WO2021169589A1 - 高炉熔渣粒化和余热回收利用装置及方法 - Google Patents

高炉熔渣粒化和余热回收利用装置及方法 Download PDF

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WO2021169589A1
WO2021169589A1 PCT/CN2020/141914 CN2020141914W WO2021169589A1 WO 2021169589 A1 WO2021169589 A1 WO 2021169589A1 CN 2020141914 W CN2020141914 W CN 2020141914W WO 2021169589 A1 WO2021169589 A1 WO 2021169589A1
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Prior art keywords
temperature
slag
sludge
granular slag
gas
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PCT/CN2020/141914
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English (en)
French (fr)
Inventor
肖永力
李永谦
张友平
关运泽
谢梦芹
王英杰
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宝山钢铁股份有限公司
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Priority to BR112022016299A priority Critical patent/BR112022016299A2/pt
Priority to EP20921621.7A priority patent/EP4112749A4/en
Priority to KR1020227030099A priority patent/KR20220144816A/ko
Priority to US17/802,605 priority patent/US20230100959A1/en
Priority to JP2022551754A priority patent/JP7532537B2/ja
Publication of WO2021169589A1 publication Critical patent/WO2021169589A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B3/00—General features in the manufacture of pig-iron
    • C21B3/04—Recovery of by-products, e.g. slag
    • C21B3/06—Treatment of liquid slag
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B3/00—General features in the manufacture of pig-iron
    • C21B3/04—Recovery of by-products, e.g. slag
    • C21B3/06—Treatment of liquid slag
    • C21B3/08—Cooling slag
    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03C—CHEMICAL COMPOSITION OF GLASSES, GLAZES OR VITREOUS ENAMELS; SURFACE TREATMENT OF GLASS; SURFACE TREATMENT OF FIBRES OR FILAMENTS MADE FROM GLASS, MINERALS OR SLAGS; JOINING GLASS TO GLASS OR OTHER MATERIALS
    • C03C13/00—Fibre or filament compositions
    • C03C13/06—Mineral fibres, e.g. slag wool, mineral wool, rock wool
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B7/00—Blast furnaces
    • C21B7/002—Evacuating and treating of exhaust gases
    • 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
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/14—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours using industrial or other waste gases
    • 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
    • F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/02—Physical or chemical treatment of slags
    • C21B2400/022—Methods of cooling or quenching molten slag
    • C21B2400/024—Methods of cooling or quenching molten slag with the direct use of steam or liquid coolants, e.g. water
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/02—Physical or chemical treatment of slags
    • C21B2400/032—Separating slag from liquid, e.g. from water, after quenching
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/05—Apparatus features
    • C21B2400/062—Jet nozzles or pressurised fluids for cooling, fragmenting or atomising slag
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2400/00—Treatment of slags originating from iron or steel processes
    • C21B2400/08—Treatment of slags originating from iron or steel processes with energy recovery
    • 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
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling
    • 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
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/25—Process efficiency
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies

Definitions

  • the invention relates to a metallurgical slag processing equipment and method, in particular to a blast furnace slag granulation and waste heat recovery and utilization device and method.
  • Blast furnace slag is the main by-product of blast furnace ironmaking.
  • the blast furnace slag produced per ton of iron is about 350 kg.
  • the temperature of blast furnace slag is 1450°C ⁇ 1550°C, and the sensible heat ((1260-1880) ⁇ 10 3 kJ) carried by one ton of slag is equivalent to the calorific value of 60kg standard coal, which has high recovery value.
  • the treatment of blast furnace slag mostly adopts the water quenching process.
  • the slag is washed into water slag by high-pressure water, and the high-grade sensible heat is transferred to the water slag and wastewater at about 80°C, which loses the value of recycling.
  • each ton of molten slag needs to consume 0.4-0.5 tons of water and discharge a large amount of waste steam rich in H 2 S, SO 2 and other pollutants.
  • 8-15% of the water in the slag needs to be dried, and one ton of slag needs to consume about 1000 m 3 of hot air at 500°C, which causes a lot of waste of resources.
  • Blast furnace slag is a high-temperature melt formed from gangue in ore, ash in fuel and non-volatile components in solvent (usually limestone) in the process of blast furnace ironmaking.
  • the temperature is about 1450°C.
  • the main chemical The ingredients are: silicon dioxide (SiO 2 ), aluminum oxide (Al 2 O 3 ), calcium oxide (CaO), magnesium oxide (MgO), manganese oxide (MnO), iron oxide (FeO), sulfur, etc.
  • the mass ratio of silicon dioxide (SiO 2 ) and aluminum oxide (Al 2 O 3 ) to calcium oxide (CaO) and magnesium oxide (MgO) is about 0.8-1.2. Therefore, blast furnace slag has the characteristics of low thermal conductivity and a sharp increase in viscosity as the temperature decreases, resulting in slow heat exchange of blast furnace slag and high difficulty in waste heat recovery.
  • the rapid dry granulation of molten slag particles can create conditions for heat recovery.
  • the rapid dry granulation of molten slag mainly includes wind crushing method and centrifugal granulation method.
  • the wind crushing method has not been popularized and applied in the field of blast furnace slag treatment due to its high noise and easy generation of slag wool. It is only suitable for the treatment of part of the steel slag with good fluidity.
  • Centrifugal granulation mainly uses a rotating disc or a cup as a granulator, and uses centrifugal force to disperse and break the slag into fine droplets for rapid cooling. After cooling, the glass content and activity of the slag particles can be maintained to meet the requirements of slag powder raw materials. , But the slag crusts, the granulated slag is not uniform in size, and it is easy to produce slag wool and other problems.
  • Chinese invention patent ZL 201410755689.9 discloses a high-temperature slag waste heat recovery system and method.
  • the device includes a slag conveying unit, a slag granulation unit and a waste heat recovery unit, which can recover the sensible heat of high-temperature slag, but in the waste heat recovery process
  • the intermediate molten slag is transported in a slag tank for a long distance, which is easy to cool down, requires additional heat supplementation, high energy consumption, and low waste heat recovery efficiency.
  • Chinese invention patent ZL 201010566938.1 discloses a metallurgical molten slag dry granulation and heat recovery system.
  • the liquid molten slag is dry granulated by centrifugal rotation and air pulse.
  • ring-shaped airflow nozzles and atomizing water nozzles are respectively arranged around the rotating shaft of the centrifugal rotating disk, a water-cooled wall is arranged on the inner side wall of the dry granulation device, and a toroidal fluidization device is arranged under the water-cooled wall, An annular fluidized bed is arranged at the bottom of the dry granulation device.
  • the waste heat utilization of the slag recovered through this invention patent is limited to the conversion of hot air/nitrogen into steam or power generation, and the efficiency is low.
  • sludge As a kind of solid waste, sludge has become the second largest source of solid waste pollution after urban garbage pollution.
  • the main traditional disposal methods of sludge include landfill, incineration, sea discharge, and agricultural use.
  • sewage treatment such as industrial sewage and domestic sewage
  • sludge treatment is also common.
  • the existing technology of sludge treatment can adopt fermentation, melting, lime addition, carbonization and other treatment methods, but the equipment cost and energy consumption are very high, the treatment efficiency is low, and there may be problems with air and water sources. Secondary pollution.
  • the purpose of the present invention is to provide a blast furnace slag granulation and waste heat recovery and utilization device and method, which realizes the complete granulation of blast furnace slag, and recovers the sensible heat of the slag and sludge drying, and prepares steam and hot water organically.
  • the coupling realizes the waste heat recovery of high-temperature gas and high-temperature granulated slag in the process of slag granulation treatment, which greatly improves the efficiency of waste heat recovery and utilization.
  • the present invention is realized as follows:
  • a blast furnace slag granulation and waste heat recovery and utilization device which is characterized in that it comprises an aerosol granulation nozzle assembly, a deflector, a cyclone separator and a waste heat recovery device;
  • the aerosol granulation nozzle assembly includes a slag flow controller, a compressed air flow control valve, a water volume control valve, and an aerosol spray gun;
  • the slag flow controller is connected to the slag inlet of the deflector;
  • the compression The air flow control valve is connected with the gas inlet of the aerosol spray gun;
  • the water volume control valve is connected with the liquid inlet of the aerosol spray gun;
  • the nozzle of the mist spray gun is arranged facing the inlet of the deflector for passing the aerosol Impact the slag flow entering the deflector through the slag flow controller to form medium-temperature gas and high-temperature granular slag with preliminary solidification on the surface;
  • the deflector is used to fully mix the medium-temperature gas and the high-temperature granular slag that has initially solidified on the surface.
  • the outlet of the deflector is connected to the inlet of the cyclone separator so that the complete The solidified high temperature granular slag and medium and high temperature gas enter the cyclone separator;
  • the cyclone separator is used to separate high-temperature granular slag and medium- and high-temperature gas; wherein the discharge port of the cyclone separator is connected to the feed port of the waste heat recovery device, and is used to separate the medium- and high-temperature gas and the completely solidified high-temperature granule.
  • the slag is transported to the waste heat recovery device.
  • the present invention provides a blast furnace slag granulation and waste heat recovery and utilization device, including an aerosol granulation nozzle assembly, a deflector, a cyclone separator and a waste heat recovery device;
  • the aerosol granulation nozzle assembly includes a slag flow controller, a compressed air flow control valve, a water volume control valve and an aerosol spray gun; the molten slag flow is controlled by the slag flow controller and flows into the slag inlet of the deflector, The high pressure gas is connected to the gas inlet of the aerosol spray gun through the compressed air flow control valve, and the water is connected to the liquid inlet of the aerosol spray gun through the water volume control valve. Flow, forming medium-temperature gas and high-temperature granular slag that is initially solidified on the surface;
  • the outlet of the deflector is connected to the feed inlet of the cyclone separator.
  • the medium-temperature gas and the high-temperature granular slag initially solidified on the surface are fully mixed in the deflector to form fully solidified high-temperature granular slag and medium-high-temperature gas before entering
  • the cyclone separator completes the separation of high-temperature granular slag and medium-high-temperature gas through the cyclone separator; the discharge port of the cyclone separator is connected to the feed port of the waste heat recovery device, and the medium-high-temperature gas and the completely solidified high-temperature granules are separated.
  • the slag is transported to the waste heat recovery device.
  • the temperature of the medium-temperature gas formed by the aerosol impact of the aerosol granulation nozzle assembly into the slag flow is 200-400°C, and the temperature of the high-temperature granular slag that is preliminarily solidified on the surface is 1000-1200°C;
  • the temperature of the medium and high temperature gas is 300-500°C, and the temperature of the fully solidified high temperature granular slag is 800-1100°C;
  • the temperature of the high temperature granular slag separated by the cyclone separator is 700-950°C, and the temperature of the medium and high temperature gas is 350-550°C.
  • the waste heat recovery device is a sludge drying component;
  • the sludge drying component includes a spiral mixer, a sludge dryer, a sludge pre-drying component, a sludge recovery component and an exhaust gas treatment component;
  • the cyclone separator The discharge port is connected with the first inlet of the screw mixer and the fully solidified high-temperature pellets are transported to the screw mixer, and the aerosol port of the cyclone separator is connected with the aerosol port of the sludge pre-drying assembly
  • the medium and high temperature gas is transported to the sludge pre-drying component, so that the medium and high temperature gas is mixed with the wet sludge in the sludge pre-drying component to form semi-dried sludge;
  • the discharge port of the sludge pre-drying component is mixed with the screw
  • the second inlet of the feeder is connected and transports the semi-dried sludge to the screw mixer, so that the semi-dried
  • the discharge port of the sludge dryer is connected to the feed port of the sludge recovery component and The dry sludge powder and slag particles are transported into the sludge recovery component; the air inlet of the exhaust gas treatment component is respectively connected with the air outlet of the sludge pre-drying component, the air outlet of the sludge dryer and the air outlet of the sludge recovery component.
  • the waste heat recovery device is a high-temperature steam preparation component, and the high-temperature steam preparation component is connected to the cyclone separator and recovers the heat of the medium and high temperature gas and the high temperature granular slag to produce high temperature steam at 200-250°C.
  • the high temperature steam is incorporated into the pipe network. Stage utilization or power generation; the tail gas outlet of the high-temperature steam preparation component is connected with the tail gas treatment component.
  • the high-temperature steam preparation components include a slag bin, an exhaust gas processor, an exhaust gas purifier, an exhaust fan, a chimney, a high-temperature feeder, a high-temperature pellet heat exchanger, a boiler, and an economizer;
  • the high-temperature conveyor is set between the discharge port of the cyclone separator and the feed port of the high-temperature granular slag heat exchanger, and is used to transport the high-temperature granular slag separated by the cyclone separator to the high-temperature granular slag for heat exchange.
