide in the wet desulphurization absorption coal gas then, adopt absorption such as sweetening agent and sorbent material further to reduce sulphur content at last again, sulfur method in the present embodiment acts synergistically together, makes that the sulphur content in the coal gas reduces.
Preferable, as a kind of embodiment, the step S203 in the present embodiment also comprises the steps:
S2031: adopt 213 pairs of the 4th coal gas of second cleaning apparatus to carry out dust removal process and obtain the 5th coal gas, the dustiness of described the 5th coal gas is lower than 1mg/m
3In the present embodiment, the 3rd cleaning apparatus is preferably wet electrical dust precipitator;
S2032: 214 pairs of the 5th coal gas of employing increasing apparatus boost to handle and obtain the 6th coal gas, and the pressure of described the 6th coal gas is about 10kPa, and temperature is 50 ± 5 ℃, and general temperature is about 50 ℃; In the present embodiment, described increasing apparatus is gas fan;
S2033: adopt 215 pairs of the 6th coal gas of second refrigerating unit to carry out cooling process and obtain the 7th coal gas; Second refrigerating unit in the present embodiment is cooling tower; The 6th coal gas enters the bottom of cooling tower in this step, and the water coolant counter current contact under with the cat head of cooling tower spray cools, and the top by cooling tower obtains the 7th coal gas then;
S2034: adopt 216 pairs of the 7th coal gas of thionizer to carry out the wet desulphurization processing and obtain the 8th coal gas, wherein thionizer has absorbed the hydrogen sulfide in the 7th coal gas.
S2035: adopt 217 pairs of the 8th coal gas of refining plant to carry out purifying treatment, fine dusts, greasy dirt, the sulphur foam removed in the 8th coal gas obtain once desulfurization coal gas, and described once desulfurization temperature of gas is 35 ℃; Refining plant in the present embodiment is high pressure static electricity decoking tower;
In order to make wet desulphurization respond well, processing such as present embodiment had carried out a series ofly boosting before coal gas enters thionizer, dedusting, cooling.Adopt sorbent material and sweetening agent to carry out dry desulfurization afterwards and handle, can further absorb the sulfide in the coal gas on the one hand.Can absorb moisture in the coal gas etc. on the other hand, make coal gas be applicable to follow-up generating acting.
First refrigerating unit 212 in the present embodiment, the water coolant of second refrigerating unit 215 all can recycle, and the doctor solution in the thionizer in the present embodiment can carry out reusing after the manipulation of regeneration, can save process cost like this, save resource.
Preferable, as a kind of embodiment, described step S300 comprises the steps:
S301: adopt 311 pairs of secondary desulfurization of gas compressor coal gas to carry out processed compressed and obtain the 9th coal gas, and the 9th coal gas is fed burner 314; The pressure of the 9th coal gas is 1.5 to 2.4MPa, and temperature is 350 ± 10 ℃, is preferably 350 ℃; In the present embodiment, through the sulphur content≤1mg/m of the secondary desulfurization coal gas after the desulfurization processing
3, dustiness≤1mg/m
3
S302: adopt 312 pairs of air of air filter to carry out dust removal process, adopt 313 pairs of air of air compressor to carry out obtaining pressurized air after the processed compressed afterwards, and part pressurized air is fed burner 314; Compressed-air actuated dustiness is lower than 1mg/m
3, pressure is 1.5 to 2.4MPa, temperature is 300 ℃;
S303: the 9th coal gas and pressurized air burn in burner 314 and produce high-temperature flue gas; The temperature of high-temperature flue gas is 1600 ± 50 ℃, and typical temperature is about 1600 ℃;
S304: high-temperature flue gas mixed obtaining second flue gas with the pressurized air of rest part, the temperature of second flue gas is 1100 ± 50 ℃, is generally 1100 ℃, and pressure is 1.4 to 2.3MPa;
S305: make second flue gas enter internal combustion turbine 316 and start the turbine acting and drive generator for electricity generation; The temperature of finishing the 3rd flue gas of discharging from internal combustion turbine after the merit is 500 ℃ to 600 ℃, and pressure is 5000Pa to 6000Pa;
S306: make the 3rd flue gas enter first waste heat boiler 411 and obtain the middle superheated vapour of pressing, the middle pressure superheated vapour of pressing superheated vapour and step S106 to produce in described mixes and enters steam turbine 413 in the lump and generate electricity, and the opposing steam flow that comes out from steam turbine to vapourizing furnace for generation of original raw gas; Steam turbine in this step can be used for loading with vapour to satisfy according to extract steam out with the vapour grade; The middle pressure superheated vapour pressure that obtains in this step is 3.82MPa to 6.5MPa, and temperature is 450 ℃ to 520 ℃; The pressure of the steam that is back to vapourizing furnace that comes out from steam turbine in this step is 0.5MPa, and temperature is 210 ℃; In the present embodiment, generally the oiler feed of first waste heat boiler can be heated to 230 ℃;
