CN111156535A - Double fluidized bed pyrolysis combustion waste heat utilization system and method - Google Patents
Double fluidized bed pyrolysis combustion waste heat utilization system and method Download PDFInfo
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 105
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 35
- 239000002918 waste heat Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 12
- 239000003245 coal Substances 0.000 claims abstract description 113
- 239000007789 gas Substances 0.000 claims abstract description 82
- 239000003034 coal gas Substances 0.000 claims abstract description 75
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000003546 flue gas Substances 0.000 claims abstract description 64
- 239000000428 dust Substances 0.000 claims abstract description 26
- 238000010248 power generation Methods 0.000 claims abstract description 21
- 239000000463 material Substances 0.000 claims abstract description 7
- 238000010926 purge Methods 0.000 claims abstract description 7
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 4
- 230000023556 desulfurization Effects 0.000 claims abstract description 4
- 239000002956 ash Substances 0.000 claims description 21
- 230000003009 desulfurizing effect Effects 0.000 claims description 20
- 238000000746 purification Methods 0.000 claims description 19
- 238000003860 storage Methods 0.000 claims description 14
- 230000009977 dual effect Effects 0.000 claims description 8
- 239000000843 powder Substances 0.000 claims description 7
- 238000000605 extraction Methods 0.000 claims description 5
- 239000010883 coal ash Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000012806 monitoring device Methods 0.000 claims 1
- 239000000779 smoke Substances 0.000 abstract description 6
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 abstract description 4
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract 2
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
- C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
- C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
- F01K17/02—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G1/00—Steam superheating characterised by heating method
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L9/00—Passages or apertures for delivering secondary air for completing combustion of fuel
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
- F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/20—Sulfur; Compounds thereof
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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
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- General Chemical & Material Sciences (AREA)
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention relates to a double fluidized bed pyrolysis combustion waste heat utilization system and method, and aims to solve the technical problems of waste heat loss, low system efficiency and environmental pollution in a double fluidized bed pyrolysis combustion system. The system mainly comprises a circulating fluidized bed power generation system and a coal pyrolysis system, wherein a raw coal preheater of the coal pyrolysis system is used as a heat source by hot smoke gas after a dust remover, and the smoke gas after heat release is used as secondary air to return to a boiler; and one part of steam from the high-temperature superheater outlet of the coal pyrolysis system is used for heating flue gas at the outlet of a desulfurization tower of the power generation system, the other part of the steam is used for heating circulating coal gas of the pyrolysis system, and the released steam is used as steam sources for purging, heat tracing, material conveying and the like of other equipment pipelines of the pyrolysis system. The invention combines the waste heat utilization of the circulating fluidized bed power generation system and the coal pyrolysis system, reduces the smoke discharge loss, improves the efficiency of the combustion furnace and the pyrolysis furnace, reduces the generation amount of phenol-containing wastewater and improves the pyrolysis efficiency.
Description
Technical Field
The invention belongs to the fields of thermal power generation technology and coal pyrolysis technology, and particularly relates to a double fluidized bed pyrolysis combustion waste heat utilization system and method.
Background
In recent years, the country emphatically encourages a technology of grading, quality-grading, converting, cleaning and efficiently utilizing the inferior coal, wherein a circulating fluidized bed power generation system and a fluidized bed pyrolysis system are coupled to realize the joint production of heat, electricity, gas and tar in one system. The overall benefit optimization of the coal utilization system is realized, and the utilization value and the utilization benefit of the inferior bituminous coal are greatly improved.