  • the upper part of the high-temperature granular slag heat exchanger is equipped with a coil with built-in circulating water for reverse heat exchange with the high-temperature granular slag through the coil and the airflow rising from the bottom;
  • the slag bin is located at the high-temperature granular slag Below the discharge port at the bottom of the heat exchanger, it is used to receive the cooled granular slag;
  • the top of the high-temperature granular slag heat exchanger is provided with an airflow port and connected to the boiler;
  • the economizer is connected to the boiler and the high-temperature granular slag heat exchanger respectively , So that the pure water sent to the economizer through the external pipe network is preheated by the exhaust gas discharged from the boiler to above 80°C, and is divided into two parts, one part is sent into the boiler, and the other part enters the high-temperature granular slag heat exchanger
  • the coil tube is used to absorb the heat of high
  • the water in the coil evaporates and rises to about 250°C, it enters the upper steam drum of the boiler, mixes with the steam generated by the boiler itself, and merges into the external pipe network.
  • the waste heat recovery device is a low-temperature hot water preparation component; the low-temperature hot water preparation component is connected to the cyclone separator and recovers the heat of the medium and high temperature gas and the high temperature granular slag to produce 70-95°C low temperature hot water and low temperature hot water It is sent to users for use or refrigeration at the same level; the tail gas outlet of the low-temperature hot water preparation component is connected with the tail gas treatment component.
  • the low-temperature hot water preparation component includes a slag bin, an exhaust gas processor, an exhaust gas purifier, an exhaust fan, a chimney, a high-temperature feeder, a high-temperature pellet heat exchanger, and a boiler;
  • the high-temperature conveyor is set between the discharge port of the cyclone separator and the feed port of the high-temperature granular slag heat exchanger, and is used to transport the high-temperature granular slag separated by the cyclone separator to the high-temperature granular slag for heat exchange.
  • the upper part of the high-temperature granular slag heat exchanger is equipped with a coil with built-in circulating water for reverse heat exchange with the high-temperature granular slag through the coil and the airflow rising from the bottom;
  • the slag bin is located at the high-temperature granular slag Below the discharge port at the bottom of the heat exchanger, it is used to receive the cooled granular slag;
  • the top of the high-temperature granular slag heat exchanger is provided with an air outlet and connected to the boiler;
  • the boiler and the high-temperature granular slag heat exchanger are respectively connected to the external pipe network , Used to receive pure water to exchange heat in the boiler and the high-temperature granular slag heat exchanger;
  • the air inlet of the exhaust gas processor is connected with the exhaust outlet of the boiler, and the air outlet of the exhaust gas processor is connected to the exhaust gas purifier.
  • the air inlet is connected, and the air outlet of the exhaust gas purifier is
  • the exhaust gas treatment assembly includes an exhaust gas processor, an exhaust gas purifier, an exhaust fan, and a chimney.
  • the air inlet of the exhaust gas processor is connected to the air outlet of the sludge pre-drying assembly and the air outlet of the sludge dryer through a pipe.
  • the outlet of the sludge recovery component, the exhaust outlet of the boiler and the exhaust outlet of the economizer, the outlet of the exhaust processor is connected with the inlet of the exhaust purifier, and the outlet of the exhaust purifier is connected to the chimney through the exhaust fan .
  • a method for granulating blast furnace slag and recycling waste heat includes the following steps:
  • Step 1 After the blast furnace slag is separated from the molten iron, it enters the slag slag ditch, and the formed slag stream flows into the deflector after being controlled by the slag flow controller;
  • Step 2 Adjust the compressed air flow control valve and water volume control valve to form a high-pressure gas mist in the aerosol spray gun and spray it through the nozzle, so that the high-pressure gas mist impacts the slag flow flowing into the deflector, forming a medium-temperature gas and a preliminary surface Solidified high-temperature pellets;
  • Step 3 The medium-temperature gas and the high-temperature granular slag initially solidified on the surface are mixed and exchanged through the deflector to form a fully solidified high-temperature granular slag and medium-high-temperature gas and transported to the cyclone separator.
  • the high-temperature granular slag and the high-temperature granular slag are separated from Medium and high temperature gas;
  • Step 4 The cyclone separator transports the medium and high temperature gas and high temperature granular slag to the waste heat recovery device.
  • the heat of the medium and high temperature gas and high temperature granular slag is recovered by the waste heat recovery device and used for sludge drying, high temperature steam preparation, power generation or low temperature heat. Water preparation.
  • the temperature of the medium-temperature gas formed by the aerosol impact of the aerosol granulation nozzle assembly into the slag flow is 200-400°C, and the temperature of the high-temperature granular slag initially solidified on the surface is 1000 -1200°C; the temperature of the medium and high temperature gas mixed by the deflector is 300-500°C, the temperature of the fully solidified high-temperature granular slag is 800-1100°C; the temperature of the high-temperature granular slag separated by the cyclone separator is 700-950°C, the temperature of medium and high temperature gas is 350-550°C.
  • the step of drying the sludge includes:
  • Step 4.1.1 The wet sludge in the sludge tank is pumped into the sludge pre-dryer through the sludge pump;
  • Step 4.1.2 The sludge pre-dryer mixes wet sludge and medium-high temperature gas and reverses heat exchange to form semi-dried sludge;
  • Step 4.1.3 The sludge pre-drying component transports the semi-dried sludge into the spiral mixer, the cyclone separator transports the high-temperature granular slag into the spiral mixer, and the semi-dried sludge and high-temperature granular slag pass through The screw mixer mixes into a sludge mixture;
  • Step 4.1.4 The screw mixer conveys the sludge mixture to the sludge dryer, and the sludge dryer dries the sludge mixture into dry sludge powder and slag particles and transports them to the sludge recovery module;
  • Step 4.1.5 The sludge separator of the sludge recovery module separates the dry sludge powder from the slag particles;
  • Step 4.1.6 The sludge separator transports the dry sludge powder into the dry sludge powder bin for temporary storage;
  • Step 4.1.7 The sludge separator transports the slag particles into the slag bin for temporary storage.
  • the method further includes: purifying and discharging wet tail gas by using the tail gas treatment component, including: the tail gas processor of the tail gas treatment component collects and pretreats the wet tail gas from a sludge pre-dryer, a sludge dryer, and a sludge separator After that, the exhaust gas purifier is deeply purified, and the exhaust gas after purification is discharged through the chimney through the exhaust fan; the fine powder collected in the exhaust gas processor and the exhaust gas purifier is pumped out through an external tanker.
  • the step of preparing the high-temperature steam includes:
  • Step 4.2.1 The cyclone separator conveys the high-temperature granular slag to the high-temperature granular slag conveyor.
  • the high-temperature granular slag is lifted by the high-temperature granular slag conveyor and sent to the high-temperature granular slag uniformly from the upper inlet of the high-temperature granular slag heat exchanger.
  • the high-temperature granular slag moves from top to bottom, and respectively contacts the cooling water in the coil and the bottom-up air in countercurrent heat exchange during the descending process;
  • Step 4.2.2 The heated steam is discharged from the top of the high-temperature granular slag heat exchanger and sent to the boiler, and the cooled granular slag is discharged from the lower part of the high-temperature granular slag heat exchanger into the slag bin;
  • Step 4.2.3 The external pipe network sends pure water to the economizer, and is preheated by the exhaust gas from the boiler to above 80°C, and one part is sent to the boiler to be continuously heated and vaporized into 200-250°C steam, and the other part Enter the coil of the high-temperature granular slag heat exchanger to absorb the heat of the high-temperature granular slag;
  • Step 4.2.4 When the water in the coil vaporizes and rises to about 250°C, it enters the upper steam drum of the boiler, mixes with the steam generated by the boiler itself, and merges into the external pipe network.
  • the preparation step of the low-temperature hot water includes:
  • Step 4.3.1 The cyclone separator transports the high-temperature granular slag to the high-temperature granular slag conveyor.
  • the high-temperature granular slag is lifted by the high-temperature granular slag conveyor and sent into the high-temperature granular slag uniformly from the upper inlet of the high-temperature granular slag heat exchanger.
  • the high-temperature granular slag moves from top to bottom, and respectively contacts the cooling water in the coil and the bottom-up air in countercurrent heat exchange during the descending process;
  • Step 4.3.2 The heated 70-95°C low-temperature hot water is discharged from the top of the high-temperature granular slag heat exchanger and sent to the boiler, and the cooled granular slag is discharged from the lower part of the high-temperature granular slag heat exchanger into the slag bin;
  • Step 4.3.3 The external pipe network sends part of the pure water into the boiler and is heated to 70-95°C by the gas passing through the boiler, and the other part enters the coil of the high-temperature granular slag heat exchanger to absorb high-temperature granular slag.
  • Step 4.3.4 The water in the coil absorbs heat and heats up, enters the upper steam drum of the boiler, mixes with the hot water generated by the boiler itself, and merges into the external pipe network.
  • the method further includes: purifying and discharging wet exhaust gas using an exhaust gas treatment component, including: the exhaust gas processor of the exhaust gas treatment component collects from a sludge pre-dryer, a sludge dryer, and a sludge separator After pretreatment, the wet exhaust gas is deeply purified by the exhaust gas purifier.
  • the exhaust gas after purification is discharged through the chimney through the exhaust fan; the fine powder collected in the exhaust gas processor and the exhaust gas purifier is pumped out by an external tanker.
  • the present invention has the following beneficial effects:
  • the blast furnace slag granulation and waste heat recovery and utilization device of the present invention separates the blast furnace slag through aerosol impact and swirling to form fully solidified high-temperature granular slag and medium-high temperature gas.
  • the granulated slag has uniform granularity and avoids granulation.
  • the production of slag and cotton in the chemical process; the separated high-temperature granular slag and medium-high temperature gas can be directly used in the various steps of sludge drying, with high waste heat recovery efficiency, and can also be used for high-temperature steam power generation, hot water recovery, etc.
  • the blast furnace slag granulation and waste heat recovery and utilization device of the present invention organically couples the sensible heat recovery of the slag and sludge drying.
  • the blast furnace slag is quickly and safely granulated while realizing the efficient drying of sludge, which not only greatly improves
  • the waste heat recovery efficiency is improved, the waste heat recovery cost is reduced, and the problem of low efficiency and high cost of sludge drying is solved at the same time.
  • the blast furnace slag granulation and waste heat recovery and utilization method of the present invention completely granulate the blast furnace slag into high-temperature granular slag suitable for high-efficiency waste heat recovery, and recover the sensible heat of the slag by recovering the waste heat of the medium- and high-temperature gas and high-temperature granular slag. Get the maximum use of the same level, can produce better economic and social benefits.
  • the present invention realizes complete granulation of blast furnace slag and uniform particle size, organically couples sensible heat recovery of slag and sludge drying, and realizes the waste heat of high-temperature gas and high-temperature granulated slag during the process of slag treatment. Recycling greatly improves the efficiency of waste heat recovery and utilization, and has good economic and social benefits. It can be popularized and applied in the field of slag treatment of various sizes and models of blast furnaces, and has a broad prospect.
  • Embodiment 2 is a process flow diagram of Embodiment 2 in the blast furnace slag granulation and waste heat recovery and utilization device of the present invention
  • Embodiment 3 is a process flow diagram of Embodiment 3 in the blast furnace slag granulation and waste heat recovery and utilization device of the present invention
  • Fig. 4 is a flow chart of the method for granulating blast furnace slag and recovering waste heat according to the present invention.
  • the dotted line is the gas flow conveying pipeline
  • the solid line is the slag particle conveying pipeline.
  • 1 slag flow 1 slag flow
  • 2 slag flow controller 3 compressed air flow control valve
  • 4 water control valve 5 aerosol spray gun
  • 6 slag particles 7 deflector
  • 8 cyclone separator 9 spiral mixer Feeder
  • 10 sludge dryer 11 slag bin
  • 12 dry sludge powder bin 13 sludge separator
  • 14 sludge pre-dryer 15 sludge pump
  • 16 sludge tank 17 exhaust gas processor
  • 18 tail gas Purifier 19 exhaust fans, 20 chimneys, 21 high temperature conveyors, 22 high temperature pellet heat exchangers, 23 boilers, 24 economizers.
  • a blast furnace slag granulation and waste heat recovery and utilization device including an aerosol granulation nozzle assembly, a deflector 7, a cyclone separator 8 and a waste heat recovery device;
  • the outlet of the deflector 7 is connected to the feed inlet of the cyclone separator 8.
  • the medium-temperature gas and the high-temperature granular slag 6 initially solidified on the surface are fully mixed in the deflector to form a fully solidified high-temperature granular slag 6 and the medium-high-temperature gas enter the cyclone separator 8 and complete the high-temperature granular slag 6 through the cyclone separator 8. Separation from medium and high temperature gas.