S307: the 4th flue gas that comes out from first waste heat boiler 411 enters second waste heat boiler 412 and obtains low-pressure steam, and the low-pressure saturated steam in the described low-pressure steam enters deoxygenator and is used for boiler water deaeration; The pressure of the low-pressure saturated steam that produces in this step is 0.2MPa, and temperature is 132 ℃ of temperature of saturation;
S308: discharge by exhaust system 414 from the 5th flue gas that second waste heat boiler 412 comes out; The temperature of the 5th flue gas is about 130 ℃ in this step.
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 effective dedusting and desulfurization in advance handles to make then and carries out waste heat recovery after the gas to generate electricity acting and make it produce steam to load with vapour to satisfy, each technology among the present invention organically combines, synergy, the requirement that can satisfy industrial power load simultaneously and load with vapour; Method of the present invention is all recycled the waste that produces in each processing step on the other hand, and good economic benefits and social benefit are arranged; Moreover method of the present invention has been carried out dust removal process and desulfurization processing in advance to coal gas in use, the acting of can better generating electricity on the one hand of the coal gas that obtains like this, follow-uply on the other hand do not need to carry out the waste gas emission standard that off gas treatment can reach country, saved the off gas treatment expense, simultaneously can be to waste rational and efficient use wherein, energy-conserving and environment-protective.
In order to realize aforesaid method, referring to Fig. 1 to Fig. 3, normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment that the present invention also provides a kind of and aforesaid method to adapt, described equipment comprise that coal gas produces part, coal gas desulfurization part, gas to generate electricity part and gas heating part; Wherein coal gas is produced partly and is carried out dust removal process for the preparation of coal gas and to coal gas, coal gas desulfurization partly is used for coal gas is carried out the sulphur content that desulfurization handles to reduce coal gas, gas to generate electricity partly is used for use coal gas and generates electricity acting to satisfy industrial power load, and the high-temperature flue gas generation steam that gas heating partly is used for after the use generating carries out waste heat recovery to satisfy with the vapour load and to high-temperature flue gas; Its working process is that described coal gas is produced the first processing coal gas that makes of part and entered and carry out desulfurization after the coal gas desulfurization part and obtain desulfurization coal gas, and desulfurization coal gas enters and enters the gas heating part after gas to generate electricity partly generates electricity and further reclaim heat and steam is provided.
Preferable, 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 communicates with described vapourizing furnace 113 by the fuel inlet that is arranged on the described vapourizing furnace 113, described oxygen enriched air system 112 communicates with described vapourizing furnace 113 by the nozzle that is arranged on the vapourizing furnace 113, and described dreg removing system 114 is arranged on the bottom of described vapourizing furnace 113; Fuel, oxygen-rich air and in vapourizing furnace 113, produces original raw gas from the steam of gas heating part, the slag that vapourizing furnace 113 reaction backs produce is by dreg removing system 114 discharges;
Described cleaning apparatus comprises tornado dust collector 121 and first cleaning apparatus 122; Described tornado dust collector 121 communicate with described vapourizing furnace 113 by return line; Described heat reclamation device is first heat reclamation device 131;
Described original raw gas is undertaken obtaining first raw gas after the dedusting by tornado dust collector 121, first raw gas obtains second raw gas and middle pressure superheated vapour after entering first heat reclamation device 131, and described second raw gas obtains just handling coal gas after entering first cleaning apparatus 122.