In the double fluidized bed pyrolysis combustion system, although the coal is utilized in a quality-divided and grading manner, a certain residual heat loss is inevitable. The heat loss of the exhaust gas of the fluidized bed combustion boiler accounts for about 80% of the total heat loss of the boiler, the exhaust gas temperature is generally 120-150 ℃, the exhaust gas amount is large, and the waste heat utilization value is large. A large amount of high-temperature superheated steam generated in a pyrolysis system is usually only used for pipeline purging, heat tracing, material conveying and the like, and a phenomenon that a large amount of high-quality steam sources are not reasonably utilized exists. Meanwhile, normal-temperature pulverized coal and circulating coal gas directly enter the high-temperature pyrolysis furnace without preheating in the double-fluidized-bed pyrolysis combustion system, the temperature of a combustion boiler and the temperature of a pyrolysis furnace bed are inevitably reduced, the combustion efficiency of the boiler, the pyrolysis efficiency of the pulverized coal and the quality of pyrolysis gas are influenced, and the efficiency of the whole system is reduced. In the system, a large amount of water vapor enters the atmosphere along with the flue gas in the process of wet desulphurization by the exhaust gas of the power generation boiler, and a large amount of white smoke is generated to cause environmental pollution and bring adverse effects to peripheral production and life.
Disclosure of Invention
The invention aims to solve the technical problems of waste heat loss, low system efficiency and environmental pollution in a double fluidized bed pyrolysis combustion system, and provides a double fluidized bed pyrolysis combustion waste heat utilization system and method.
In order to solve the technical problems, the invention adopts the technical scheme that:
a double fluidized bed pyrolysis combustion waste heat utilization system comprises a circulating fluidized bed power generation system and a coal pyrolysis system; the circulating fluidized bed power generation system comprises a boiler, a separator, an air preheater, a dust remover, a desulfurizing tower, a first steam-gas heat exchanger and a chimney, wherein a flue gas outlet of the boiler is connected with a flue gas inlet of the separator through a pipeline, an ash outlet of the separator is connected with a hearth of the boiler through a pipeline, a flue gas outlet of the separator is connected with a flue gas inlet of the air preheater through a pipeline, a flue gas outlet of the air preheater is connected with a flue gas inlet of the dust remover through a pipeline, a flue gas outlet of the dust remover is connected with a flue gas inlet of the desulfurizing tower through a pipeline, a flue gas outlet of the desulfurizing tower is connected with a flue gas inlet of the first steam-gas heat exchanger through a pipeline, and a flue gas outlet of the first steam-gas heat exchanger is connected with a flue gas inlet of the chimney through a pipeline;
the coal pyrolysis system consists of a pyrolysis furnace, a high-temperature superheater, a coal gas coarse purification unit, a coal bunker, a raw coal preheater, an intermediate coal storage bunker, a spiral coal feeder, a second steam-gas heat exchanger, a circulating fan and a coal gas post-treatment system; the coal bunker discharge port is connected with a raw coal preheater coal powder inlet through a pipeline, a raw coal preheater coal powder outlet is connected with a middle coal storage bunker feed port through a pipeline, a middle coal storage bunker discharge port is connected with a spiral coal feeder feed port through a pipeline, a spiral coal feeder discharge port is connected with a pyrolysis furnace feed port through a pipeline, a pyrolysis furnace ash inlet is connected with a separator ash outlet through a pipeline, and a pyrolysis furnace ash outlet is connected with a boiler ash inlet through a pipeline;
the coal gas outlet of the pyrolysis furnace is connected with the coal gas inlet of the high-temperature superheater through a pipeline, the coal gas outlet of the high-temperature superheater is connected with the coal gas inlet of the coal gas rough purification unit through a pipeline, one path of the coal gas outlet of the coal gas rough purification unit is connected with a coal gas post-treatment system through a pipeline, the other path of the coal gas outlet of the coal gas rough purification unit is connected with the coal gas inlet of a second steam-gas heat exchanger through a circulating fan, and the coal gas outlet of the second steam-gas heat exchanger is connected with the coal gas inlet of the pyrolysis furnace;
a high-temperature steam inlet of the high-temperature superheater is connected with a steam extraction outlet of a four-section steam turbine of the circulating fluidized bed power generation system, one path of a high-temperature steam outlet of the high-temperature superheater is connected with a steam inlet of the first steam-gas heat exchanger through a pipeline, and the other path of the high-temperature steam outlet of the high-temperature superheater is connected with a steam inlet of the second steam-gas heat exchanger through a pipeline;
the flue gas inlet of the raw coal preheater is connected with the flue gas outlet of the dust remover through a pipeline, and the flue gas outlet of the raw coal preheater is connected with the secondary air inlet of the boiler through a pipeline.