  • the discharge port of the cyclone separator 8 is connected to the feed port of the waste heat recovery device, and conveys the medium and high temperature gas and the fully solidified high temperature granular slag 6 into the waste heat recovery device.
  • the high-temperature granular slag 6 and the medium-temperature gas initially solidified on the surface are fully mixed in the deflector 7, and enter the cyclone separator 8 to fully mix and exchange heat, so that the high-temperature granular slag 6 is completely solidified, and the generation of slag and cotton is avoided. It is more conducive to heat recovery, and at the same time realizes the separation of medium and high temperature airflow and high temperature granular slag 6.
  • the temperature of the separated high-temperature granular slag 6 is reduced to 700-950°C, preferably 800-850°C, which is convenient for the waste heat recovery component to heat it recycle and re-use.
  • the temperature of the slag stream 1 is 1450-1550°C; the temperature of the medium-temperature gas formed by the gas mist impacting the slag stream 1 through the aerosol granulation nozzle assembly is 200-400°C, and the surface of the high-temperature granular slag 6 that is initially solidified
  • the temperature is 1000-1200°C, preferably 1100°C; the temperature of the medium-high temperature gas mixed by the deflector 7 is 300-500°C, preferably 400°C, and the temperature of the fully solidified high-temperature granular slag 6 is 800-1100°C , Preferably 950°C; the temperature of the high-temperature granular slag 6 separated by the cyclone separator 8 is 700-950°C, preferably 800-850°C, and the temperature of the medium-high temperature gas is 350-550°C.
  • the waste heat recovery device is a sludge drying component, which can be directly used for sludge drying.
  • the problem of difficult sludge treatment and high energy consumption is solved.
  • the sludge drying components include spiral mixer 9, sludge dryer 10, sludge pre-drying component, sludge recovery component and exhaust gas treatment component; cyclone
  • the discharge port of the separator 8 is connected with the first feed port of the spiral mixer 9 and the fully solidified high-temperature granular slag 6 is transported into the spiral mixer 9.
  • the aerosol port of the cyclone separator 8 and the sludge The aerosol port of the pre-drying component is connected and conveys the medium and high temperature gas to the sludge pre-drying component, so that the medium and high temperature gas is mixed with the wet sludge in the sludge pre-drying component to form semi-dried sludge; the sludge is pre-dried
  • the discharge port of the component is connected with the second inlet of the screw mixer 9 and the semi-dried sludge is transported into the screw mixer 9, so that the semi-dried sludge and the fully solidified high-temperature granular slag 6 are in the screw
  • the mixer 9 is mixed into a sludge mixture; the discharge port of the spiral mixer 9 is connected with the feed port of the sludge dryer 10 and the sludge mixture is transported to the sludge dryer 10, the sludge mixture
  • the sludge dryer 10 is further mixed and dried into dry sludge powder and low
  • the discharge port of the sludge dryer 10 is connected with the feed port of the sludge recovery component and the dry sludge powder and slag particles are transported to Inside the sludge recovery assembly; the air inlet of the exhaust gas treatment assembly is respectively connected with the air outlet of the sludge pre-drying assembly, the air outlet of the sludge dryer 10, and the air outlet of the sludge recovery assembly.
  • the sludge pre-drying component includes a sludge pre-dryer 14, a sludge pump 15, and a sludge tank 16.
  • the discharge port of the sludge tank 16 is connected to the sludge pre-dryer 14 through a pipeline through the sludge pump 15
  • the feed port enables the wet sludge in the sludge tank 16 to be transported to the sludge pre-dryer 14; the sludge pre-dryer 14 is provided with an aerosol port and is connected to the aerosol port of the cyclone separator 8.
  • the aerosol port and the feed port of the sludge pre-dryer 14 are respectively located at the two ends of the sludge pre-dryer 14, so that the medium and high temperature gas and the sludge move relative to each other and reverse heat exchange.
  • the contact area between the medium and high temperature gas and the sludge is
  • the sludge pre-dryer 14 is provided with an air outlet and is connected with the air inlet of the exhaust gas treatment assembly.
  • the wet sludge in the sludge tank 16 is pumped to the sludge pre-dryer 14 through the sludge pump 15 and exchanges heat with the medium and high temperature gas in the sludge pre-dryer 14 to form semi-dried sludge.
  • the sludge recovery component includes a slag bin 11, a dry sludge powder bin 12, and a sludge separator 13; the sludge separator 13 is provided with an inlet, two outlets and an air outlet, and a sludge dryer 10
  • the discharge port of the sludge separator 13 is connected to the feed port of the sludge separator 13, the two discharge ports of the sludge separator 13 are respectively connected to the slag bin 11 and the dry mud powder bin 12; the air inlet of the tail gas treatment component is connected to the slag The air outlet of the mud separator 13.
  • the mixture of dry mud powder and slag particles enters the slag sludge separator 13 and is separated by the slag sludge separator 13, and the dry sludge powder is temporarily stored in the dry sludge powder bin 12, and the slag particles are temporarily stored in the slag bin 11 for later recovery and treatment.
  • the wet tail gas in the sludge separator 13 enters the tail gas treatment component.
  • the exhaust gas treatment assembly includes an exhaust gas processor 17, an exhaust gas purifier 18, an exhaust fan 19, and a chimney 20.
  • the air inlets of the exhaust gas processor 17 are respectively connected to the sludge pre-dryer 14 in the sludge pre-drying assembly through pipes.
  • the intake port of the exhaust gas purifier 18 is connected, and the exhaust port of the exhaust gas purifier 18 is connected to the chimney 20 through the exhaust fan 19;
  • the exhaust gas purifier 18 performs a deep purification process, and then is discharged through the chimney 20 through the exhaust fan 19.
  • the lower part of the exhaust gas processor 17 and the exhaust gas purifier 18 are both provided with a discharge port.
  • the discharge port is connected to the tanker through a pipeline.
  • the exhaust gas processor 17 and the exhaust gas purifier 18 can be filtered through the external tanker to extract a small amount of fine powder.
  • the normal operation of the exhaust gas processor 17 and the exhaust gas purifier 18 also facilitates the subsequent utilization and processing of the micropowder.
  • the waste heat recovery device is a high-temperature steam preparation component, which can be used to prepare high-temperature steam and generate electricity.
  • the high-temperature steam preparation component is connected to the cyclone separator 8 and recovers the heat of the medium and high temperature gas and the high-temperature granular slag 6 to produce high-temperature steam at 200-250°C.
  • the high-temperature steam is incorporated into the pipeline network for use or power generation at the same level;
  • the tail gas outlet of the economizer 24 is connected with a tail gas processing component.
  • the high-temperature steam preparation components include a slag bin 11, an exhaust gas processor 17, an exhaust gas purifier 18, an exhaust fan 19, a chimney 20, a high-temperature conveyor 21, a high-temperature granular slag heat exchanger 22, a boiler 23, and an economizer. 24;
  • the high-temperature conveyor 21 is set between the discharge port of the cyclone separator 8 and the inlet of the high-temperature granular slag heat exchanger 22, and the high-temperature granular slag 6 separated by the cyclone separator 8 passes through the high-temperature conveyor 21 is transported to the upper part of the high-temperature granular slag heat exchanger 22 and slowly descends.
  • the high-temperature granular slag heat exchanger 22 is equipped with a coil with built-in circulating water, and the high-temperature granular slag 6 is reversed with the coil and the upward airflow.
  • the temperature is lowered to 100°C;
  • the slag bin 11 is set under the discharge port at the bottom of the high-temperature granular slag heat exchanger 22, and the cooled granular slag is sent to the slag bin 11 for post-processing;
  • the high-temperature granular slag heat exchanger 22 There is an airflow port on the top and it is connected to the boiler 23;
  • the economizer 24 is connected to the boiler 23, and the external pipe network sends pure water to the economizer 24, and is pre-prepared by the medium and low temperature exhaust gas (below 250°C) discharged from the boiler 23
  • the medium and low temperature exhaust gas (below 250°C)
  • the water in the coil evaporates and rises to about 250°C, it enters the upper steam drum of the boiler 23, mixes with the steam generated by the boiler 23 itself, and merges into the external pipe network for use at the same level or to generate electricity; the intake of the exhaust gas processor 17
  • the outlet is connected with the exhaust outlet of the economizer 24, the outlet of the exhaust processor 17 is connected with the inlet of the exhaust purifier 18, and the outlet of the exhaust purifier 18 is connected to the chimney 20 through an exhaust fan 19 for exhaust gas Purification and emission.
  • the waste heat recovery device is a low-temperature hot water preparation component, which can be used to prepare domestic hot water.
  • the low-temperature hot water preparation component is connected to the cyclone separator 8 and recovers the heat of the medium and high temperature gas and the high-temperature granular slag 6 to prepare low-temperature hot water at 70-95°C.
  • the low-temperature hot water is sent to the user for use or refrigeration at the same level;
  • the exhaust gas outlet of the boiler 23 of the preparation assembly is connected with an exhaust gas treatment assembly.
  • the low-temperature hot water preparation components include a slag bin 11, an exhaust gas processor 17, an exhaust gas purifier 18, an exhaust fan 19, a chimney 20, a high-temperature feeder 21, a high-temperature granular slag heat exchanger 22 and a boiler 23;
  • the feeder 21 is arranged between the discharge port of the cyclone separator 8 and the feed port of the high-temperature granular slag heat exchanger 22, and the high-temperature granular slag 6 separated by the cyclone separator 8 is transported to the high temperature by the high-temperature conveyor 21
  • the upper part of the granular slag heat exchanger 22 slowly descends.
  • the high-temperature granular slag heat exchanger 22 is equipped with a coil with a built-in circulating water.
  • the slag bin 11 is set under the discharge port at the bottom of the high-temperature granular slag heat exchanger 22, and the cooled granular slag is sent to the slag bin 11 for post-processing; the top of the high-temperature granular slag heat exchanger 22 is provided There is a gas flow port and connected to the waste heat boiler 23; the external pipe network sends a part of the pure water into the boiler 23 and is heated to 70-95°C, and the other part enters the coil of the high-temperature granular slag heat exchanger 22 to absorb the high-temperature granular slag 6 When the water in the coil absorbs heat and heats up, it enters the upper steam drum of the boiler 23, mixes with the hot water generated by the boiler 23 itself, and merges into the external pipe network for use as domestic water or cooling; the intake of the exhaust gas processor 17 The outlet is connected with the exhaust outlet of the boiler 23, the outlet of the exhaust processor 17 is connected with the inlet of the exhaust purifier 18, and
  • the exhaust gas purifier 18 can be a cloth bag or an electrostatic precipitator.
  • the cyclone separator 8 is provided with a feed port, a discharge port and an aerosol port, the feed port of the cyclone separator 8 is connected to the discharge port of the deflector 7, and the cyclone separator
  • the discharge port of 8 is connected with the first feed port of the spiral mixer 9, and the aerosol port of the cyclone separator 8 is connected with the aerosol port of the sludge pre-dryer 14 of the sludge pre-drying assembly, which can be connected by a rotary High-efficiency separation of high-temperature slag particles 6 and medium- and high-temperature gas.
  • a blast furnace slag granulation and waste heat recovery method including the following steps:
  • Step 1 The blast furnace slag is separated from the molten iron and enters the slag ditch.
  • the slag flow 1 flows into the deflector 7 after being controlled by the slag flow controller 2.
  • Step 2 Adjust the compressed air flow control valve 3 and the water volume control valve 4 to form a high-pressure gas mist in the aerosol spray gun 5 and spray it through the nozzle, so that the high-pressure gas mist impacts the slag flow 1 flowing into the deflector 7 to form Medium-temperature gas and high-temperature granular slag initially solidified on the surface 6.
  • Step 3 After the medium-temperature gas and the high-temperature granular slag 6 initially solidified on the surface are mixed and heat exchanged by the deflector 7, the completely solidified high-temperature granular slag 6 and the medium-high temperature gas are formed and sent to the cyclone separator 8, and separated by the cyclone.
  • the cyclone 8 separates the high temperature granular slag 6 from the medium and high temperature gas.
  • Step 4 The cyclone separator 8 transports the medium and high temperature gas and the high temperature granular slag 6 to the waste heat recovery device.
  • the heat of the medium and high temperature gas and the high temperature granular slag 6 is recovered by the waste heat recovery device and used for sludge drying, high temperature steam preparation, and power generation. Or low-temperature hot water preparation.
  • Step 4.1.1 The wet sludge in the sludge tank 16 is pumped into the sludge pre-dryer 14 through the sludge pump 15.
  • Step 4.1.2 The sludge pre-dryer 14 mixes the wet sludge and the medium and high temperature gas and reverses heat exchange to form semi-dried sludge.