Wherein, preferable, the fuel delivery system 111 in the present embodiment comprises coal bunker and fuel transfer roller, need add N when general coal is stored in the coal bunker
2(P=0.015Pa) protection, described fuel transfer roller is arranged on bottom and the described fuel transfer roller of coal bunker coal is sent into vapourizing furnace from the fuel inlet that is arranged on vapourizing furnace one side; Described fuel transfer roller can be for a plurality of according to design flow.
Wherein, preferable, first heat reclamation device 131 can be waste heat boiler (superheat section, evaporator section, economizer), and first cleaning apparatus 122 can be sack cleaner or electric precipitator.Vapourizing furnace can be the grace stove.
Wherein, preferable, the dreg removing system 114 in the present embodiment comprises the ash ejector that is arranged on the vapourizing furnace bottom and the ash bucket that is used for the storage slag, described slag needs to adopt steam to cool off after entering ash bucket, wherein ash ejector can be the spiral ash ejector, and quantity can be for a plurality of.Slag discharge process in the present embodiment continues to carry out, and the slag that enters ash bucket regularly pulls away discharging.
Preferable, 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 nozzle and second nozzle, first nozzle of the described first oxygen enrichment mixing tank and described vapourizing furnace is connected, second nozzle of the described second oxygen enrichment mixing tank and described vapourizing furnace is connected, and described first nozzle is arranged on the centrum portion of described vapourizing furnace; Described second nozzle is arranged on the top of described vapourizing furnace.Namely first nozzle is arranged on the close phase section of vapourizing furnace, and second nozzle is arranged on the dilute phase section of vapourizing furnace.The purpose that second nozzle is set is to add the secondary oxygen-rich air.
Preferable, as a kind of embodiment, first nozzle in the present embodiment is arranged on the below of fuel inlet, and the distance of first nozzle and described fuel inlet is 1.0 to 2.0 meters, and the angle between the central axis of described first nozzle and the central axis of described vapourizing furnace is 10 to 25 degree.In the present embodiment, can form 15 degree between the central axis of first nozzle and the central axis of vapourizing furnace to the elevation angle that makes progress of 17 degree, also can form the downward oblique angle about 21 degree, spray an easier and fuel mix of oxygen-rich air that enters like this, promote the fuel combustion reaction.The number of first nozzle in the present embodiment is 6, and these 6 first nozzles evenly are arranged on the vapourizing furnace.
Preferable, as a kind of embodiment, the central axis of described second nozzle is vertical with the central axis of described vapourizing furnace.Being the secondary oxygen-rich air enters in the vapourizing furnace from the horizontal direction of the body of heater of vapourizing furnace.The number of second nozzle in the present embodiment is 24, and the secondary oxygen-rich air enters in the vapourizing furnace from 24 second nozzles respectively after the second oxygen enrichment mixing tank comes out.
Preferable, as a kind of embodiment, the coal gas desulfurization in the present embodiment partly 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;
The described coal gas of processing just is hydrolyzed to handle by hydrolysis device 211 and obtains the 3rd coal gas, described the 3rd coal gas carries out the dedusting cooling by first refrigerating unit 212 and the gas-water separation processing obtains the 4th coal gas, described the 4th coal gas enters second cleaning apparatus 213 to carry out obtaining the 5th coal gas after the dust removal process, described the 5th coal gas obtains the 6th coal gas after entering increasing apparatus 214, described the 6th coal gas obtains the 7th coal gas after entering second refrigerating unit 215, described the 7th coal gas obtains the 8th coal gas after entering thionizer 216, described the 8th coal gas enters and obtains once desulfurization coal gas after refining plant 217 purifies, and described once desulfurization coal gas obtains secondary desulfurization coal gas after entering dry desulfurization device 218;
Described circulating water device is connected with second refrigerating unit 215 with described first refrigerating unit 212 respectively, and described recirculated water is back to circulating water device after circulating water device enters washing unit, first refrigerating unit and 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 the circulation water station, sprayed downwards by shower nozzle in the tower or nozzle, with the coal gas counter current contact, play the effect of cleaning and cooling off respectively, come out to be back to the circulation water station by the tower bottom then, and after circulating water treatment device is handled, recycle.