And furthermore, a third induced draft fan is arranged on a connecting pipeline between the dust remover and the desulfurizing tower.
Furthermore, a first temperature on-line monitor is arranged on a connecting pipeline of the first steam-gas heat exchanger and the chimney, and a first adjusting door is arranged on a connecting pipeline of the high-temperature superheater and the first steam-gas heat exchanger.
Furthermore, a second adjusting door is arranged on a connecting pipeline of the high-temperature superheater and the second steam-gas heat exchanger, and a second temperature on-line monitor is arranged on a connecting pipeline of the second steam-gas heat exchanger and the pyrolysis furnace.
And furthermore, a second induced draft fan is arranged on a connecting pipeline between the dust remover and the raw coal preheater.
Furthermore, a first induced draft fan is arranged on a connecting pipeline between the raw coal preheater and the boiler.
Further, the raw coal preheater is a fluidized bed preheater.
A double fluidized bed pyrolysis combustion waste heat utilization method comprises the following steps:
hot flue gas generated by a boiler enters a separator for treatment, the flue gas treated by the separator enters an air preheater for preheating primary air and secondary air, then enters a dust remover for dust removal, then enters a desulfurizing tower for desulfurization, then enters a first steam-gas heat exchanger for heat exchange, and finally enters a chimney for emission; part of the high-temperature ash generated by the separator enters a hearth of the boiler, and the other part of the high-temperature ash enters the pyrolysis furnace for pyrolysis, and clean coal ash generated after pyrolysis by the pyrolysis furnace enters the boiler again for combustion and power generation; wherein, part of the high-temperature flue gas dedusted by the deduster enters the raw coal preheater through a second induced draft fan to be used as a heat source, and the flue gas utilized by the raw coal preheater is introduced into the boiler through the first induced draft fan to be used as secondary air;
coal powder in the coal bunker enters a raw coal preheater for preheating and then enters a middle coal storage bunker, then enters a pyrolysis furnace through a spiral coal feeder for pyrolysis, hot coal gas generated by the pyrolysis furnace enters a high-temperature superheater for cooling, the cooled coal gas enters a coal gas coarse purification unit for purification, one part of the purified coal gas enters a second steam-gas heat exchanger through a circulating fan and then enters the pyrolysis furnace as a fluidizing medium of the pyrolysis furnace, and the other part of the purified coal gas enters a coal gas post-treatment system for treatment;
one part of high-temperature steam generated by the high-temperature superheater enters a first steam-gas heat exchanger to exchange heat with outlet flue gas of the desulfurizing tower, and the other part of high-temperature steam enters a second steam-gas heat exchanger to heat circulating coal gas entering the pyrolyzing furnace; the steam generated after the heat release of the first steam-gas heat exchanger and the second steam-gas heat exchanger is used for purging pipelines of other equipment in the coal pyrolysis system, heat tracing and a material conveying steam source.
Further, the method for utilizing the waste heat of the double fluidized bed pyrolysis combustion further comprises the following steps of:
setting the flue gas temperature of a first temperature online monitor to be 80 ℃, and automatically adjusting the size of a valve by a first adjusting valve according to the temperature monitored by the first temperature online monitor so as to adjust the amount of steam entering a first steam-gas heat exchanger;
the second temperature on-line monitor monitors the temperature of the circulating coal gas entering the pyrolysis furnace in real time, and the second adjusting valve automatically adjusts the size of the valve according to the temperature monitored by the second temperature on-line monitor, so that the amount of steam entering the second steam-gas heat exchanger is adjusted.
Further, the steam of the high-temperature superheater comes from a four-section steam extraction of a steam turbine of the circulating fluidized bed power generation system.