  • step 4.1.2 the wet tail gas generated when the wet sludge is mixed with the medium and high temperature gas is purified and discharged after being purified by the tail gas treatment component.
  • Step 4.1.3 The sludge pre-drying component transports the semi-dried sludge into the spiral mixer 9, and the cyclone separator 8 transports the high-temperature granular slag 6 into the spiral mixer 9.
  • the semi-dried sludge and The high-temperature granular slag 6 is mixed by the screw mixer 9 into a sludge mixture.
  • Step 4.1.4 The screw mixer 9 transports the sludge mixture to the sludge dryer 10, and the sludge dryer 10 dries the sludge mixture into dry sludge powder and slag particles and transports them to the sludge recovery module .
  • the temperature of the slag particles is below 200°C.
  • the wet tail gas generated by the sludge dryer 10 when the sludge mixture is dried is purified by the tail gas treatment component and then discharged.
  • Step 4.1.5 The sludge separator 13 of the sludge recovery component separates the dry sludge powder from the slag particles.
  • step 4.1.5 the wet tail gas generated when the sludge separator 13 separates dry sludge powder and slag particles is purified by the tail gas treatment component and then discharged.
  • Step 4.1.6 The sludge separator 13 transports the dry sludge powder into the dry sludge powder bin 12 for temporary storage.
  • Step 4.1.7 The sludge separator 13 transports the slag particles into the slag bin 11 for temporary storage.
  • the method for purifying and discharging wet exhaust gas from the exhaust gas treatment assembly is as follows: the exhaust gas processor 17 of the exhaust gas treatment assembly collects the wet exhaust gas from the sludge pre-dryer 14, the sludge dryer 10, and the sludge separator 13 and pre-treatment. After treatment (such as cyclone treatment, removing millimeter-level large particles of dust), it is deeply purified by the exhaust gas purifier 18. The exhaust gas after purification is discharged through the chimney 20 through the exhaust fan 19; the exhaust gas processor 17 and the exhaust gas purifier 18 are collected The micronized powder is pumped out through an external tanker.
  • the preparation steps of the high-temperature steam are:
  • Step 4.2.1 The cyclone 8 transports the high-temperature granular slag 6 to the high-temperature granular slag conveyor 21, and the high-temperature granular slag 6 is lifted by the high-temperature granular slag conveyor 21 and uniformly distributed from the upper inlet of the high-temperature granular slag heat exchanger 22 It is sent into the high-temperature granular slag heat exchanger 22, and the high-temperature granular slag 6 moves from top to bottom, and respectively contacts the cooling water in the coil and the bottom-up air in countercurrent heat exchange during the descending process.
  • Step 4.2.2 The heated high-temperature gas (300-600°C) is discharged from the top of the high-temperature granular slag heat exchanger 22 and sent to the boiler 23, and the cooled granular slag is discharged from the lower part of the high-temperature granular slag heat exchanger into the slag bin 11.
  • the temperature of the cooled granular slag is below 200°C.
  • Step 4.2.3 The external pipe network sends pure water to the economizer 24, and is preheated to above 80°C by the medium and low temperature (below 250°C) tail gas discharged from the boiler 23, and part of it is sent to the boiler 23 to be continuously heated and steamed. It is transformed into high-temperature steam (about 200-250°C), and the other part enters the coil of the high-temperature granular slag heat exchanger 22 to absorb the heat of the high-temperature granular slag 6.
  • Step 4.2.4 When the water in the coil vaporizes and rises to about 250°C, it enters the upper steam drum of the boiler 23, mixes with the steam generated by the boiler 23 itself, and merges into the external pipe network for use or power generation at the same level.
  • the preparation steps of the low-temperature hot water are:
  • Step 4.3.1 The cyclone 8 transports the high-temperature granular slag 6 to the high-temperature granular slag conveyor 21, and the high-temperature granular slag 6 is lifted by the high-temperature granular slag conveyor 21 and uniformly distributed from the upper inlet of the high-temperature granular slag heat exchanger 22 It is sent into the high-temperature granular slag heat exchanger 22, and the high-temperature granular slag 6 moves from top to bottom, and respectively contacts the cooling water in the coil and the bottom-up air in countercurrent heat exchange during the descending process.
  • Step 4.3.2 The heated low-temperature hot water (70-95°C) is discharged from the top of the high-temperature granular slag heat exchanger 22 and sent to the boiler 23, and the cooled granular slag is discharged from the lower part of the high-temperature granular slag heat exchanger.
  • Warehouse 11 The temperature of the cooled granular slag is below 200°C.
  • Step 4.3.3 The external pipe network sends part of the pure water into the boiler 23, and is heated to 70-95°C by the medium and high temperature gas (300-600°C) passing through the boiler 23, and the other part enters the high-temperature granular slag heat exchanger 22
  • the coil tube is used to absorb the heat of the high-temperature granular slag 6.
  • Step 4.3.4 The water in the coil absorbs heat and heats up and enters the upper steam drum of the boiler 23, mixes with the hot water generated by the boiler 23 itself, and merges it into the external pipe network for use as domestic water or cooling.
  • the blast furnace When the blast furnace is tapping, the blast furnace slag enters the main ditch from the tap hole along with the molten iron, and is divided by the slag stopper.
  • the slag at 1450-1550°C separates from the molten iron and enters the slag slag ditch.
  • the aerosol granulation nozzle assembly is granulated: the slag flow 1 flows out after being controlled by the slag flow controller 2, and the slag flow 1 is sprayed by the aerosol spray gun 5 during the falling process after leaving the slag flow controller 2
  • the blowing high-pressure gas mist is dispersed, granulated and initially cooled to form high-temperature granular slag 6 at 1000-1200°C and medium-temperature gas at 200-400°C.
  • the flow rate of the high-pressure gas mist is determined by the compressed air flow control valve 3 and the water volume control valve 4, and is automatically adjusted within a certain range with the size of the slag flow 1.
  • the medium-temperature airflow wraps the granulated high-temperature granular slag 6 through the deflector 7 and enters the waste heat recovery device.
  • the medium-temperature gas and the high-temperature granular slag 6 further mix and exchange heat during the process of passing through the deflector 7.
  • the gas temperature When the temperature rises to 300-500°C, a medium-high temperature gas is formed, the temperature of the high-temperature granular slag 6 drops to 900-1100°C, and the high-temperature granular slag 6 is completely solidified.
  • the aerosol granulated slag technology draws on the advantages of the gas quenching and water quenching slag technology.
  • the high vitrification rate of the slag retains the resource properties of the water quenched slag, and the dried slag reduces the cost of micronization and the transportation process.
  • the medium and high temperature gas and the high temperature granular slag 6 enter the cyclone separator 8.
  • the cyclone separator 8 has a high-efficiency separation capability and can separate most of the high temperature granular slag 6 from the medium and high temperature gas.
  • the medium and high temperature gas is led out from the upper part of the rotary separator 8 and enters the sludge pre-dryer 14, and the wet sludge pumped by the sludge pump 15 (wet converter dust removal sludge with moisture between 60-90wt%, namely OG Mud) conducts reverse contact heat exchange, the moisture of the sludge drops to about 50%, and the gas temperature drops to 200°C.
  • the 800-950°C high-temperature granular slag 6 collected by the cyclone separator 8 and the semi-dried sludge from the sludge pre-dryer 14 are stirred and mixed under the action of the spiral mixer 9, and the slag and sludge mixture is directly sent Into the sludge dryer 10, the slag and sludge directly contact and exchange heat in the sludge dryer 10, the mixing ratio of slag and sludge is 2:1--3:1, and the sludge is dried to the set moisture index (E.g. 6%), the temperature of the slag particles will drop below 200°C.
  • the dry sludge powder and slag will be separated by the sludge separator 13 and sent to the temporary silo, namely the slag silo 11 and the dry sludge. Warehouse 12, waiting for outbound transportation, for subsequent resource utilization.
  • the temperature of the wet tail gas generated by the sludge pre-dryer 14, the sludge dryer 10, and the sludge separator 13 is controlled to be above 200°C.
  • the cyclone treatment of the tail gas processor 17 the millimeter-level large particles of dust are removed.
  • the exhaust gas temperature is reduced to 150-200°C, after the exhaust gas purifier 18 removes more than 95% of all kinds of fine dust, it is pressurized by the exhaust fan 19 and discharged through the chimney 20 to reach the standard.
  • the exhaust gas purifier 18 can be a cloth bag or an electrostatic precipitator.
  • the fine powder collected by the exhaust gas processor 17 and the exhaust gas purifier 18 is regularly pumped out by the tanker and directly sent to the subsequent utilization unit.
  • the molten slag from the blast furnace enters the main ditch from the tap hole and is divided by the slag stopper.
  • the slag at 1450-1550°C separates from the molten iron and enters the slag ditch.
  • the aerosol granulation nozzle assembly is granulated: the slag flow 1 flows out after being controlled by the slag flow controller 2, and the slag flow 1 is sprayed by the aerosol spray gun 5 during the falling process after leaving the slag flow controller 2
  • the blowing high-pressure gas mist is dispersed, granulated and initially cooled to form high-temperature granular slag 6 at 1000-1200°C and medium-temperature gas at 200-400°C.
  • the flow rate of the high-pressure gas mist is determined by the compressed air flow control valve 3 and the water volume control valve 4, and is automatically adjusted within a certain range with the size of the slag flow 1.
  • the medium-temperature airflow wraps the granulated high-temperature granular slag 6 through the deflector 7 and enters the waste heat recovery device.
  • the medium-temperature gas and the high-temperature granular slag 6 further mix and exchange heat during the process of passing through the deflector 7, and the gas temperature rises.
  • a medium-high temperature gas is formed, the temperature of the high-temperature granular slag 6 drops to 800-1100°C, and the high-temperature granular slag 6 is completely solidified.
  • the aerosol granulated slag technology draws on the advantages of the gas quenching and water quenching slag technology.
  • the high vitrification rate of the slag retains the resource properties of the water quenched slag, and the dried slag reduces the cost of micronization and the transportation process.
  • Environmental impact, the high-temperature granular slag and medium-high temperature airflow generated during the granulation process create favorable conditions for heat energy recovery and utilization.
  • the medium and high temperature gas and the high temperature granular slag 6 enter the cyclone separator 8.
  • the cyclone separator 8 has high-efficiency separation capability, which can separate most of the high temperature granular slag 6 from the medium and high temperature gas.
  • the cyclone separator 8 separates 700
  • the high-temperature granular slag 6 at -950°C is transported to the upper part of the high-temperature granular slag heat exchanger 22 through the high-temperature conveyor 21.
  • the high-temperature granular slag 6 slowly descends in the high-temperature granular slag heat exchanger 22, and is connected to the coil in the process of descending.
  • the circulating water and the rising air flow from the lower part exchange heat in the opposite direction.
  • the high-temperature granular slag is cooled to about 200°C and sent to the lower slag bin 11. It is discharged from the top, merges with the medium and high temperature air flow discharged from the cyclone separator 8 and enters the boiler 23.
  • the pure water sent from the external pipe network first passes through the economizer 24, and is preheated to above 80°C by the medium and low temperature exhaust gas discharged from the boiler 23.
  • the gas in it is removed, and part of it is sent to the boiler 23 where it is heated by 300-600°C.
  • the air is heated and vaporized into steam at 200-250°C, and the other part enters the heat exchange coil in the high-temperature granular slag heat exchanger 22.
  • This part of water directly absorbs the heat of the high-temperature granular slag 6, and enters after the temperature rises to about 250°C.
  • the steam drum in the upper part of the boiler 23 is mixed with the steam generated by the boiler itself and then merged into the external pipe network for use or power generation at the same level.
  • the temperature of the wet exhaust gas discharged from the economizer 24 is controlled above 200°C. After the cyclone treatment of the exhaust gas processor 17, the millimeter-level large particles of dust are removed. The exhaust gas temperature is reduced to 150-200°C, and then the exhaust gas purifier 18 is deep. After purification, the dust content is less than 10 mg, and finally it is pressurized by the exhaust fan 19 and discharged through the chimney 20 to meet the standard.
  • the small amount of fine powder collected by the exhaust gas processor 17 and the exhaust gas purifier 18 is regularly pumped out by the tanker and directly sent to the subsequent utilization unit.
  • the blast furnace When the blast furnace is tapping, the blast furnace slag enters the main ditch from the tap hole along with the molten iron, and is divided by the slag stopper.
  • the slag at 1450-1550°C separates from the molten iron and enters the slag slag ditch.