Preferable, as a kind of embodiment, the coal gas desulfurization part in the present embodiment also comprises doctor solution compounding system 219, 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 tank, 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 the solution Preparation tank, and the doctor solution in the 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 the sulphur foam chute, and described sulfur recovery unit is communicated with described lean solution groove;
According to the prescription of doctor solution the raw material adding doctor solution of doctor solution is prepared pump and make suitable doctor solution, the doctor solution that configures is kept in the solution Preparation tank, doctor solution enters top and the middle part of by desulfur pump doctor solution being delivered to thionizer behind the lean solution groove, doctor solution sprays from top to bottom, contact with back flow of gas, the hydrogen sulfide that absorbs in the gas obtains the doctor solution rich solution, described doctor solution rich solution enters regenerative pump after being gone out by the tower bottom flow of thionizer then, the liquid inlet of the injector that is arranged on the regeneration tank top delivered to the doctor solution rich solution by described regenerative pump, described doctor solution rich solution enters the regeneration tank bottom after the air of self-priming sprays by injector, airborne oxygen and doctor solution reaction in injector and regeneration tank, the sulphur foam that generates carries out sulfur recovery by top overflow to the sulfur recovery unit of regeneration tank, and the doctor solution lean solution after the regeneration enters the lean solution groove and recycles; Described sulphur foam filters to isolate sulphur foam and clear liquid by the pressurization of sulphur foam pump through filter, and the sulphur foam enters sulfur melting kettle and obtains Sulphur element slab 99.5, and described clear liquid flows into the lean solution groove and recycles.Raw material and the water regular replenishment of the loss of doctor solution institute.Wherein the raw material of doctor solution comprises alkali and tannin extract.
The doctor solution configuration-system of present embodiment setting is on the one hand in order to provide doctor solution to thionizer, and the doctor solution after using can be regenerated simultaneously the sulphur that absorbs to be extracted on the other hand obtains the sulphur product, has realized the maximum valueization of product.Doctor solution compounding system of the present invention is reused the purpose reached the conserve water resource after with desulfurization regeneration, can obtain the sulphur product simultaneously and make the waste that produces among the present invention have certain output value.
Further, the sulphur foam that enters the sulphur foam chute in the present embodiment is squeezed into filter by the sulphur foam pump, by filter separate sulfur foam and clear liquid; Clear liquid returns the lean solution groove, and the sulphur foam enters the continuous sulfur melting still, heats by jacket steam, melting down at 135 ℃ is the sulphur melt, lower part outlet by the continuous sulfur melting still enters the sulphur disc molding, and top solution flows into the solution receiving tank, sends into the lean solution groove by solution pump and recycles.
Preferable, as a kind of embodiment, the described gas to generate electricity in the present embodiment partly 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 and described air compressor 313 all are communicated with described burner 314, the exhanst gas outlet of described burner is communicated with described internal combustion turbine 316 by high-temperature flue gas passage 315, and described air compressor 313 is communicated with described high-temperature flue gas passage 315;
Secondary desulfurization coal gas adopts gas compressor 311 to carry out obtaining the 9th coal gas after the processed compressed, described the 9th coal gas enters burner 314, cooling air carries out obtaining filtrated air after the filtration treatment through air filter 312 after atmosphere sucks, described filtrated air enters air compressor 313 to carry out obtaining pressurized air after the processed compressed, the 9th coal gas and part pressurized air feed burner 314 and burning generation high-temperature flue gas in burner, described high-temperature flue gas obtains second flue gas in high-temperature flue gas passage 315 with after part pressurized air mixes, described second flue gas enters internal combustion turbine 316 and starts the turbine acting and drive generator for electricity generation.