Compared with the prior art, the invention has the following advantages and beneficial effects:
1. the invention preheats the raw coal entering the pyrolysis furnace by utilizing the waste heat of the hot flue gas of the combustion furnace, on one hand, the heat loss of the exhaust gas can be reduced, the thermal efficiency of the combustion furnace is improved, on the other hand, the heat absorption capacity of the pulverized coal in the pyrolysis furnace can be reduced, the thermal efficiency of the pyrolysis furnace is improved, and particularly, in winter, the coal as fired can be unfrozen, the moisture in the coal is reduced, and the physical sensible heat of the coal as.
2. The high-temperature steam heats the flue gas at the outlet of the desulfurizing tower and then is used as a steam source for other equipment, pipeline purging, heat tracing, material conveying and the like of the coal pyrolysis system, so that the aim of gradient utilization of the waste heat of the steam is fulfilled, and white smoke at the outlet of a chimney can be eliminated.
3. According to the invention, after circulating coal gas required by the high-temperature steam preheating pyrolysis furnace is subjected to pipeline purging, heat tracing, material conveying and the like, the heat absorption capacity of the coal gas entering the pyrolysis furnace is reduced, the thermal efficiency of the pyrolysis furnace is improved, and the cascade utilization of energy is realized.
4. The raw coal preheater is a fluidized bed preheater, the flue gas is used as a fluidizing medium, and the coal is in direct contact with the flue gas in a fluidized state for rapid heat exchange to remove most of water in the coal, so that the phenolic wastewater generated by a coal pyrolysis system is greatly reduced, and the phenolic wastewater treatment cost is reduced.
5. The flue gas from the raw coal preheater is fed into the combustion furnace as secondary air, so that the oxygen content of the combustion furnace can be effectively reduced, and the reduction of NO is realizedXEffect on production amount.
Drawings
FIG. 1 is a schematic structural view of the present invention;
in the figure, a boiler-1, an air preheater-2, a dust remover-3, a desulfurizing tower-4, a first steam-gas heat exchanger-5, a chimney-6, a pyrolysis furnace-7, a high-temperature superheater-8, a coal gas coarse purification unit-9, a coal bunker-10, a raw coal preheater-11, an intermediate coal storage bunker-12, a spiral coal feeder-13, a second steam-gas heat exchanger-14, a circulating fan-15, a first induced draft fan-16, a second induced draft fan-17, a third induced draft fan-18, a first adjusting door-19, a first temperature on-line monitor-20, a second adjusting door-21, a second temperature on-line monitor-22, a separator-23 and a coal gas post-treatment system-24 are arranged.
Detailed Description
The invention is further illustrated by the following figures and examples.
As shown in fig. 1, the system for utilizing waste heat from dual fluidized bed pyrolysis combustion in the embodiment includes a circulating fluidized bed power generation system and a coal pyrolysis system; the circulating fluidized bed power generation system comprises a boiler 1, a separator 23, an air preheater 2, a dust remover 3, a desulfurizing tower 4, a first steam-gas heat exchanger 5 and a chimney 6, wherein the separator 23 is a cyclone separator, a flue gas outlet of the boiler 1 is connected with a flue gas inlet of the separator 23 through a pipeline, an ash outlet of the separator 23 is connected with a hearth of the boiler 1 through a pipeline, a flue gas outlet of the separator 23 is connected with a flue gas inlet of the air preheater 2 through a pipeline, a flue gas outlet of the air preheater 2 is connected with a flue gas inlet of the dust remover 3 through a pipeline, a flue gas outlet of the dust remover 3 is connected with a flue gas inlet of the desulfurizing tower 4 through a pipeline, a flue gas outlet of the desulfurizing tower 4 is connected with a flue gas inlet of the first steam-gas heat exchanger 5 through a pipeline, a flue gas outlet of the first steam-gas heat exchanger 5 is connected with a flue gas inlet of the chimney 6 through a pipeline, and a third induced draft fan 18 is arranged on a connecting pipeline of the dust remover 3 and the desulfurizing tower 4.