  • the aerosol granulation nozzle assembly is granulated: the slag flow 1 flows out after being controlled by the slag flow controller 2, and the slag flow 1 is sprayed by the aerosol spray gun 5 during the falling process after leaving the slag flow controller 2
  • the blowing high-pressure gas mist is dispersed, granulated and initially cooled to form high-temperature granular slag 6 at 1000-1200°C and medium-temperature gas at 200-400°C.
  • the flow rate of the high-pressure gas mist is determined by the compressed air flow control valve 3 and the water volume control valve 4, and is automatically adjusted within a certain range with the size of the slag flow 1.
  • the medium-temperature gas wraps the granulated high-temperature granulated slag 6 through the deflector 7 and then enters the waste heat recovery component.
  • the medium-temperature gas and the high-temperature granular slag 6 further mix and exchange heat during the process of passing through the deflector 7.
  • the temperature rises to 300-500°C to form a medium-high temperature gas, and the temperature of the high-temperature granular slag 6 drops to 800-1100°C and is completely solidified.
  • the aerosol granulated slag technology draws on the advantages of the gas quenching and water quenching slag technology.
  • the high vitrification rate of the slag retains the resource properties of the water quenched slag, and the dried slag reduces the cost of micronization and the transportation process.
  • the medium and high temperature gas and the high temperature slag particles 6 enter the cyclone separator 8.
  • the cyclone separator 8 has a high-efficiency separation capability and can separate most of the high temperature slag particles 6 from the medium and high temperature gas.
  • the cyclone separator 8 separates 700
  • the high-temperature granular slag 6 at -950°C is transported to the upper part of the high-temperature granular slag heat exchanger 22 through the high-temperature conveyor 21.
  • the high-temperature granular slag 6 slowly descends in the high-temperature granular slag heat exchanger 22, and is connected to the coil in the process of descending.
  • the circulating water and the rising airflow from the lower part exchange heat in the reverse direction.
  • the high-temperature granular slag is cooled to about 200°C and sent to the lower slag bin 11, and the rising airflow is heated to 300-600°C and discharged from the top of the heat exchanger 22. It merges with the medium and high temperature air flow discharged from the cyclone separator 8 and enters the boiler 23.
  • Part of the pure water sent from the external pipe network is sent to the boiler 23 and heated by the hot air at 300-600°C into hot water at 70-95°C, and the other part enters the heat exchange coil in the high-temperature granular slag heat exchanger 22.
  • Part of the water directly absorbs the heat of the high-temperature granular slag 6, and enters the upper part of the boiler 23 after the temperature rises to about 70-95°C, mixes with the hot water generated by the boiler itself, and merges into the external pipe network for domestic water use or cooling.
  • the wet tail gas temperature of the exhaust gas discharged from the boiler 23 is controlled above 200°C. After the cyclone treatment of the tail gas processor 17, the millimeter-level large particles of dust are removed, the temperature is reduced to 150-200°C, and then the tail gas purifier 18 is deeply purified. , The dust content is less than 10mg, and finally it is pressurized by the exhaust fan 19 and discharged through the chimney 20 to reach the standard.
  • the small amount of fine powder collected by the exhaust gas processor 17 and the exhaust gas purifier 18 is regularly pumped out by the tanker and directly sent to the subsequent utilization unit.

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Abstract

本发明公开了一种高炉熔渣粒化和余热回收利用装置及方法，该装置包括气雾粒化喷嘴组件、导流器(7)、旋流分离器(8)和余热回收器；气雾粒化喷嘴组件包括熔渣控流器(2)、压缩空气流量控制阀(3)、水量控制阀(4)和气雾喷枪(5)；在导流器内实现中温气体与高温粒渣(6)混合换热及高温粒渣固化，并将换热后的中高温气体和高温粒渣导入旋流分离器；旋流分离器完成中高温气体和高温粒渣的分离，并将中高温气体和高温粒渣输送至余热回收器内。本发明实现高炉熔渣的完全颗粒化，将熔渣显热回收与污泥干化、高温蒸汽制备、发电、低温热水制备的有机耦合，实现熔渣粒化处理过程中中温气体和高温粒渣的余热回收，提高余热回收利用效率。

Description

高炉熔渣粒化和余热回收利用装置及方法 技术领域
本发明涉及一种冶金熔渣处理设备及方法，尤其涉及一种高炉熔渣粒化和余热回收利用装置及方法。
背景技术
高炉熔渣是高炉炼铁的主要副产物，吨铁产生的高炉熔渣为350公斤左右。高炉熔渣的出炉温度在1450℃～1550℃，吨渣携带的显热((1260-1880)×10 3kJ)相当于60kg标准煤的发热量，具有较高的回收价值。
目前，高炉熔渣的处理多采用水淬工艺，熔渣被高压水冲制成水渣，高品位的显热随之转移到80℃左右的水渣和废水中，失去回收利用价值。另外，每处理1吨熔渣需要消耗0.4～0.5吨水、同时排放大量富含H 2S、SO 2等污染物的废蒸汽。在后续资源化利用(如微粉化)时，还需要将水渣中8～15％的水分烘干，吨渣又需要消耗大约1000m 3的500℃的热风，造成了大量资源的浪费。
高炉熔渣是在高炉炼铁过程中，由矿石中的脉石、燃料中的灰分和溶剂(一般是石灰石)中的非挥发组分形成的高温熔体，温度在1450℃左右，主要的化学成分是：二氧化硅(SiO 2)、三氧化二铝(Al 2O 3)、氧化钙(CaO)、氧化镁(MgO)、氧化锰(MnO)、氧化铁(FeO)和硫等，其中二氧化硅(SiO 2)、三氧化二铝(Al 2O 3)与氧化钙(CaO)和氧化镁(MgO)的质量比在0.8-1.2左右。因此，高炉熔渣具有导热系数低、粘度随温度降低而急剧升高的特性，造成高炉熔渣换热慢，余热回收难度高。
熔渣颗粒的快速干式粒化能为回收热量创造条件，目前，熔渣快速干式粒化的工艺主要有风碎法和离心粒化法。风碎法因噪音大、易产生渣棉而未能在高炉熔渣的处理领域推广应用，只适用于部分流动性好的钢渣的处理。离心粒化主要采用转碟或转杯为粒化器，利用离心力将熔渣分散、碎裂成细小的熔滴以便快速冷却，保持冷却后渣粒的玻璃体含量和活性能够达到矿渣微粉原料的要求，但在炉渣结壳、粒化渣粒度不均匀、易产生渣棉等问题。
中国发明专利ZL 201410755689.9公开了一种高温熔渣余热回收系统及方法，该装置包括熔渣输送单元、熔渣粒化单元及余热回收单元，能回收高温熔渣的显热，但在余热回收过程中熔渣采用渣罐远距离输送，容易降温，需要另外的补热，能耗较高，余热回收效率较低。
中国发明专利ZL 201010566938.1公开了一种冶金熔渣干式粒化及热能回收系统，液态熔渣采用离心旋转和气流脉冲的方式进行干式粒化。在离心旋转盘的下方围绕离心旋转盘的转轴分别设置环形布置的气流喷嘴和雾化水喷嘴，在干式粒化装置的内侧壁设置水冷壁，在水冷壁下方设置环锥面流化装置，在干式粒化装置的底部设置环形流化床。通过该发明专利回收熔渣的余热利用局限于通过热空气/氮气转化成蒸汽或发电，效率低下。