The air of the secondary desulfurization coal gas of the process processed compressed in the present embodiment and process dedusting, processed compressed enters the high-temperature flue gas that burning obtains in the burner together and enters internal combustion turbine acting generating to satisfy industrial power load.The flue gas of finishing after the merit enters the gas heating part for generation of steam and further carries out UTILIZATION OF VESIDUAL HEAT IN.
Preferable, as a kind of embodiment, the described gas heating in the present embodiment partly comprises first waste heat boiler 411, second waste heat boiler 412, steam turbine 413 and exhaust system 414;
Wherein first waste heat boiler 411 is communicated with steam turbine 413, and second waste heat boiler 412 is communicated with deoxygenator, and first waste heat boiler 411 is communicated with second waste heat boiler 412, and second waste heat boiler 412 is communicated with exhaust system 414; Described steam turbine 413 is connected for delivery of steam with described vapourizing furnace 113;
The 3rd flue gas from internal combustion turbine 316 discharges after the generating enters first waste heat boiler 411 successively and discharge by exhaust system 414 second waste heat boiler, 412 backs, wherein first waste heat boiler 411 is pressed superheated vapour in producing, second waste heat boiler 412 produces low-pressure steam, the middle pressure superheated vapour that produces enters steam turbine 413, and the low-pressure steam that produces enters deoxygenator and is used for boiler supply water deaerating.First waste heat boiler in the present embodiment can be middle pressure waste heat boiler, and second waste heat boiler is the low pressure waste heat boiler.
Steam turbine in the present embodiment can be used for loading with vapour to satisfy according to extract steam out with the vapour grade.Low-pressure saturated steam in the described low-pressure steam enters deoxygenator and is used for boiler supply water deaerating, and that satisfies low-pressure steam uses the vapour demand.
Preferable, as a kind of embodiment, first heat reclamation device 131 that described coal gas is produced part also is communicated with described steam turbine 413, and namely the middle pressure superheated vapour that produces of first heat reclamation device also enters steam turbine.
Normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heating equipment can solve flue gas to the pollution problem of atmosphere, simultaneously can effectively utilize low grade coal again, can improve the heat energy utilization rate, and be well positioned to meet industrial electricity consumption and use the 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 with scale.
Adopt the acting in conjunction of wet method string dry method to remove inorganic sulfur, organosulfurs such as hydrogen sulfide in the coal gas, sulphur carbonoxide among the present invention, the sulphur content in the coal gas after the actual treatment is≤1mg/m
3Coal gas burns in internal combustion 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 discharging
3, SO
2≤ 400mg/Nm
3, NOx≤450mg/Nm
3Therefore normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method and equipment have absolute predominance in exhaust gas emission.
The mode that dust removal process among the present invention has adopted dry process and wet processing to combine uses dry process to have the decontamination effect improving of efficient stable on the one hand, handles its dustiness of back and is lower than 1mg/m
3Save water resources on the other hand, fundamentally be separated out the facility of gas mud and sewage disposal to the pollution of environment; Moreover equipment occupation of land of the present invention is little, and the conserve water resource is reduced 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, has realized the environmental friendliness operation, and dust removal installation level of automation height of the present invention, has reduced labour intensity.