The coal pyrolysis system consists of a pyrolysis furnace 7, a high-temperature superheater 8, a coal gas coarse purification unit 9, a coal bunker 10, a raw coal preheater 11, an intermediate coal storage bunker 12, a spiral coal feeder 13, a second steam-gas heat exchanger 14, a circulating fan 15 and a coal gas post-treatment system 24; the discharge gate of coal bunker 10 passes through the pipe connection with 11 buggy entrys of raw coal preheater, the buggy export of raw coal preheater 11 passes through the pipe connection with the feed inlet of middle coal storage bunker 12, the discharge gate of middle coal storage bunker 12 passes through the pipe connection with the feed inlet of spiral coal feeder 13, the discharge gate of spiral coal feeder 13 passes through the pipe connection with the feed inlet of pyrolysis oven 7, the ash inlet of pyrolysis oven 7 passes through the pipe connection with the ash outlet of separator 23, the lime-ash export of pyrolysis oven 7 passes through the pipe connection with the lime-ash import of boiler 1 and connects, middle coal storage bunker 12 and spiral coal feeder 13 and relevant pipe-line system all have made heat preservation measure.
A coal gas outlet of the pyrolysis furnace 7 is connected with a coal gas inlet of a high-temperature superheater 8 through a pipeline, a coal gas outlet of the high-temperature superheater 8 is connected with a coal gas inlet of a coal gas rough purification unit 9 through a pipeline, one path of the coal gas outlet of the coal gas rough purification unit 9 is connected with a coal gas post-treatment system 24 through a pipeline, the other path of the coal gas outlet of the coal gas rough purification unit 9 is connected with a coal gas inlet of a second steam-gas heat exchanger 14 through a circulating fan 15, and a coal gas outlet of the second steam-gas heat exchanger 14 is connected with a coal gas inlet of the pyrolysis furnace 7;
a high-temperature steam inlet of the high-temperature superheater 8 is connected with a steam extraction outlet of a four-section steam turbine of the circulating fluidized bed power generation system, one path of a high-temperature steam outlet of the high-temperature superheater 8 is connected with a steam inlet of the first steam-gas heat exchanger 5 through a pipeline, and the other path of the high-temperature steam outlet of the high-temperature superheater 8 is connected with a steam inlet of the second steam-gas heat exchanger 14 through a pipeline;
raw coal preheater 11 is the fluidized bed preheater, and the buggy directly contacts the heat transfer with the hot flue gas that gets into the fluidized bed preheater, and heat exchange efficiency is high, is favorable to the desorption of moisture in the coal, and then the production of the pyrolysis system phenol-containing waste water that has significantly reduced. The flue gas inlet of raw coal preheater 11 passes through the pipe connection with the exhanst gas outlet of dust remover 3, be equipped with second draught fan 17 on the connecting line of dust remover 3 and raw coal preheater 11, the exhanst gas outlet of raw coal preheater 11 passes through the pipe connection with boiler 1's overgrate air entry, be equipped with first draught fan 16 on raw coal preheater 11 and boiler 1's the connecting line.
The first induced draft fan-16, the second induced draft fan-17 and the third induced draft fan-18 can be adjusted in a variable speed mode.
A first temperature on-line monitor 20 is arranged on a connecting pipeline of the first steam-gas heat exchanger 5 and the chimney 6, and a first adjusting door 19 is arranged on a connecting pipeline of the high-temperature superheater 8 and the first steam-gas heat exchanger 5.
And a second adjusting door 21 is arranged on a connecting pipeline of the high-temperature superheater 8 and the second steam-gas heat exchanger 14, and a second temperature on-line monitor 22 is arranged on a connecting pipeline of the second steam-gas heat exchanger 14 and the pyrolysis furnace 7.