污泥作为一种固体废弃物，已经成为继城市垃圾污染的第二大固体废物污染源。传统的污泥的主要处置方式有填埋、焚烧、排海、农用等。在工业污水、生活污水等污水处理领域中，污泥处理也普遍存在。随着技术的发展，现有技术的污泥处理可采用发酵、熔化、投加石灰、碳化等处理方式，但设备成本和能耗非常高，处理效率低下，也可能存在对空气、水源等的二次污染。
发明内容
本发明的目的在于提供一种高炉熔渣粒化和余热回收利用装置及方法，实现了高炉熔渣的完全颗粒化，并将熔渣显热回收与污泥干化、制备蒸汽和热水有机耦合，实现了熔渣粒化处理过程中中高温气体和高温粒渣的余热回收，大大提高了余热回收利用效率。
本发明是这样实现的：
一种高炉熔渣粒化和余热回收利用装置，其特征是：包括气雾粒化喷嘴组件、导流器、旋流分离器和余热回收器；
所述气雾粒化喷嘴组件包括熔渣控流器、压缩空气流量控制阀、水量控制阀和气雾喷枪；所述熔渣控流器与所述导流器的进渣口连接；所述压缩空气流量控制阀与所述气雾喷枪的气体进口连接；所述水量控制阀与所述气雾喷枪的液体进口连接；所述雾喷枪的喷嘴面向导流器的进口设置，用于通过气雾冲击通过所述熔渣控流器进入所述导流器的熔渣流，形成中温气体和表面初步固化的高温粒渣；
所述导流器用于使中温气体和表面初步固化的高温粒渣在其内部充分混合， 所述导流器的出口连接至旋流分离器的进料口，以使导流器内形成的完全固化的高温粒渣和中高温气体进入旋流分离器；
所述旋流分离器用于分离高温粒渣和中高温气体；其中，所述旋流分离器的出料口连接至余热回收器的进料口，用于将中高温气体和完全固化的高温粒渣输送至余热回收器内。
在一些实施方案中，本发明提供一种高炉熔渣粒化和余热回收利用装置，包括气雾粒化喷嘴组件、导流器、旋流分离器和余热回收器；
所述的气雾粒化喷嘴组件包括熔渣控流器、压缩空气流量控制阀、水量控制阀和气雾喷枪；熔渣流通过熔渣控流器控流后流入导流器的进渣口，高压气体通过压缩空气流量控制阀连接至气雾喷枪的气体进口，水通过水量控制阀连接至气雾喷枪的液体进口，气雾喷枪的喷嘴面向导流器的进口设置并通过气雾冲击熔渣流，形成中温气体和表面初步固化的高温粒渣；
所述的导流器的出口连接至旋流分离器的进料口，中温气体和表面初步固化的高温粒渣在导流器内充分混合，形成完全固化的高温粒渣和中高温气体后进入旋流分离器，通过旋流分离器完成高温粒渣和中高温气体的分离；旋流分离器的出料口连接至余热回收器的进料口，并将中高温气体和完全固化的高温粒渣输送至余热回收器内。
经所述的气雾粒化喷嘴组件气雾冲击熔渣流形成的中温气体的温度为200-400℃，表面初步固化的高温粒渣的温度为1000-1200℃；经导流器混合后的中高温气体的温度为300-500℃，完全固化的高温粒渣的温度为800-1100℃；经旋流分离器分离后的高温粒渣的温度为700-950℃，中高温气体的温度为350-550℃。
所述的余热回收器为污泥干化组件；污泥干化组件包括螺旋混料器、污泥干化器、污泥预干组件、渣泥回收组件和尾气处理组件；旋流分离器的出料口与螺旋混料器的第一进料口连接并将完全固化的高温粒渣输送至螺旋混料器内，旋流分离器的气雾口与污泥预干组件的气雾口连接并将中高温气体输送至污泥预干组件内，使中高温气体在污泥预干组件内与含湿污泥混合形成半干化污泥；污泥预干组件的出料口与螺旋混料器的第二进料口连接并将半干化污泥输送至螺旋混料器内，使半干化污泥与高温粒渣在螺旋混料器内混合成渣泥混合物；螺旋混料器的出料口与污泥干化器的进料口连接并将渣泥混合物输送至污泥干化器内，污泥干化器的出料口与渣泥回收组件的进料口连接并将干泥粉和渣粒输送至渣泥回收 组件内；尾气处理组件的进气口分别与污泥预干组件的出气口、污泥干化器的出气口和渣泥回收组件的出气口连接。
所述的余热回收器为高温蒸汽制备组件，高温蒸汽制备组件连接至旋流分离器并回收中高温气体和高温粒渣的热量，制备出200-250℃的高温蒸汽，高温蒸汽并入管网同级利用或发电；高温蒸汽制备组件的尾气出口连接有尾气处理组件。
在一些实施方案中，所述的高温蒸汽制备组件包括渣仓、尾气处理器、尾气净化器、排气风机、烟囱、高温输料机、高温粒渣换热器、锅炉和省煤器；
其中，高温输料机设置在旋流分离器的出料口与高温粒渣换热器的进料口之间，用于将旋流分离器分离出来的高温粒渣输送至高温粒渣换热器的上部；高温粒渣换热器内设有内置循环水的盘管，用于通过该盘管和从下向上升的气流与高温粒渣进行逆向换热；渣仓设置在位于高温粒渣换热器底部的出料口下方，用于接收降温后的粒渣；高温粒渣换热器的顶部设有气流口并连接至锅炉；省煤器与锅炉和高温粒渣换热器分别连接，以使经由外部管网送入省煤器的纯水被锅炉中排出的尾气预热到80℃以上，并被分成两部分，一部分被送入锅炉内，另一部分进入高温粒渣换热器的盘管，用于吸收高温粒渣的热量；尾气处理器的进气口与省煤器的尾气出口连接，尾气处理器的出气口与尾气净化器的进气口连接，尾气净化器的出气口通过排气风机连接至烟囱，用于尾气的净化和排放。
在一些实施方案中，当盘管内的水汽化并升高到250℃左右时进入锅炉上部汽包内，与锅炉本身生成的蒸汽混合后并入外部管网。
所述的余热回收器为低温热水制备组件；低温热水制备组件连接至旋流分离器并回收中高温气体和高温粒渣的热量，制备出70-95℃的低温热水，低温热水送用户同级利用或制冷；低温热水制备组件的尾气出口连接有尾气处理组件。
在一些实施方案中，所述的低温热水制备组件包括渣仓、尾气处理器、尾气净化器、排气风机、烟囱、高温输料机、高温粒渣换热器和锅炉；
其中，高温输料机设置在旋流分离器的出料口与高温粒渣换热器的进料口之间，用于将旋流分离器分离出来的高温粒渣输送至高温粒渣换热器的上部；高温粒渣换热器内设有内置循环水的盘管，用于通过该盘管和从下向上升的气流与高温粒渣进行逆向换热；渣仓设置在位于高温粒渣换热器底部的出料口下方，用于接收降温后的粒渣；高温粒渣换热器的顶部设有气流口并连接至锅炉；锅炉和高温粒渣换热器分别与外部管网连接，用于接收纯水，以在所述锅炉内和高温粒渣 换热器内进行换热；尾气处理器的进气口与锅炉的尾气出口连接，尾气处理器的出气口与尾气净化器的进气口连接，尾气净化器的出气口通过排气风机连接至烟囱，用于尾气的净化和排放。
所述的尾气处理组件包括尾气处理器、尾气净化器、排气风机和烟囱，尾气处理器的进气口分别通过管道连接至污泥预干组件的出气口、污泥干化器的出气口、渣泥回收组件的出气口、锅炉的尾气出口和省煤器的尾气出口，尾气处理器的出气口与尾气净化器的进气口连接，尾气净化器的出气口通过排气风机连接至烟囱。
一种高炉熔渣粒化和余热回收利用方法，包括以下步骤：
步骤1：高炉熔渣与铁水分离后进入熔渣渣沟，形成的熔渣流经过熔渣控流器控流后流入导流器内；
步骤2：调节压缩空气流量控制阀和水量控制阀，在气雾喷枪内形成高压气雾并通过喷嘴喷出，使高压气雾冲击流入导流器内的熔渣流，形成中温气体以及表面初步固化的高温粒渣；
步骤3：中温气体以及表面初步固化的高温粒渣通过导流器混合换热，形成完全固化的高温粒渣和中高温气体并输送至旋流分离器，通过旋流分离器分离高温粒渣和中高温气体；
步骤4：旋流分离器将中高温气体和高温粒渣输送至余热回收器，中高温气体和高温粒渣的热量通过余热回收器回收并用于污泥干化、高温蒸汽制备、发电或低温热水制备。
在一些实施方案中，所述方法中，经所述的气雾粒化喷嘴组件气雾冲击熔渣流形成的中温气体的温度为200-400℃，表面初步固化的高温粒渣的温度为1000-1200℃；经导流器混合后的中高温气体的温度为300-500℃，完全固化的高温粒渣的温度为800-1100℃；经旋流分离器分离后的高温粒渣的温度为700-950℃，中高温气体的温度为350-550℃。
在一些实施方案中，所述的污泥干化的步骤包括：
步骤4.1.1：污泥池内的含湿污泥通过污泥泵泵送入污泥预干器中；
步骤4.1.2：污泥预干器将含湿污泥和中高温气体混合并逆向换热，形成半干化污泥；
步骤4.1.3：污泥预干组件将半干化污泥输送至螺旋混料器内，旋流分离器将 高温粒渣输送至螺旋混料器内，半干化污泥和高温粒渣通过螺旋混料器混合成渣泥混合物；
步骤4.1.4：螺旋混料器将渣泥混合物输送至污泥干化器内，污泥干化器将渣泥混合物干化成干泥粉和渣粒并输送至渣泥回收组件内；
步骤4.1.5：渣泥回收组件的渣泥分离器将干泥粉与渣粒分离；
步骤4.1.6：渣泥分离器将干泥粉输送入干泥粉仓暂存；
步骤4.1.7：渣泥分离器将渣粒输送入渣仓暂存。
所述方法还包括：利用尾气处理组件净化和排放含湿尾气，包括：尾气处理组件的尾气处理器从污泥预干器、污泥干化器和渣泥分离器收集含湿尾气并预处理后通过尾气净化器深度净化，净化达标后的尾气通过排气风机经烟囱排放；尾气处理器和尾气净化器中收集的微粉通过外部罐车抽出。
在一些实施方案中，所述的高温蒸汽的制备步骤包括：
步骤4.2.1：旋流分离器将高温粒渣输送到高温粒渣输送器，高温粒渣被高温粒渣输送器提升并从高温粒渣换热器的上部入口均匀的送入高温粒渣换热器内，高温粒渣自上而下移动，下降过程中分别与盘管内的冷却水和自下而上的空气逆流接触换热；
步骤4.2.2：被加热后的蒸汽从高温粒渣换热器顶部排出并送入锅炉，冷却后的粒渣从高温粒渣换热器下部排入渣仓；
步骤4.2.3：外部管网将纯水送入省煤器，并被锅炉中排出的尾气预热到80℃以上，一部分送入锅炉被继续加热、汽化成200-250℃的蒸汽，另一部分进入高温粒渣换热器的盘管，用于吸收高温粒渣的热量；
步骤4.2.4：盘管内的水汽化并升高到250℃左右时进入锅炉上部汽包内，与锅炉本身生成的蒸汽混合后并入外部管网。
在一些实施方案中，所述的低温热水的制备步骤包括：
步骤4.3.1：旋流分离器将高温粒渣输送到高温粒渣输送器，高温粒渣被高温粒渣输送器提升并从高温粒渣换热器的上部入口均匀的送入高温粒渣换热器内，高温粒渣自上而下移动，下降过程中分别与盘管内的冷却水和自下而上的空气逆流接触换热；
步骤4.3.2：被加热后的70-95℃的低温热水从高温粒渣换热器顶部排出并送入锅炉，冷却后的粒渣从高温粒渣换热器下部排入渣仓；
步骤4.3.3：外部管网将纯水一部分送入锅炉，并被经过锅炉中的气体加热到70-95℃，另一部分进入高温粒渣换热器的盘管，用于吸收高温粒渣的热量；
步骤4.3.4：盘管内的水吸热升温后进入锅炉上部汽包内，与锅炉本身生成的热水混合后并入外部管网。
在一些实施方案中，所述方法还包括：利用尾气处理组件净化和排放含湿尾气，包括：尾气处理组件的尾气处理器从污泥预干器、污泥干化器和渣泥分离器收集含湿尾气并预处理后通过尾气净化器深度净化，净化达标后的尾气通过排气风机经烟囱排放；尾气处理器和尾气净化器中收集的微粉通过外部罐车抽出。
本发明与现有技术相比，具有如下有益效果：
1、本发明高炉熔渣粒化和余热回收利用装置将高炉熔渣通过气雾冲击以及旋流分离后形成完全固化的高温粒渣和中高温气体，粒渣化的粒度均匀，且避免了粒化过程中渣棉的产生；分离后的高温粒渣和中高温气体能直接应用于污泥干化的各步序中，余热回收效率高，也可用于高温蒸汽发电、热水回收等。
2、本发明高炉熔渣粒化和余热回收利用装置将熔渣显热回收与污泥干化有机耦合，高炉熔渣快速、安全粒化的同时实现了污泥的高效干化，不仅大大提高了余热回收利用效率，且降低了余热回收成本，同时解决了污泥干化低效且高成本的问题。
3、本发明高炉熔渣粒化和余热回收利用方法将高炉熔渣完全粒化成适合高效余热回收的高温粒渣，并通过对中高温气体和高温粒渣的余热回收，使熔渣的显热得到最大限度的同级利用，能产生较好的经济效益和社会效益。
综上所述，本发明实现了高炉熔渣的完全颗粒化且粒度均匀，将熔渣显热回收与污泥干化有机耦合，实现了熔渣处理过程中中高温气体和高温粒渣的余热回收，大大提高了余热回收利用效率，具有较好的经济效益和社会效益，可以在各种大小型号高炉的渣处理领域推广应用，前景广阔。
附图说明
图1是本发明高炉熔渣粒化和余热回收利用装置中实施例1的工艺流程图；
图2是本发明高炉熔渣粒化和余热回收利用装置中实施例2的工艺流程图；
图3是本发明高炉熔渣粒化和余热回收利用装置中实施例3的工艺流程图；
图4是本发明高炉熔渣粒化和余热回收利用方法的流程图。图中，虚线为气 流输送管道，实线为渣粒输送管道。
图中，1熔渣流，2熔渣控流器，3压缩空气流量控制阀，4水量控制阀，5气雾喷枪，6渣粒，7导流器，8旋流分离器，9螺旋混料器，10污泥干化器，11渣仓，12干泥粉仓，13渣泥分离器，14污泥预干器，15污泥泵，16污泥池，17尾气处理器，18尾气净化器，19排气风机，20烟囱，21高温输料机，22高温粒渣换热器，23锅炉，24省煤器。