The gas to generate electricity efficient height of normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method reaches as high as more than 58% at present.Be example with the 50MW of Steel Plant scale unit; the generating efficiency of normal pressure oxygen-enriched continuous gasification of the present invention-combined combustion and steam turbine power heat supply method can reach 40～46%; and only be about 23～30% with the Boiler Steam generating efficiency of scale, thermo-efficiency of the present invention exceeds more than 80%.The present invention has adopted the method for vapourizing furnace normal pressure oxygen-enriched continuous gasification to produce coal gas; adopt 50MW scale unit cogeneration; be example with melanism grace stove; it is 80% that coal gas is produced thermo-efficiency (thermo-efficiency=(coal gas lower heating value+useless pot producing steam enthalpy)/(going into stove coal lower calorific value+steam in the boiler enthalpy)); cogeneration efficient is 32～37%; with compare with scale Boiler Steam generating efficiency 23～30%, the thermo-efficiency of gas maked coal cogeneration exceeds 40% approximately.In addition, outer power supply mark of the present invention coal consumption is 395～480g/kwh, and the steam boiler mark coal consumption of powering outward is 430～500g/kwh.Save mark coal 20～35g/kwh.
The above embodiment has only expressed several embodiment of the present invention, and it describes comparatively concrete and detailed, but can not therefore be interpreted as the restriction to claim of the present invention.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 (10)
1. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heat supply method, it is characterized in that: described method comprises the steps:
S100: produce coal gas; Fuel, oxygen-rich air and steam are added vapourizing furnace respectively produce original raw gas, then original raw gas is carried out dedusting and lower the temperature to handle obtaining just handling coal gas;
S200: coal gas desulfurization: first processing coal gas is carried out the desulfurization processing obtain desulfurization coal gas;
S300: power generation and heat supply: will obtain high-temperature flue gas after desulfurization coal gas and the air feeding burner combustion, then high-temperature flue gas is handled back feeding internal combustion turbine startup turbine through hybrid cooling and do work to drive generator for electricity generation, finishing high-temperature flue gas after the merit presses in entering waste heat boiler to press superheated vapour in producing, pressing superheated vapour to enter steam turbine in described is used for being back to vapourizing furnace after the generating, the high-temperature flue gas of therefrom pressing waste heat boiler to come out enters the low pressure waste heat boiler and produces low-pressure steam, described low-pressure steam is that saturation steam is used for boiler supply water deaerating, and the low-temperature flue gas of discharging from the low pressure waste heat boiler directly enters atmosphere.
2. normal pressure oxygen-enriched continuous gasification according to claim 1-combined combustion and steam turbine power heat supply method, it is characterized in that: described step S100 comprises the steps:
S101: fuel is delivered into vapourizing furnace by fuel delivery system;
S102: the configuration oxygen concentration is 70% to 99.5% oxygen-rich air, and make oxygen-rich air enter the first oxygen enrichment mixing tank and the second oxygen enrichment mixing tank respectively, an oxygen-rich air that enters the first oxygen enrichment mixing tank enters vapourizing furnace by first nozzle, and the secondary oxygen-rich air that enters 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 burn in vapourizing furnace and form original raw gas; Then original raw gas is drawn by top of gasification furnace and enter tornado dust collector; This moment, the temperature of original raw gas was 950 ± 20 ℃;
S105: isolate flying dust in the original raw gas by tornado dust collector, obtain first raw gas through the dust removal process first time, and flying dust is returned vapourizing furnace further carry out second gasification; Wherein the temperature of first raw gas is 850 ± 20 ℃, and dustiness is 180 to 210g/m
3
S106: first raw gas is carried out waste heat recovery processing, obtain second raw gas, press superheated vapour in obtaining simultaneously; This moment, the temperature of second raw gas was 150 ± 10 ℃, and dustiness is 12 to 18g/m
3
S107: second raw gas is carried out handling coal gas at the beginning of the second time, dust removal process obtained, and just handling temperature of gas is 150 ℃, and dustiness is 75mg/m