The double fluidized bed pyrolysis combustion waste heat utilization method comprises the following steps:
the hot flue gas generated by the boiler 1 enters a separator 23 for treatment, the flue gas treated by the separator 23 enters an air preheater 2 for preheating primary air and secondary air, and then enters the air preheaterThe waste gas enters a dust remover 3 for dust removal, then enters a desulfurizing tower 4 for desulfurization, then enters a first steam-gas heat exchanger 5 for heat exchange, and finally enters a chimney 6 for discharge; part of the high-temperature ash generated by the separator 23 enters a hearth of the boiler 1, and the other part of the high-temperature ash enters the pyrolysis furnace 7 as a high-temperature heat source, and clean coal ash generated after raw coal is pyrolyzed by the pyrolysis furnace 7 enters the boiler 1 again for combustion and power generation; wherein, part of the high-temperature flue gas with the temperature of 120-150 ℃ after being dedusted by the deduster 3 enters the raw coal preheater 11 through the second induced draft fan 17 to be used as a heat source, and the flue gas utilized by the raw coal preheater 11 is introduced into the boiler 1 through the first induced draft fan 16 to be used as secondary air, thus the waste heat of the hot flue gas can be utilized, the smoke discharge loss is reduced, the heat efficiency of the combustion furnace is improved, the oxygen content entering the combustion furnace can be reduced, and the NO is reducedXAnd (4) discharging the amount.
Coal powder in a coal bunker 10 enters a raw coal preheater 11 for preheating, then enters an intermediate coal storage bunker 12, then enters a pyrolysis furnace 7 through a spiral coal feeder 13 for pyrolysis, hot coal gas generated by the pyrolysis furnace 7 enters a high-temperature superheater 8 for cooling, the cooled coal gas enters a coal gas coarse purification unit 9 for purification, one part of the purified coal gas enters a second steam-gas heat exchanger 14 through a circulating fan 15, then enters the pyrolysis furnace 7 as a fluidizing medium of the pyrolysis furnace 7, and the other part of the purified coal gas enters a coal gas post-treatment system 23 for treatment;
the steam of the high-temperature superheater 8 is extracted from the four sections of a steam turbine of the circulating fluidized bed power generation system. One part of high-temperature steam with the temperature of about 500 ℃ generated by the high-temperature superheater 8 enters the first steam-gas heat exchanger 5 to exchange heat with the outlet flue gas of the desulfurizing tower 4, and the other part of the high-temperature steam enters the second steam-gas heat exchanger 14 to heat the circulating coal gas entering the pyrolyzing furnace 7; the steam generated after the heat release of the first steam-gas heat exchanger 5 and the second steam-gas heat exchanger 14 is used as a steam source for purging, heat tracing and material conveying of other equipment pipelines in the coal pyrolysis system.
The steam amount entering the first steam-gas heat exchanger 5 can be adjusted and turned off through the first adjusting door 19 and the first temperature on-line monitor 20, and the first temperature on-line monitor 20 can monitor the temperature of the steam entering the first steam-gas heat exchanger 5 in real time. Firstly, setting the flue gas temperature of a first temperature online monitor 20 to be 80 ℃, and automatically adjusting the size of a valve by a first adjusting valve 19 according to the temperature monitored by the first temperature online monitor 20 so as to adjust the amount of steam entering a first steam-gas heat exchanger 5;
the steam amount entering the second steam-gas heat exchanger 14 can be adjusted and shut off through a second adjusting door 21 and a second temperature on-line monitor 22, and the second temperature on-line monitor 22 can monitor the temperature of the circulating coal gas entering the pyrolysis furnace 7 in real time. The second adjusting valve 21 can automatically adjust the size of the valve according to the temperature monitored by the second online temperature monitor 22, so as to adjust the amount of steam entering the second steam-gas heat exchanger 14.
