CN110437849B - Dry quenching and coke oven flue gas combined purification process and system - Google Patents
Dry quenching and coke oven flue gas combined purification process and system Download PDFInfo
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- CN110437849B CN110437849B CN201910774753.0A CN201910774753A CN110437849B CN 110437849 B CN110437849 B CN 110437849B CN 201910774753 A CN201910774753 A CN 201910774753A CN 110437849 B CN110437849 B CN 110437849B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 164
- 239000003546 flue gas Substances 0.000 title claims abstract description 164
- 239000000571 coke Substances 0.000 title claims abstract description 127
- 238000010791 quenching Methods 0.000 title claims abstract description 59
- 230000000171 quenching effect Effects 0.000 title claims abstract description 59
- 238000000746 purification Methods 0.000 title claims abstract description 21
- 239000002699 waste material Substances 0.000 claims abstract description 136
- 239000000428 dust Substances 0.000 claims abstract description 88
- 239000002918 waste heat Substances 0.000 claims abstract description 59
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 21
- 230000023556 desulfurization Effects 0.000 claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 18
- 230000008569 process Effects 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 239000007789 gas Substances 0.000 claims description 22
- 239000002912 waste gas Substances 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 10
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- 238000004939 coking Methods 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 230000003009 desulfurizing effect Effects 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 6
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- 238000010248 power generation Methods 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 238000004062 sedimentation Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- 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
- C10B39/00—Cooling or quenching coke
- C10B39/02—Dry cooling outside the oven
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
- Chimneys And Flues (AREA)
Abstract
The invention relates to a dry quenching and coke oven flue gas combined purification process and a system, wherein the system comprises a coke oven waste flue gas introduction system, a first heat exchanger, a dry quenching furnace, a dry desulfurization device, a primary dust remover, a waste heat boiler, an SCR denitration device, a second heat exchanger, a secondary dust remover, an induced draft fan and a chimney; according to the invention, the coke oven waste flue gas waste heat recovery and desulfurization and denitrification purification process and the dry quenching process are organically combined, and the purification of the coke oven waste flue gas is completed while the red coke waste heat and the coke oven waste flue gas waste heat are recovered, so that the flue gas emission meets the national standard, and the atmospheric pollution is reduced.
Description
Technical Field
The invention relates to the technical field of coking waste heat recovery and flue gas purification, in particular to a dry quenching and coke oven flue gas combined purification process and system.
Background
In the production process of the coke oven, coal gas (blast furnace gas, coke oven gas or mixed coal gas) is combusted in a combustion chamber and simultaneously supplies heat to a carbonization chamber, high-temperature flue gas generated by combustion is discharged after heat exchange by a heat storage chamber, and the temperature of the flue gas reaches 200-300 ℃ at the moment, and is called coke oven waste flue gas. Besides N 2 carried in the air, CO 2 and H 2 O generated after combustion, the waste flue gas of the coke oven also contains a small amount of residual O 2 and SO 2、NOX generated in the combustion process, SO 2 contained in the waste flue gas of the coke oven is one of important pollution sources of the atmosphere, and NO X is one of pollution sources for causing photochemical fog, and the pollution and the harm to the atmosphere are great.
The emission standards for pollutants in the coking chemistry industry (GB 16171-2012) specify: sulfur dioxide emission in coke oven flue gas must not exceed 50mg/m 3 and nitrogen oxide emission must not exceed 500mg/m 3 from 1 month 1 2015, and as the importance of ecological environmental protection in China increases, more places and industries begin to execute stricter special emission standards, and comprehensive treatment of pollutants in coke oven waste flue gas becomes a basic requirement of a coking production enterprise. At present, the waste flue gas of the coke oven is purified by adopting a process flow of desulfurization and SCR denitration by a sodium carbonate method. The Selective Catalytic Reduction (SCR) is the most mature flue gas denitration technology at present, and a reducing agent (NH 3, urea) is utilized to selectively react with NO x under the action of a metal catalyst to generate N 2 and H 2 O, so that the flue gas meets the emission requirement. The mainstream SCR reactor is divided into medium-temperature (260-380 ℃) catalytic denitration and low-temperature (120-300 ℃) catalytic denitration. Because the distance of the common conveying process is longer before the waste flue gas of the coke oven enters the desulfurization and denitrification device, the cooling is obvious due to the large heat dissipation capacity of the pipeline, and therefore, a flue gas heating system is required to be configured to ensure that the temperature of the waste flue gas of the coke oven meets the condition of SCR denitrification reaction.