3
3. normal pressure oxygen-enriched continuous gasification according to claim 1-combined combustion and steam turbine power heat supply method, it is characterized in that: described step S200 comprises the steps:
S201: to the processing that is hydrolyzed of first processing coal gas, the organic sulfide in the coal gas is converted into hydrogen sulfide, obtains the 3rd coal gas;
S202: the 3rd coal gas is carried out obtaining the 4th coal gas after dedusting cooling and gas-water separation are handled, and the 4th temperature of gas is 35 ± 5 ℃, and dustiness is 8 to 12mg/m
3, hydrogen sulfide content is 1400 to 1600mg/Nm
3
S203: the 4th coal gas is carried out wet desulphurization handle and to obtain once desulfurization coal gas, the equipment that wet desulphurization is adopted is thionizer, and the hydrogen sulfide content of once desulfurization coal gas is 40 to 60mg/Nm
3, temperature is 40 ± 5 ℃;
S204: adopt sweetening agent and sorbent material that once desulfurization coal gas is carried out the dry desulfurization processing and obtain secondary desulfurization coal gas, the hydrogen sulfide content of secondary desulfurization coal gas is less than 1mg/Nm
3
4. normal pressure oxygen-enriched continuous gasification according to claim 3-combined combustion and steam turbine power heat supply method, it is characterized in that: described step S203 comprises the steps:
S2031: the 4th coal gas is carried out dust removal process obtain the 5th coal gas, the dustiness of described the 5th coal gas is lower than 1mg/m
3
S2032: the 5th coal gas boosted to handle obtains the 6th coal gas, and the pressure of described the 6th coal gas is 10KPa, and temperature is 50 ± 5 ℃;
S2033: the 6th coal gas is carried out cooling process, obtain the 7th coal gas, described the 7th temperature of gas is 35 ℃;
S2034: adopt thionizer to carry out the wet desulphurization processing to the 7th coal gas and obtain the 8th coal gas, thionizer has absorbed the hydrogen sulfide in the 7th coal gas;
S2035: the 8th coal gas is carried out purifying treatment, remove fine dust, elaioleucite, sulphur foam in the coal gas, obtain once desulfurization coal gas.
5. normal pressure oxygen-enriched continuous gasification according to claim 1-combined combustion and steam turbine power heat supply method, it is characterized in that: described step S300 comprises the steps:
S301: secondary desulfurization coal gas is carried out processed compressed obtain the 9th coal gas, and the 9th coal gas is fed burner; The pressure of the 9th coal gas is 1.5 to 2.4MPa, and temperature is 350 ± 10 ℃;
S302: air is carried out obtaining pressurized air after dust removal process and the processed compressed, and part pressurized air is fed burner; Compressed-air actuated dustiness is lower than 1mg/m
3, pressure is 1.5 to 2.4MPa;
S303: the 9th coal gas and pressurized air burn in burner and produce high-temperature flue gas; The temperature of high-temperature flue gas is 1600 ± 50 ℃;
S304: high-temperature flue gas mixed obtaining second flue gas with rest part pressurized air, the temperature of second flue gas is 1100 ± 50 ℃, and pressure is 1.4 to 2.3MPa;
S305: make second flue gas enter internal combustion turbine and start the turbine acting and drive generator for electricity generation; The temperature of finishing the 3rd flue gas of discharging from internal combustion turbine after the merit is 500 to 600 ℃, and pressure is 5000 to 6000Pa;
S306: make the 3rd flue gas enter first waste heat boiler and press superheated vapour in obtaining, press superheated vapour to enter steam turbine in described and generate electricity, the opposing steam flow that comes out from steam turbine is to vapourizing furnace;
S307: the 4th flue gas that comes out from first waste heat boiler enters second waste heat boiler and obtains low-pressure steam, and described low-pressure steam is that saturated low-pressure steam is supplied with deoxygenator and is used for boiler supply water deaerating;
S308: discharge from the 5th flue gas that second waste heat boiler comes out.
6. normal pressure oxygen-enriched continuous gasification-combined combustion and steam turbine power heating equipment is characterized in that: described equipment comprises that coal gas produces part, coal gas desulfurization part, gas to generate electricity part and gas heating part:
Described coal gas is produced the first processing coal gas that makes of part and is entered and carry out desulfurization after the coal gas desulfurization part and obtain desulfurization coal gas, and desulfurization coal gas enters and enters the gas heating part after gas to generate electricity partly generates electricity and further reclaim heat and steam is provided.