Claims (10)
1. The utility model provides a double fluidized bed pyrolysis combustion waste heat utilization system which characterized in that: comprises a circulating fluidized bed power generation system and a coal pyrolysis system; circulating fluidized bed power generation system comprises boiler (1), separator (23), air preheater (2), dust remover (3), desulfurizing tower (4), first vapour gas heat exchanger (5) and chimney (6), the exhanst gas outlet of boiler (1) passes through the pipe connection with the flue gas entry of separator (23), the ash export of separator (23) passes through the pipe connection with the furnace of boiler (1), the exhanst gas outlet of separator (23) passes through the pipe connection with the flue gas inlet of air preheater (2), the exhanst gas outlet of air preheater (2) passes through the pipe connection with the flue gas inlet of dust remover (3), the exhanst gas outlet of dust remover (3) passes through the pipe connection with the flue gas inlet of desulfurizing tower (4), the exhanst gas outlet of desulfurizing tower (4) passes through the pipe connection with the flue gas inlet of first vapour gas heat exchanger (5), the exhanst gas outlet of first vapour gas heat exchanger (5) passes through the pipe connection with the flue gas inlet of chimney (6) through the pipe connection Connecting;
the coal pyrolysis system consists of a pyrolysis furnace (7), a high-temperature superheater (8), a coal gas coarse purification unit (9), a coal bunker (10), a raw coal preheater (11), an intermediate coal storage bunker (12), a spiral coal feeder (13), a second steam-gas heat exchanger (14), a circulating fan (15) and a coal gas post-treatment system (24); the coal bunker is characterized in that a discharge port of the coal bunker (10) is connected with a coal powder inlet of a raw coal preheater (11) through a pipeline, a coal powder outlet of the raw coal preheater (11) is connected with a feed port of an intermediate coal storage bunker (12) through a pipeline, a discharge port of the intermediate coal storage bunker (12) is connected with a feed port of a spiral coal feeder (13) through a pipeline, a discharge port of the spiral coal feeder (13) is connected with a feed port of a pyrolysis furnace (7) through a pipeline, an ash inlet of the pyrolysis furnace (7) is connected with an ash outlet of a separator (23) through a pipeline, and an ash outlet of the pyrolysis furnace (7) is connected with an ash inlet of a boiler (1) through a pipeline;
a coal gas outlet of the pyrolysis furnace (7) is connected with a coal gas inlet of a high-temperature superheater (8) through a pipeline, a coal gas outlet of the high-temperature superheater (8) is connected with a coal gas inlet of a coal gas rough purification unit (9) through a pipeline, one path of the coal gas outlet of the coal gas rough purification unit (9) is connected with a coal gas post-treatment system (24) through a pipeline, the other path of the coal gas outlet of the coal gas rough purification unit (9) is connected with a coal gas inlet of a second steam-gas heat exchanger (14) through a circulating fan (15), and a coal gas outlet of the second steam-gas heat exchanger (14) is connected with a coal gas inlet of the pyrolysis furnace (7);
a high-temperature steam inlet of the high-temperature superheater (8) is connected with a steam extraction outlet of a four-section steam turbine of the circulating fluidized bed power generation system, one path of a high-temperature steam outlet of the high-temperature superheater (8) is connected with a steam inlet of the first steam-gas heat exchanger (5) through a pipeline, and the other path of the high-temperature steam outlet of the high-temperature superheater (8) is connected with a steam inlet of the second steam-gas heat exchanger (14) through a pipeline;
the flue gas inlet of the raw coal preheater (11) is connected with the flue gas outlet of the dust remover (3) through a pipeline, and the flue gas outlet of the raw coal preheater (11) is connected with the secondary air inlet of the boiler (1) through a pipeline.
2. The dual fluidized bed pyrolysis combustion waste heat utilization system of claim 1, characterized in that: and a third induced draft fan (18) is arranged on a connecting pipeline of the dust remover (3) and the desulfurizing tower (4).
3. The dual fluidized bed pyrolysis combustion waste heat utilization system of claim 1, characterized in that: the high-temperature online monitoring device is characterized in that a first temperature online monitor (20) is arranged on a connecting pipeline of the first steam-gas heat exchanger (5) and the chimney (6), and a first adjusting door (19) is arranged on a connecting pipeline of the high-temperature superheater (8) and the first steam-gas heat exchanger (5).