The dry quenching process is a technology for continuously recovering and utilizing sensible heat of high-temperature (950-1100 ℃) red coke by utilizing inert gas with high efficiency, and mainly comprises equipment such as a dry quenching furnace, a circulating fan, a primary dust remover, a boiler, a secondary dust remover and the like and pipeline connection. In the quenching process, red coke enters from the top of the dry quenching furnace and flows reversely with circulating cooling gas to complete the convective heat exchange process, cooled solid particles are discharged from the bottom of the shaft furnace, and high-temperature gas fully absorbing red Jiao Xianre enters a subsequent device through a gas outlet of the dry quenching furnace for waste heat utilization, such as steam generation or power generation. The process has the advantages of high waste heat recovery rate, environment-friendly operation and the like, and is widely used. However, in the dry quenching process, due to the combustion of residual volatile matters in red coke and the burning loss of part of coke powder, a certain amount of sulfur dioxide is contained in the circulating gas, and is continuously accumulated in the operation process, so that the content of sulfur dioxide in the circulating gas diffused after a fan is higher, and therefore, desulfurization and purification treatment are required to be carried out on the circulating gas in the diffused part before the circulating gas is discharged into the atmosphere. The prior art has different methods of desulfurizing and purifying the part of the diffused circulating gas, namely a complete system with complete facilities is needed to be put into the device for independently arranging the desulfurizing and purifying device, and a certain investment is increased. The flue gas is led into the flue gas desulfurization and denitrification system of the coke oven, but because the part of the scattered gas contains dust with higher concentration, necessary dust removal facilities are needed to be additionally arranged, and meanwhile, the temperature of the flue gas of the coke oven can be reduced to a certain extent, thereby adversely affecting the operation of the flue gas desulfurization and denitrification system of the coke oven.
Disclosure of Invention
The invention provides a dry quenching and coke oven flue gas combined purification process and a system, which organically integrate a coke oven waste flue gas waste heat recovery and desulfurization and denitrification purification process with a dry quenching process, realize red coke waste heat and coke oven waste flue gas waste heat recovery, and finish purification of coke oven waste flue gas at the same time, so that the flue gas emission meets the national standard, and the atmospheric pollution is reduced.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
The coke oven waste flue gas generated in the heating process of the coke oven is sent to the dry quenching furnace after heat exchange and cooling, the heat exchange and cooling are carried out on high-temperature coke, the waste flue gas discharged by the dry quenching furnace is dedusted by a primary deduster, meanwhile, a desulfurizing agent NaHCO 3 is sprayed into the primary deduster, the desulfurized waste flue gas enters a waste heat boiler to recover heat, the waste flue gas outlet temperature is controlled by the waste heat boiler, and the waste flue gas discharged after heat exchange directly enters an SCR denitration device to carry out SCR denitration catalytic reaction; and the waste flue gas after denitration is sent to a chimney for discharging after heat exchange and temperature reduction and secondary dust removal.
The dry quenching and coke oven flue gas combined purification process specifically comprises the following steps:
1) The method comprises the steps that through a coke oven waste flue gas introduction system, coke oven waste flue gas generated in the heating process of a coke oven is led out of a coke oven main flue and enters a first heat exchanger;
2) In the first heat exchanger, the coke oven waste flue gas with the temperature of 200-300 ℃ is cooled to below 150 ℃ by desalted water from a waste heat boiler in an indirect heat exchange mode, part of heat carried by the coke oven waste flue gas is recovered and sent into the waste heat boiler, and the coke oven waste flue gas after heat exchange enters the dry quenching furnace through a gas supply device at the lower part of the dry quenching furnace;
3) In the dry quenching furnace, the waste flue gas of the coke oven is reversely contacted with high-temperature coke, the waste flue gas after absorbing the heat of the coke is discharged from the upper section of the dry quenching furnace and then enters a primary dust remover, and the cooled coke is discharged through a coke discharging system at the lower part of the dry quenching furnace;
4) The dry desulfurization device sprays NaHCO 3 into the primary dust remover through a NaHCO 3 spraying pipeline, and in the primary dust remover, naHCO 3 fully contacts and reacts with SO 2 in the waste flue gas to generate NaHSO 3、Na2SO3, SO that SO 2 in the waste flue gas is removed; the generated NaHSO 3、Na2SO3 and coke powder carried by waste flue gas are separated from the flue gas in a primary dust remover through inertial collision and sedimentation;
5) Waste flue gas after primary dust removal enters a waste heat boiler, and the waste heat boiler utilizes heat carried by the waste flue gas to generate high-temperature and high-pressure steam for power generation or driving equipment so as to realize recycling of coking waste heat; directly entering waste flue gas after heat recovery of a waste heat boiler into an SCR denitration device through a pipeline for denitration treatment;
6) The waste flue gas subjected to denitration treatment by the SCR denitration device enters a second heat exchanger for cooling treatment; in the second heat exchanger, the waste flue gas is cooled by desalted water from the waste heat boiler in an indirect heat exchange mode, part of heat carried by the waste flue gas is recovered and sent into the waste heat boiler, and the cooled waste flue gas is sent into a secondary dust remover;
7) In the secondary dust remover, solid particles and dust carried in waste flue gas are removed by adopting a filtering dust removing mode, the captured particles and dust are recovered by a dust collecting device at the lower part of the secondary dust remover and then discharged, and the waste flue gas after filtering dust removing is sent to a chimney by an induced draft fan to be discharged.