具体实施方式
下面结合附图和具体实施例对本发明作进一步说明。
请参见附图1，一种高炉熔渣粒化和余热回收利用装置，包括气雾粒化喷嘴组件、导流器7、旋流分离器8和余热回收器；
所述的气雾粒化喷嘴组件包括熔渣控流器2、压缩空气流量控制阀3、水量控制阀4和气雾喷枪5；熔渣流1通过熔渣控流器2控流后流入导流器7的进渣口，高压气体通过压缩空气流量控制阀3连接至气雾喷枪5的气体进口，少量的水通过水量控制阀4连接至气雾喷枪5的液体进口，气雾喷枪5的喷嘴面向导流器7的进口设置并通过气雾冲击熔渣流1，形成中温气体和表面初步固化的高温粒渣6；气雾粒化喷嘴组件利用高压气体和少量的水破碎、粒化、快冷高炉熔渣，使高炉熔渣的温度从1450℃快速降至1000-1200℃，优选为1100℃，完成高炉熔渣的表面初步固化，颗粒渣的粒度均匀。
所述的导流器7的出口连接至旋流分离器8的进料口。中温气体和表面初步固化的高温粒渣6在导流器内充分混合，形成完全固化的高温粒渣6和中高温气体后进入旋流分离器8，通过旋流分离器8完成高温粒渣6和中高温气体的分离。旋流分离器8的出料口连接至余热回收器的进料口，并将中高温气体和完全固化的高温粒渣6输送至余热回收器内。表面初步固化的高温粒渣6和中温气体在导流器7内充分混合，并进入旋流分离器8内充分混合、换热，使高温粒渣6实现完全固化，避免了渣棉的产生，更利于热量的回收，同时实现中高温气流和高温粒渣6的分离，分离后的高温粒渣6的温度降至700-950℃，优选为800-850℃，便于余热回收组件对其进行余热回收利用。
所述的熔渣流1的温度为1450-1550℃；经气雾粒化喷嘴组件气雾冲击熔渣流1形成的中温气体的温度为200-400℃，表面初步固化的高温粒渣6的温度为 1000-1200℃，优选为1100℃；经导流器7混合后的中高温气体的温度为300-500℃，优选为400℃，完全固化的高温粒渣6的温度为800-1100℃，优选为950℃；经旋流分离器8分离后的高温粒渣6的温度为700-950℃，优选为800-850℃，中高温气体的温度为350-550℃。
所述的余热回收器为污泥干化组件，可直接用于污泥干化。解决了污泥处理困难且能耗较高的问题，污泥干化组件包括螺旋混料器9、污泥干化器10、污泥预干组件、渣泥回收组件和尾气处理组件；旋流分离器8的出料口与螺旋混料器9的第一进料口连接并将完全固化的高温粒渣6输送至螺旋混料器9内，旋流分离器8的气雾口与污泥预干组件的气雾口连接并将中高温气体输送至污泥预干组件内，使中高温气体在污泥预干组件内与含湿污泥混合形成半干化污泥；污泥预干组件的出料口与螺旋混料器9的第二进料口连接并将半干化污泥输送至螺旋混料器9内，使半干化污泥与完全固化的高温粒渣6在螺旋混料器9内混合成渣泥混合物；螺旋混料器9的出料口与污泥干化器10的进料口连接并将渣泥混合物输送至污泥干化器10内，渣泥混合物在污泥干化器10内进一步混合干化成干泥粉和低温渣粒，污泥干化器10的出料口与渣泥回收组件的进料口连接并将干泥粉和渣粒输送至渣泥回收组件内；尾气处理组件的进气口分别与污泥预干组件的出气口、污泥干化器10的出气口和渣泥回收组件的出气口连接。
所述的污泥预干组件包括污泥预干器14、污泥泵15和污泥池16，污泥池16的出料口通过管道经污泥泵15连接至污泥预干器14的进料口，使污泥池16内的含湿污泥输送至污泥预干器14内；污泥预干器14上设有气雾口并与旋流分离器8的气雾口连接，且污泥预干器14的气雾口和进料口分别位于污泥预干器14的两端，使中高温气体与污泥相对移动并逆向换热，中高温气体与污泥的接触面积大，混合充分，换热效率高；污泥预干器14上设有出气口并与尾气处理组件的进气口连接。污泥池16内的含湿污泥通过污泥泵15泵送到污泥预干器14内，并在污泥预干器14内与中高温气体换热形成半干化污泥。
所述的渣泥回收组件包括渣仓11、干泥粉仓12和渣泥分离器13；渣泥分离器13设有进料口、两个出料口和出气口，污泥干化器10的出料口连接至渣泥分离器13的进料口，渣泥分离器13的两个出料口分别连接至渣仓11和干泥粉仓12；尾气处理组件的进气口连接至渣泥分离器13的出气口。干泥粉和渣粒的混合物进入渣泥分离器13后通过渣泥分离器13分离，并将干泥粉暂存在干泥粉仓12内， 渣粒暂存在渣仓11内，便于后期回收处理，渣泥分离器13内的含湿尾气进入尾气处理组件。
所述的尾气处理组件包括尾气处理器17、尾气净化器18、排气风机19和烟囱20，尾气处理器17的进气口分别通过管道连接至污泥预干组件中污泥预干器14的出气口、污泥干化器10的出气口、渣泥回收组件中渣泥分离器13的出气口、锅炉23的尾气出口和省煤器24的尾气出口，尾气处理器17的出气口与尾气净化器18的进气口连接，尾气净化器18的出气口通过排气风机19连接至烟囱20；尾气处理器17收集含湿尾气并进行初步净化处理，经初步净化后的尾气被送入尾气净化器18进行深度净化处理，再通过排气风机19经烟囱20排放。
所述的尾气处理器17和尾气净化器18的下部均设有排料口，排料口通过管道外接罐车，通过外部罐车可将尾气处理器17和尾气净化器18过滤下来少量微粉抽出，确保尾气处理器17和尾气净化器18的正常运行，也便于微粉的后续利用和处理。
请参见附图2，所述的余热回收器为高温蒸汽制备组件，可用于制备高温蒸汽、发电。高温蒸汽制备组件连接至旋流分离器8并回收中高温气体和高温粒渣6的热量，制备出200-250℃的高温蒸汽，高温蒸汽并入管网同级利用或发电；高温蒸汽制备组件的省煤器24的尾气出口连接有尾气处理组件。
所述的高温蒸汽制备组件包括渣仓11、尾气处理器17、尾气净化器18、排气风机19、烟囱20、高温输料机21、高温粒渣换热器22、锅炉23和省煤器24；高温输料机21设置在旋流分离器8的出料口与高温粒渣换热器22的进料口之间，旋流分离器8分离出来的高温粒渣6通过高温输料机21输送至高温粒渣换热器22的上部并缓慢下降，高温粒渣换热器22内设有内置循环水的盘管，高温粒渣6与盘管和从下向上升的气流进行逆向换热，降温至100℃；渣仓11设置在位于高温粒渣换热器22底部的出料口下方，降温后的粒渣被送入渣仓11用于后期处理；高温粒渣换热器22的顶部设有气流口并连接至锅炉23；省煤器24与锅炉23连接，外部管网将纯水送入省煤器24，并被锅炉23中排出的中低温尾气(250℃以下)预热到80℃以上，一部分送入锅炉23被继续加热、汽化成高温蒸汽(200-250℃)，另一部分进入高温粒渣换热器22的盘管，用于吸收高温粒渣6的热量，当盘管内的水汽化并升高到250℃左右时进入锅炉23上部汽包内，与锅炉23本身生成的蒸汽混合后并入外部管网，同级使用或发电；尾气处理器17的进气口与省煤器24 的尾气出口连接，尾气处理器17的出气口与尾气净化器18的进气口连接，尾气净化器18的出气口通过排气风机19连接至烟囱20，用于尾气的净化和排放。
请参见附图3，所述的余热回收器为低温热水制备组件，可用于制备生活热水。低温热水制备组件连接至旋流分离器8并回收中高温气体和高温粒渣6的热量，制备出70-95℃的低温热水，低温热水送用户同级利用或制冷；低温热水制备组件的锅炉23的尾气出口连接有尾气处理组件。
所述的低温热水制备组件包括渣仓11、尾气处理器17、尾气净化器18、排气风机19、烟囱20、高温输料机21、高温粒渣换热器22和锅炉23；高温输料机21设置在旋流分离器8的出料口与高温粒渣换热器22的进料口之间，旋流分离器8分离出来的高温粒渣6通过高温输料机21输送至高温粒渣换热器22的上部并缓慢下降，高温粒渣换热器22内设有内置循环水的盘管，高温粒渣6与盘管和从下向上升的气流进行逆向换热，降温至200℃以下；渣仓11设置在位于高温粒渣换热器22底部的出料口下方，降温后的粒渣被送入渣仓11用于后期处理；高温粒渣换热器22的顶部设有气流口并连接至余热锅炉23；外部管网将纯水一部分送入锅炉23被加热到70-95℃，另一部分进入高温粒渣换热器22的盘管，用于吸收高温粒渣6的热量，当盘管内的水吸热升温后进入锅炉23上部汽包内，与锅炉23本身生成的热水混合后并入外部管网，作为生活用水使用或制冷；尾气处理器17的进气口与锅炉23的尾气出口连接，尾气处理器17的出气口与尾气净化器18的进气口连接，尾气净化器18的出气口通过排气风机19连接至烟囱20，用于尾气的净化和排放。
本文中，尾气净化器18可采用布袋或静电除尘器。
请参见附图1，所述的旋流分离器8设有进料口、出料口和气雾口，旋流分离器8的进料口连接导流器7的出料口，旋流分离器8的出料口与螺旋混料器9的第一进料口连接，旋流分离器8的气雾口与污泥预干组件的污泥预干器14的气雾口连接，可通过旋流高效分离高温渣粒6和中高温气体。
请参见附图4，一种高炉熔渣粒化和余热回收方法，包括以下步骤：
步骤1：高炉熔渣与铁水分离后进入熔渣渣沟，熔渣流1经过熔渣控流器2控流后流入导流器7内。
步骤2：调节压缩空气流量控制阀3和水量控制阀4，在气雾喷枪5内形成高压气雾并通过喷嘴喷出，使高压气雾冲击流入导流器7内的熔渣流1，形成中温气 体以及表面初步固化的高温粒渣6。
步骤3：中温气体和表面初步固化的高温粒渣6通过导流器7混合、换热后，形成完全固化的高温粒渣6和中高温气体并输送至旋流分离器8，通过旋流分离器8旋流分离高温粒渣6与中高温气体。
步骤4：旋流分离器8将中高温气体和高温粒渣6输送至余热回收器，中高温气体和高温粒渣6的热量通过余热回收器回收并用于污泥干化、高温蒸汽制备、发电或低温热水制备。
所述的污泥干化的步骤是：
步骤4.1.1：污泥池16内的含湿污泥通过污泥泵15泵送入污泥预干器14中。
步骤4.1.2：污泥预干器14将含湿污泥和中高温气体混合并逆向换热，形成半干化污泥。
在步骤4.1.2中，含湿污泥与中高温气体混合时产生的含湿尾气通过尾气处理组件净化后排放。
步骤4.1.3：污泥预干组件将半干化污泥输送至螺旋混料器9内，旋流分离器8将高温粒渣6输送至螺旋混料器9内，半干化污泥和高温粒渣6通过螺旋混料器9混合成渣泥混合物。
步骤4.1.4：螺旋混料器9将渣泥混合物输送至污泥干化器10内，污泥干化器10将渣泥混合物干化成干泥粉和渣粒并输送至渣泥回收组件内。
在所述的步骤4.1.4中，渣粒的温度为200℃以下。
在所述的步骤4.1.4中，污泥干化器10在干化渣泥混合物时产生的含湿尾气通过尾气处理组件净化后排放。
步骤4.1.5：渣泥回收组件的渣泥分离器13将干泥粉与渣粒分离。
在步骤4.1.5中，渣泥分离器13分离干泥粉和渣粒时产生的含湿尾气通过尾气处理组件净化后排放。
步骤4.1.6：渣泥分离器13将干泥粉输送入干泥粉仓12暂存。
步骤4.1.7：渣泥分离器13将渣粒输送入渣仓11暂存。
所述的尾气处理组件净化和排放含湿尾气的方法是：尾气处理组件的尾气处理器17从污泥预干器14、污泥干化器10和渣泥分离器13收集含湿尾气并预处理(如旋流处理，去除毫米级别的大颗粒粉尘)后通过尾气净化器18深度净化，净化达标后的尾气通过排气风机19经烟囱20排放；尾气处理器17和尾气净化器18 中收集的微粉通过外部罐车抽出。
所述的高温蒸汽的制备步骤是：
步骤4.2.1：旋流分离器8将高温粒渣6输送到高温粒渣输送器21，高温粒渣6被高温粒渣输送器21提升并从高温粒渣换热器22的上部入口均匀的送入高温粒渣换热器22内，高温粒渣6自上而下移动，下降过程中分别与盘管内的冷却水和自下而上的空气逆流接触换热。
步骤4.2.2：被加热后的高温气体(300-600℃)从高温粒渣换热器22顶部排出并送入锅炉23，冷却后的粒渣从高温粒渣换热器下部排入渣仓11。所述的冷却后的粒渣温度200℃以下。
步骤4.2.3：外部管网将纯水送入省煤器24，并被锅炉23中排出的中低温(250℃以下)尾气预热到80℃以上，一部分送入锅炉23被继续加热、汽化成高温蒸汽(约200-250℃)，另一部分进入高温粒渣换热器22的盘管，用于吸收高温粒渣6的热量。
步骤4.2.4：盘管内的水汽化并升高到250℃左右时进入锅炉23上部汽包内，与锅炉23本身生成的蒸汽混合后并入外部管网，同级使用或发电。
所述的低温热水的制备步骤是：
步骤4.3.1：旋流分离器8将高温粒渣6输送到高温粒渣输送器21，高温粒渣6被高温粒渣输送器21提升并从高温粒渣换热器22的上部入口均匀的送入高温粒渣换热器22内，高温粒渣6自上而下移动，下降过程中分别与盘管内的冷却水和自下而上的空气逆流接触换热。