4. The dual fluidized bed pyrolysis combustion waste heat utilization system of claim 1, characterized in that: and a second adjusting door (21) is arranged on a connecting pipeline of the high-temperature superheater (8) and the second steam-gas heat exchanger (14), and a second temperature on-line monitor (22) is arranged on a connecting pipeline of the second steam-gas heat exchanger (14) and the pyrolysis furnace (7).
5. The dual fluidized bed pyrolysis combustion waste heat utilization system of claim 1, characterized in that: and a second draught fan (17) is arranged on a connecting pipeline between the dust remover (3) and the raw coal preheater (11).
6. The dual fluidized bed pyrolysis combustion waste heat utilization system of claim 1, characterized in that: and a first induced draft fan (16) is arranged on a connecting pipeline between the raw coal preheater (11) and the boiler (1).
7. The dual fluidized bed pyrolysis combustion waste heat utilization system of claim 1, characterized in that: the raw coal preheater (11) is a fluidized bed preheater.
8. The method for utilizing the waste heat of the dual fluidized bed pyrolysis combustion in the claims 1-7 is characterized by comprising the following steps of:
hot flue gas generated by a boiler (1) enters a separator (23) for treatment, the flue gas treated by the separator (23) enters an air preheater (2) for preheating primary air and secondary air, then enters a dust remover (3) for dust removal, then enters a desulfurizing tower (4) for desulfurization, then enters a first steam-gas heat exchanger (5) for heat exchange, and finally enters a chimney (6) for discharge; part of high-temperature ash generated by the separator (23) enters a hearth of the boiler (1), part of high-temperature ash enters the pyrolysis furnace (7) for pyrolysis, and clean coal ash generated after pyrolysis by the pyrolysis furnace (7) enters the boiler (1) again for combustion and power generation; wherein, part of the high-temperature flue gas after being dedusted by the deduster (3) enters the raw coal preheater (11) through a second induced draft fan (17) to be used as a heat source, and the flue gas after being utilized by the raw coal preheater (11) is introduced into the boiler (1) through a first induced draft fan (16) to be used as secondary air;
coal powder in a coal bunker (10) enters a raw coal preheater (11) for preheating, then enters a middle coal storage bunker (12), then enters a pyrolysis furnace (7) for pyrolysis through a spiral coal feeder (13), hot coal gas generated by the pyrolysis furnace (7) enters a high-temperature superheater (8) for cooling, the cooled coal gas enters a coal gas coarse purification unit (9) for purification, one part of the purified coal gas enters a second steam-gas heat exchanger (14) through a circulating fan (15), then enters the pyrolysis furnace (7) as a fluidizing medium of the pyrolysis furnace (7), and the other part of the purified coal gas enters a coal gas post-treatment system (23) for treatment;
one part of high-temperature steam generated by the high-temperature superheater (8) enters a first steam-gas heat exchanger (5) to exchange heat with outlet flue gas of the desulfurizing tower (4), and the other part of high-temperature steam enters a second steam-gas heat exchanger (14) to heat circulating coal gas entering the pyrolyzing furnace (7); the steam generated after the heat release of the first steam-gas heat exchanger (5) and the second steam-gas heat exchanger (14) is used as a steam source for purging, heat tracing and material conveying of other equipment pipelines in the coal pyrolysis system.
9. The waste heat utilization method according to claim 8, further comprising the steps of:
setting the flue gas temperature of a first temperature online monitor (20) to be 80 ℃, and automatically adjusting the size of a valve by a first adjusting valve (19) according to the temperature monitored by the first temperature online monitor (20), so as to adjust the steam quantity entering a first steam-gas heat exchanger (5);
the temperature of the circulating coal gas entering the pyrolysis furnace (7) is monitored by a second temperature online monitor (22) in real time, and the size of a valve is automatically adjusted by a second adjusting valve (21) according to the temperature monitored by the second temperature online monitor (22), so that the steam quantity entering a second steam-gas heat exchanger (14) is adjusted.
10. The waste heat utilization method according to claim 8, characterized in that: and the steam of the high-temperature superheater (8) comes from a four-section steam extraction of a steam turbine of the circulating fluidized bed power generation system.
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