The dry quenching and coke oven flue gas combined purification system comprises a coke oven waste flue gas introduction system, a first heat exchanger, a dry quenching oven, a dry desulfurization device, a primary dust remover, a waste heat boiler, an SCR denitration device, a second heat exchanger, a secondary dust remover, an induced draft fan and a chimney; the coke oven waste smoke gas introducing system comprises a coke oven main flue and a flue turning plate, wherein a coke oven waste gas outlet is arranged on the coke oven main flue, and the flue turning plate is arranged on the coke oven main flue between the coke oven waste smoke gas outlet and the chimney; the coke oven waste gas outlet is connected with a waste gas inlet of the first heat exchanger through a coke oven waste gas pipeline, and a waste gas outlet of the first heat exchanger is connected with a gas supply device at the lower part of the dry quenching furnace; the waste flue gas outlet at the upper part of the dry quenching furnace is sequentially connected with a primary dust remover, a waste heat boiler, an SCR denitration device, a second heat exchanger, a secondary dust remover, an induced draft fan and a chimney through a waste flue gas conveying pipeline; and along the flow direction of the waste flue gas, a NaHCO 3 injection port is arranged on a waste flue gas conveying pipeline at the upstream of the primary dust remover, the NaHCO 3 supply device is connected with the NaHCO 3 injection pipeline, and the NaHCO 3 injection pipeline and the NaHCO 3 supply device jointly form the dry desulfurization device.
And the first heat exchanger is provided with a demineralized water inlet and a demineralized water outlet, and the demineralized water inlet and the demineralized water outlet are respectively connected with an economizer of the waste heat boiler through demineralized water pipelines.
The second heat exchanger is provided with a waste flue gas inlet, a waste flue gas outlet, a desalted water inlet and a desalted water outlet, the waste flue gas inlet is connected with a waste flue gas conveying pipeline at the upstream of the second heat exchanger, and the waste flue gas outlet is connected with a waste flue gas conveying pipeline at the downstream of the second heat exchanger; the desalted water inlet and the desalted water outlet are respectively connected with the economizer of the waste heat boiler through desalted water pipelines.
The primary dust remover is a gravity dust remover.
The secondary dust remover is a bag type dust remover.
Compared with the prior art, the invention has the beneficial effects that:
1) The invention uses the waste flue gas of the coke oven as a heat exchange medium to cool the high-temperature coke, organically integrates the waste heat recovery of two waste heat resources of the high-temperature red coke and the waste flue gas of the coke oven in a waste heat recovery system in the coking production process, improves the waste heat recovery heat quality of the waste flue gas of the coke oven, increases the utilization capacity of the waste heat of the dry quenching coke, realizes the desulfurization and denitrification purification treatment of the waste flue gas of the coke oven, reduces the configuration of related flue gas treatment equipment such as dust removal facilities, fans and power facilities, has simple overall process layout, small occupied area and low one-time construction cost and operation cost;
2) The waste flue gas of the coke oven is heated by utilizing high-temperature coke, and the flue gas environment suitable for the medium-temperature SCR denitration catalytic reaction is formed by controlling the temperature of the waste flue gas of the coke oven behind the waste heat boiler, so that a heating system is not required to be additionally arranged, the cost of a denitration catalyst is reduced, and the denitration efficiency is improved;
3) After SCR denitration, the waste flue gas is purified by adopting a bag type dust collector, the dust collection efficiency is high, the dust concentration discharged by a secondary dust collector is below 10mg/m 3, so that a draught fan arranged behind the secondary dust collector does not need to be provided with special wear-resistant measures, compared with a traditional dry quenching circulating fan, the replacement and maintenance cost of the fan can be obviously reduced, the failure occurrence rate is reduced, and the stability of continuous operation of dry quenching is improved;
4) Compared with the existing dry quenching process, the desulfurization and denitration purification treatment of the waste flue gas of the coke oven is performed, the desulfurization problem of the diffused circulating gas is not needed to be considered, and the gas discharged into a chimney can completely meet the environmental protection standard requirement.