7. normal pressure oxygen-enriched continuous gasification according to claim 6-combined combustion and steam turbine power heating equipment is characterized in that: 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 communicates with described vapourizing furnace by the fuel inlet that is arranged on the described vapourizing furnace, and described oxygen enriched air system communicates with described vapourizing furnace by the nozzle that is arranged on the vapourizing furnace, and described dreg removing system is arranged on the bottom of described vapourizing furnace; Fuel, oxygen-rich air and in vapourizing furnace, produce original raw gas from the steam of gas heating part;
Described cleaning apparatus comprises tornado dust collector and first cleaning apparatus; Described tornado dust collector communicate with described vapourizing furnace by return line;
Described heat reclamation device comprises first heat reclamation device;
Described original raw gas is undertaken obtaining first raw gas after the dedusting by tornado dust collector, and first raw gas obtains second raw gas and middle pressure superheated vapour after entering first heat reclamation device, and second raw gas obtains just handling coal gas after entering first cleaning apparatus.
8. normal pressure oxygen-enriched continuous gasification according to claim 7-combined combustion and steam turbine power heating equipment, it is characterized in that: 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 nozzle and second nozzle, first nozzle of the described first oxygen enrichment mixing tank and described vapourizing furnace is connected, second nozzle of the described second oxygen enrichment mixing tank and described vapourizing furnace is connected, and described first nozzle is arranged on the centrum portion of described vapourizing furnace; Described second nozzle is arranged on the top of described vapourizing furnace.
9. normal pressure oxygen-enriched continuous gasification according to claim 8-combined combustion and steam turbine power heating equipment, it is characterized in that: described first nozzle is arranged on the below of described fuel inlet, the distance of described first nozzle and described fuel inlet is 1.0 to 2.0 meters, and the angle between the central axis of described first nozzle and the central axis of described vapourizing furnace is 10 to 25 degree.
10. normal pressure oxygen-enriched continuous gasification according to claim 6-combined combustion and steam turbine power heating equipment, it is characterized in that: described coal gas desulfurization partly comprises hydrolysis device, first refrigerating unit, second cleaning apparatus, increasing apparatus, second refrigerating unit, thionizer, refining plant, dry desulfurization device and circulating water device;
Hydrolysis device, first refrigerating unit, second cleaning apparatus, increasing apparatus, second refrigerating unit, thionizer, refining plant, dry desulfurization device connect successively; Wherein be provided with sweetening agent and sorbent material in the dry desulfurization device;
The described coal gas of processing just is hydrolyzed to handle by hydrolysis device and obtains the 3rd coal gas, described the 3rd coal gas carries out the dedusting cooling by first refrigerating unit and the gas-water separation processing obtains the 4th coal gas, described the 4th coal gas enters second cleaning apparatus to carry out obtaining the 5th coal gas after the dust removal process, described the 5th coal gas obtains the 6th coal gas after entering increasing apparatus, described the 6th coal gas obtains the 7th coal gas after entering second refrigerating unit, described the 7th coal gas obtains the 8th coal gas after entering thionizer, described the 8th coal gas enters and obtains once desulfurization coal gas after refining plant purifies, and described once desulfurization coal gas obtains secondary desulfurization coal gas after entering dry desulfurization device;
Described circulating water device is connected with second refrigerating unit with described first refrigerating unit respectively, and described recirculated water is back to circulating water device after circulating water device enters first refrigerating unit and second refrigerating unit respectively.
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Address after: 101318 No. 5 Anxiang Road, Area B, Tianzhu Airport Industrial Zone, Shunyi District, Beijing, 1 Building, 4 Floors Patentee after: Bluestar Engineering Co., Ltd. Address before: 100143 No. 19 Fushi Road, Haidian District, Beijing Patentee before: Haohua Engineering Co., Ltd. |