Drawings
FIG. 1 is a schematic diagram of the dry quenching and coke oven flue gas combined purification system.
In the figure: 1. the dry quenching furnace 2, the dry desulfurization device 3, the primary dust remover 4, the waste heat boiler 5, the SCR denitration device 6, the secondary dust remover 7, the dust collecting device 8, the first heat exchanger 9, the induced draft fan 10, the first heat exchanger 11, the coke oven main flue 12, the chimney 13, the flue turning plate 14 and the high-temperature coke
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
As shown in fig. 1, according to the coke dry quenching and coke oven flue gas combined purification process disclosed by the invention, coke oven waste flue gas generated in the heating process of a coke oven is subjected to heat exchange and cooling and then is sent into a dry quenching furnace 1, high-temperature coke 14 is subjected to heat exchange and cooling, waste flue gas discharged from the dry quenching furnace 1 is subjected to dust removal by a primary dust remover 3, meanwhile, a desulfurizing agent NaHCO 3 is sprayed into the primary dust remover 3, the desulfurized waste flue gas enters a waste heat boiler 4 to recover heat, and the waste heat boiler 4 controls the outlet temperature of the waste flue gas, so that the waste flue gas discharged after heat exchange directly enters an SCR denitration device 5 to carry out SCR denitration catalytic reaction; the waste flue gas after denitration is sent to the chimney 12 for discharging after heat exchange and temperature reduction and secondary dust removal.
The dry quenching and coke oven flue gas combined purification process specifically comprises the following steps:
1) The coke oven waste flue gas generated in the heating process of the coke oven is led out from the coke oven main flue 11 through the coke oven waste flue gas leading-in system and enters the first heat exchanger 10;
2) In the first heat exchanger 10, the coke oven waste flue gas with the temperature of 200-300 ℃ is cooled to below 150 ℃ by desalted water from the waste heat boiler 4 in an indirect heat exchange mode, part of heat carried by the coke oven waste flue gas is recovered and sent into the waste heat boiler 4, and the coke oven waste flue gas after heat exchange enters the dry quenching furnace 1 through a gas supply device at the lower part of the dry quenching furnace 1;
3) In the dry quenching furnace 1, the waste flue gas of the coke oven is reversely contacted with the high-temperature coke 14, the waste flue gas after absorbing the heat of the coke is discharged from the upper section of the dry quenching furnace 1 and then enters the primary dust remover 3, and the cooled coke is discharged through a coke discharging system at the lower part of the dry quenching furnace 1;
4) The dry desulfurization device 2 sprays NaHCO 3 into the primary dust remover 3 through a NaHCO 3 spraying pipeline, and NaHCO 3 fully contacts and reacts with SO 2 in waste flue gas in the primary dust remover 3 to generate NaHSO 3、Na2SO3, SO that SO 2 in the waste flue gas is removed; the generated NaHSO 3、Na2SO3 and coke powder carried by waste flue gas are separated from the flue gas in the primary dust remover 3 through inertial collision and sedimentation;
5) Waste flue gas after primary dust removal enters a waste heat boiler 4, and the waste heat boiler 4 utilizes heat carried by the waste flue gas to generate high-temperature and high-pressure steam for power generation or driving equipment so as to realize recycling of coking waste heat; the waste flue gas after heat recovery by the waste heat boiler 4 directly enters the SCR denitration device 5 through a pipeline for denitration treatment;
6) The waste flue gas subjected to denitration treatment by the SCR denitration device 5 enters a second heat exchanger 8 for cooling treatment; in the second heat exchanger 8, the waste flue gas is cooled by desalted water from the waste heat boiler 4 in an indirect heat exchange mode, part of heat carried by the waste flue gas is recovered and sent into the waste heat boiler 4, and the cooled waste flue gas is sent into the secondary dust remover 6;
7) In the secondary dust remover 6, solid particles and dust carried in waste flue gas are removed by adopting a filtering dust removing mode, the captured particles and dust are recovered by a dust collecting device 7 at the lower part of the secondary dust remover 6 and then discharged, and the waste flue gas after filtering dust removal is sent to a chimney 12 by an induced draft fan 9 to be discharged.
The dry quenching and coke oven flue gas combined purification system comprises a coke oven waste flue gas introduction system, a first heat exchanger 10, a dry quenching furnace 1, a dry desulfurization device 2, a primary dust remover 3, a waste heat boiler 4, an SCR denitration device 5, a second heat exchanger 8, a secondary dust remover 6, an induced draft fan 9 and a chimney 12; the coke oven waste flue gas introducing system comprises a coke oven main flue 11 and a flue turning plate 13, wherein a coke oven waste gas outlet is arranged on the coke oven main flue 11, and the flue turning plate 13 is arranged on the coke oven main flue 11 between the coke oven waste flue gas outlet and the chimney 12; the coke oven waste gas outlet is connected with a waste gas inlet of the first heat exchanger 10 through a coke oven waste gas pipeline, and a waste gas outlet of the first heat exchanger 10 is connected with a gas supply device at the lower part of the dry quenching furnace 1; the waste flue gas outlet at the upper part of the dry quenching furnace 1 is sequentially connected with a primary dust remover 3, a waste heat boiler 4, an SCR denitration device 5, a second heat exchanger 8, a secondary dust remover 6, an induced draft fan 9 and a chimney 12 through a waste flue gas conveying pipeline; and along the flow direction of the waste flue gas, a NaHCO 3 injection port is arranged on a waste flue gas conveying pipeline at the upstream of the primary dust remover 3, the NaHCO 3 supply device is connected with the NaHCO 3 injection pipeline, and the NaHCO 3 injection pipeline and the NaHCO 3 supply device jointly form the dry desulfurization device 2.
And a demineralized water inlet and a demineralized water outlet are arranged on the first heat exchanger 10 and are respectively connected with an economizer of the waste heat boiler 4 through demineralized water pipelines.
The second heat exchanger 8 is provided with a waste flue gas inlet, a waste flue gas outlet, a desalted water inlet and a desalted water outlet, the waste flue gas inlet is connected with a waste flue gas conveying pipeline at the upstream of the second heat exchanger 8, and the waste flue gas outlet is connected with a waste flue gas conveying pipeline at the downstream of the second heat exchanger 8; the desalted water inlet and the desalted water outlet are respectively connected with the economizer of the waste heat boiler 4 through desalted water pipelines.
The primary dust remover is a gravity dust remover.
The secondary dust collector 6 is a bag type dust collector.
The configurations of the coke loading device and the coke discharging device matched with the dry quenching furnace 1, and the raw material supply facilities, the powder discharging facilities, the denitration catalyst regeneration facilities and the like matched with the devices such as the primary dust remover 3, the secondary dust remover 6, the dry desulfurization device 2, the SCR denitration device 5 and the like are all the prior art, belong to the technology known to the person skilled in the art, and are not repeated here.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (4)
1. The coke oven waste flue gas generated in the heating process of the coke oven is sent into the dry quenching oven after heat exchange and cooling, the high-temperature coke is subjected to heat exchange and cooling, the waste flue gas discharged by the dry quenching oven is dedusted by a primary deduster, meanwhile, a desulfurizing agent NaHCO 3 is sprayed into the primary deduster, the desulfurized waste flue gas enters a waste heat boiler to recover heat, and the waste flue gas outlet temperature is controlled by the waste heat boiler, so that the waste flue gas discharged after heat exchange directly enters an SCR denitration device to carry out SCR denitration catalytic reaction; the waste flue gas after denitration is sent to a chimney for discharging after heat exchange, temperature reduction and secondary dust removal; the process specifically comprises the following steps:
1) The method comprises the steps that through a coke oven waste flue gas introduction system, coke oven waste flue gas generated in the heating process of a coke oven is led out of a coke oven main flue and enters a first heat exchanger;
2) In the first heat exchanger, the coke oven waste flue gas with the temperature of 200-300 ℃ is cooled to below 150 ℃ by desalted water from a waste heat boiler in an indirect heat exchange mode, part of heat carried by the coke oven waste flue gas is recovered and sent into the waste heat boiler, and the coke oven waste flue gas after heat exchange enters the dry quenching furnace through a gas supply device at the lower part of the dry quenching furnace;
3) In the dry quenching furnace, the waste flue gas of the coke oven is reversely contacted with high-temperature coke, the waste flue gas after absorbing the heat of the coke is discharged from the upper section of the dry quenching furnace and then enters a primary dust remover, and the cooled coke is discharged through a coke discharging system at the lower part of the dry quenching furnace;
4) The dry desulfurization device sprays NaHCO 3 into the primary dust remover through a NaHCO 3 spraying pipeline, and in the primary dust remover, naHCO 3 fully contacts and reacts with SO 2 in the waste flue gas to generate NaHSO 3、Na2SO3, SO that SO 2 in the waste flue gas is removed; the generated NaHSO 3、Na2SO3 and coke powder carried by waste flue gas are separated from the flue gas in a primary dust remover through inertial collision and sedimentation;
5) Waste flue gas after primary dust removal enters a waste heat boiler, and the waste heat boiler utilizes heat carried by the waste flue gas to generate high-temperature and high-pressure steam for power generation or driving equipment so as to realize recycling of coking waste heat; directly entering waste flue gas after heat recovery of a waste heat boiler into an SCR denitration device through a pipeline for denitration treatment;
6) The waste flue gas subjected to denitration treatment by the SCR denitration device enters a second heat exchanger for cooling treatment; in the second heat exchanger, the waste flue gas is cooled by desalted water from the waste heat boiler in an indirect heat exchange mode, part of heat carried by the waste flue gas is recovered and sent into the waste heat boiler, and the cooled waste flue gas is sent into a secondary dust remover;
7) In the secondary dust remover, solid particles and dust carried in waste flue gas are removed by adopting a filtering dust removing mode, the captured particles and dust are recovered by a dust collecting device at the lower part of the secondary dust remover and then discharged, and the waste flue gas after filtering dust removing is sent to a chimney by an induced draft fan to be discharged.
2. The dry quenching and coke oven flue gas combined purification system for realizing the process of claim 1 is characterized by comprising a coke oven waste flue gas introducing system, a first heat exchanger, a dry quenching furnace, a dry desulfurizing device, a primary dust remover, a waste heat boiler, an SCR denitration device, a second heat exchanger, a secondary dust remover, an induced draft fan and a chimney; the coke oven waste smoke gas introducing system comprises a coke oven main flue and a flue turning plate, wherein a coke oven waste gas outlet is arranged on the coke oven main flue, and the flue turning plate is arranged on the coke oven main flue between the coke oven waste smoke gas outlet and the chimney; the coke oven waste gas outlet is connected with a waste gas inlet of the first heat exchanger through a coke oven waste gas pipeline, and a waste gas outlet of the first heat exchanger is connected with a gas supply device at the lower part of the dry quenching furnace; the waste flue gas outlet at the upper part of the dry quenching furnace is sequentially connected with a primary dust remover, a waste heat boiler, an SCR denitration device, a second heat exchanger, a secondary dust remover, an induced draft fan and a chimney through a waste flue gas conveying pipeline; along the flow direction of the waste flue gas, a NaHCO 3 injection port is arranged on a waste flue gas conveying pipeline at the upstream of the primary dust remover, the NaHCO 3 supply device is connected with the NaHCO 3 injection pipeline, and the NaHCO 3 injection pipeline and the NaHCO 3 supply device jointly form a dry desulfurization device;
The first heat exchanger is provided with a demineralized water inlet and a demineralized water outlet, and the demineralized water inlet and the demineralized water outlet are respectively connected with an economizer of the waste heat boiler through a demineralized water pipeline;
The second heat exchanger is provided with a waste flue gas inlet, a waste flue gas outlet, a desalted water inlet and a desalted water outlet, the waste flue gas inlet is connected with a waste flue gas conveying pipeline at the upstream of the second heat exchanger, and the waste flue gas outlet is connected with a waste flue gas conveying pipeline at the downstream of the second heat exchanger; the desalted water inlet and the desalted water outlet are respectively connected with the economizer of the waste heat boiler through desalted water pipelines.
3. The combined dry quenching and coke oven flue gas cleaning system according to claim 2, wherein the primary dust remover is a gravity dust remover.
4. The combined dry quenching and coke oven flue gas purification system of claim 2, wherein the secondary dust collector is a bag collector.
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| CN111793504A (en) * | 2020-06-08 | 2020-10-20 | 新兴铸管股份有限公司 | Dust-containing gas discharge device of dry quenching coke powder bin |
| CN113416559A (en) * | 2021-07-16 | 2021-09-21 | 中煤能源研究院有限责任公司 | Boiler flue gas dry quenching system and use method thereof |
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