步骤4.3.2：被加热后的低温热水(70－95℃)从高温粒渣换热器22顶部排出并送入锅炉23，冷却后的粒渣从高温粒渣换热器下部排入渣仓11。所述的冷却后的粒渣温度200℃以下。
步骤4.3.3：外部管网将纯水一部分送入锅炉23，并被经过锅炉23中的中高温气体(300-600℃)加热到70-95℃，另一部分进入高温粒渣换热器22的盘管，用于吸收高温粒渣6的热量。
步骤4.3.4：盘管内的水吸热升温后进入锅炉23上部汽包内，与锅炉23本身生成的热水混合后并入外部管网，作为生活用水使用或制冷。
实施例1：
请参见附图1，高炉出铁时，高炉熔渣伴随着铁水从出铁口进入主沟，经挡 渣器分割，1450-1550℃的熔渣与铁水分离并进入熔渣渣沟，再进入气雾粒化喷嘴组件进行粒化：熔渣流1经过熔渣控流器2控流后流出，熔渣流1在脱离熔渣控流器2后在下落的过程中被气雾喷枪5喷吹的高压气雾吹散、粒化和初步冷却，形成1000-1200℃的高温粒渣6和200-400℃的中温气体。高压气雾的流量由压缩空气流量控制阀3和水量控制阀4确定，并随熔渣流1的大小在一定范围内自动调节。中温气流卷裹着粒化后的高温粒渣6通过导流器7导流进入余热回收器，中温气体和高温粒渣6在通过导流器7的过程中进一步的混合、换热，气体温度上升到300-500℃，形成中高温气体，高温粒渣6温度下降到900-1100℃，高温粒渣6完全固化。气雾粒化熔渣技术汲取了气淬和水淬熔渣技术的优点，高玻璃化率的粒渣保留了水淬渣的资源化物性，干燥的粒渣降低了微粉化成本和运输过程的环境影响，粒化过程中产生的高温粒渣和中高温气流为热能回收利用创造了有利条件。
中高温气体和高温粒渣6进入旋流分离器8，旋流分离器8具备高效分离能力，可以将绝大部分高温粒渣6从中高温气体中分离出来。中高温气体从旋转分离器8的上部导出并进入污泥预干器14，与污泥泵15泵入的含湿污泥(水分在60-90wt％之间的湿法转炉除尘泥，即OG泥)进行逆向接触换热，污泥水分下降到50％左右，气体温度下降到200℃。旋流分离器8收集下来的800-950℃的高温粒渣6与污泥预干器14出来的半干化污泥在螺旋混料器9的作用下被搅拌混合，渣泥混合物直接被送入污泥干化器10，渣与泥在污泥干化器10内直接接触换热，渣、泥混配比例为2:1--3:1，污泥被烘干到设定水分指标(如6％)，渣粒温度则下降到200℃以下，烘干后干泥粉和粒渣经过渣泥分离器13的分离，并分别送入临时料仓，即渣仓11和干泥粉仓12，等候外运，用于后续的资源化利用。
污泥预干化器14、污泥干化器10和渣泥分离器13产生的含湿尾气温度控制在200℃以上，经过尾气处理器17的旋流处理，去除毫米级别的大颗粒粉尘，尾气温度降至150-200℃，再经过尾气净化器18的深度净化去除95％以上的各类微细粉尘后，由排气风机19加压，并通过烟囱20达标排放。尾气净化器18可采用布袋或静电除尘器。
尾气处理器17和尾气净化器18收集下来的微粉，定时由罐车抽出，直接送入后续利用单元。
实施例2：
请参见附图2，高炉出铁时，高炉熔渣伴随着铁水从出铁口进入主沟，经挡渣器分割，1450-1550℃的熔渣与铁水分离并进入熔渣渣沟，再进入气雾粒化喷嘴组件进行粒化：熔渣流1经过熔渣控流器2控流后流出，熔渣流1在脱离熔渣控流器2后在下落的过程中被气雾喷枪5喷吹的高压气雾吹散、粒化和初步冷却，形成1000-1200℃的高温粒渣6和200-400℃的中温气体。高压气雾的流量由压缩空气流量控制阀3和水量控制阀4确定，并随熔渣流1的大小在一定范围内自动调节。中温气流卷裹着粒化后的高温粒渣6通过导流器7导流进入余热回收器，中温气体和高温粒渣6在通过导流器7的过程中进一步混合、换热，气体温度上升到300-500℃，形成中高温气体，高温粒渣6温度下降到800-1100℃，高温粒渣6完全固化。气雾粒化熔渣技术汲取了气淬和水淬熔渣技术的优点，高玻璃化率的粒渣保留了水淬渣的资源化物性，干燥的粒渣降低了微粉化成本和运输过程的环境影响，粒化过程中产生的高温粒渣和中高温气流为热能回收利用创造了有利条件。
中高温气体和高温粒渣6进入旋流分离器8，旋流分离器8具备高效分离能力，可以将绝大部分高温粒渣6从中高温气体中分离出来，旋流分离器8分离出来的700-950℃的高温粒渣6经过高温输料机21输送到高温粒渣换热器22的上部，高温粒渣6在高温粒渣换热器22中缓慢下降，下降过程中分别与盘管中的循环水和下部上升的气流逆向换热，高温粒渣被冷却到200℃左右后送入下部的渣仓11，上升的气流被加热到300-600℃后从高温粒渣换热器22的顶部排出，与旋流分离器8排出的中高温气流汇合后进入锅炉23。
外部管网送来的纯水首先经过省煤器24，被从锅炉23排放出来的中低温尾气预热到80℃以上，排除其中的气体，一部分送入锅炉23，被300-600℃的热空气加热、汽化成200-250℃的蒸汽，另一部分进入高温粒渣换热器22中的换热盘管，这部分水直接吸收高温粒渣6的热量，温度升高到250℃左右后进入锅炉23上部汽包内，与锅炉本身生成的蒸汽混合后并入外部管网，同级使用或发电。
省煤器24排出的含湿尾气温度控制在200℃以上，经过尾气处理器17的旋流处理，除去毫米级别的大颗粒粉尘，尾气温度降至150-200℃，再经过尾气净化器18深度净化后，粉尘含量小于10mg，最后由排气风机19加压，通过烟囱20达标排放。
尾气处理器17和尾气净化器18收集下来的少量微粉，定时由罐车抽出，直 接送后续利用单元。
实施例3：
请参见附图3，高炉出铁时，高炉熔渣伴随着铁水从出铁口进入主沟，经挡渣器分割，1450-1550℃的熔渣与铁水分离并进入熔渣渣沟，再进入气雾粒化喷嘴组件进行粒化：熔渣流1经过熔渣控流器2控流后流出，熔渣流1在脱离熔渣控流器2后在下落的过程中被气雾喷枪5喷吹的高压气雾吹散、粒化和初步冷却，形成1000-1200℃的高温粒渣6和200-400℃的中温气体。高压气雾的流量由压缩空气流量控制阀3和水量控制阀4确定，并随熔渣流1的大小在一定范围内自动调节。中温气体卷裹着粒化后的高温粒渣6通过导流器7导流后进入余热回收组件，中温气体和高温粒渣6在通过导流器7的过程中进一步的混合、换热，气体温度上升到300-500℃，形成中高温气体，高温粒渣6温度下降到800-1100℃并完全固化。气雾粒化熔渣技术汲取了气淬和水淬熔渣技术的优点，高玻璃化率的粒渣保留了水淬渣的资源化物性，干燥的粒渣降低了微粉化成本和运输过程的环境影响，粒化过程中产生的高温粒渣和中温气流为热能回收利用创造了有利条件。
中高温气体和高温渣粒6进入旋流分离器8，旋流分离器8具备高效分离能力，可以将绝大部分高温渣粒6从中高温气体中分离出来，旋流分离器8分离出来的700-950℃的高温粒渣6经过高温输料机21输送到高温粒渣换热器22的上部，高温粒渣6在高温粒渣换热器22中缓慢下降，下降过程中分别与盘管中的循环水和下部上升的气流逆向换热，高温粒渣被冷却到200℃左右后送入下部的渣仓11，上升的气流被加热到300-600℃后从换热器22的顶部排出，与旋流分离器8排出的中高温气流汇合后进入锅炉23。
外部管网送来的纯水一部分送入锅炉23，被300-600℃的热空气加热成70－95℃的热水，另一部分进入高温粒渣换热器22中的换热盘管，这部分水直接吸收高温粒渣6的热量，温度升高到70-95℃左右后进入锅炉23上部，与锅炉本身生成的热水混合后并入外部管网，供生活用水使用或制冷。
锅炉23排出的尾气含湿尾气温度控制在200℃以上，经过尾气处理器17的旋流处理，除去毫米级别的大颗粒粉尘，温度降至150-200℃，再经过尾气净化器18深度净化后，粉尘含量小于10mg，最后由排气风机19加压，通过烟囱20达标排放。
尾气处理器17和尾气净化器18收集下来的少量微粉，定时由罐车抽出，直 接送后续利用单元。
以上仅为本发明的较佳实施例而已，并非用于限定本发明的保护范围，因此，凡在本发明的精神和原则之内所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。

Claims (15)

  1. 一种高炉熔渣粒化和余热回收利用装置，其特征是：包括气雾粒化喷嘴组件、导流器(7)、旋流分离器(8)和余热回收器；
    所述气雾粒化喷嘴组件包括熔渣控流器(2)、压缩空气流量控制阀(3)、水量控制阀(4)和气雾喷枪(5)；所述熔渣控流器(2)与所述导流器(7)的进渣口连接；所述压缩空气流量控制阀(3)与所述气雾喷枪(5)的气体进口连接；所述水量控制阀(4)与所述气雾喷枪(5)的液体进口连接；所述气雾喷枪(5)的喷嘴面向导流器(7)的进口设置，用于通过气雾冲击通过所述熔渣控流器(2)进入所述导流器(7)的熔渣流，形成中温气体和表面初步固化的高温粒渣(6)；
    所述导流器(7)用于使中温气体和表面初步固化的高温粒渣(6)在其内部充分混合，所述导流器(7)的出口连接至旋流分离器(8)的进料口，以使导流器(7)内形成的完全固化的高温粒渣(6)和中高温气体进入旋流分离器(8)；
    所述旋流分离器(8)用于分离高温粒渣(6)和中高温气体；其中，所述旋流分离器(8)的出料口连接至余热回收器的进料口，用于将中高温气体和完全固化的高温粒渣(6)输送至余热回收器内。
  2. 根据权利要求1所述的高炉熔渣粒化和余热回收利用装置，其特征是：熔渣流(1)通过熔渣控流器(2)控流后流入导流器(7)的进渣口，高压气体通过压缩空气流量控制阀(3)连接至气雾喷枪(5)的气体进口，水通过水量控制阀(4)连接至气雾喷枪(5)的液体进口，气雾喷枪(5)的喷嘴面向导流器(7)的进口设置并通过气雾冲击熔渣流(1)，形成中温气体和表面初步固化的高温粒渣(6)。
  3. 根据权利要求1所述的高炉熔渣粒化和余热回收利用装置，其特征是：经所述的气雾粒化喷嘴组件气雾冲击熔渣流(1)形成的中温气体的温度为200-400℃，表面初步固化的高温粒渣(6)的温度为1000-1200℃；经导流器(7)混合后的中高温气体的温度为300-500℃，完全固化的高温粒渣(6)的温度为800-1100℃；经旋流分离器(8)分离后的高温粒渣(6)的温度为700-950℃，中高温气体的温度为350-550℃。
  4. 根据权利要求1所述的高炉熔渣粒化和余热回收利用装置，其特征是：所述的余热回收器为污泥干化组件；污泥干化组件包括螺旋混料器(9)、污泥干化 器(10)、污泥预干组件、渣泥回收组件和尾气处理组件；旋流分离器(8)的出料口与螺旋混料器(9)的第一进料口连接，用于将完全固化的高温粒渣(6)输送至螺旋混料器(9)内，旋流分离器(8)的气雾口与污泥预干组件的气雾口连接，用于将中高温气体输送至污泥预干组件内，使中高温气体在污泥预干组件内与含湿污泥混合形成半干化污泥；污泥预干组件的出料口与螺旋混料器(9)的第二进料口连接，用于将半干化污泥输送至螺旋混料器(9)内，使半干化污泥与高温粒渣(6)在螺旋混料器(9)内混合成渣泥混合物；螺旋混料器(9)的出料口与污泥干化器(10)的进料口连接，用于将渣泥混合物输送至污泥干化器(10)内；污泥干化器(10)的出料口与渣泥回收组件的进料口连接，用于将干泥粉和渣粒输送至渣泥回收组件内；尾气处理组件的进气口分别与污泥预干组件的出气口、污泥干化器(10)的出气口和渣泥回收组件的出气口连接。
  5. 根据权利要求1所述的高炉熔渣粒化和余热回收利用装置，其特征是：所述的余热回收器为高温蒸汽制备组件；其中，所述高温蒸汽制备组件连接至旋流分离器(8)，用于回收中高温气体和高温粒渣(6)的热量，以制备出200-250℃的高温蒸汽；所述高温蒸汽制备组件的尾气出口连接有尾气处理组件。
  6. 根据权利要求5所述的高炉熔渣粒化和余热回收利用装置，其特征是：所述的高温蒸汽制备组件包括渣仓(11)、尾气处理器(17)、尾气净化器(18)、排气风机(19)、烟囱(20)、高温输料机(21)、高温粒渣换热器(22)、锅炉(23)和省煤器(24)；
    其中，高温输料机(21)设置在旋流分离器(8)的出料口与高温粒渣换热器(22)的进料口之间，用于将旋流分离器(8)分离出来的高温粒渣(6)输送至高温粒渣换热器(22)的上部；高温粒渣换热器(22)内设有内置循环水的盘管，用于通过该盘管和从下向上升的气流与高温粒渣(6)进行逆向换热；渣仓(11)设置在位于高温粒渣换热器(22)底部的出料口下方，用于接收降温后的粒渣；高温粒渣换热器(22)的顶部设有气流口并连接至锅炉(23)；省煤器(24)与锅炉(23)和高温粒渣换热器(22)分别连接，以使经由外部管网送入省煤器(24)的纯水被锅炉(23)中排出的尾气预热到80℃以上，并被分成两部分，一部分被送入锅炉(23)内，另一部分进入高温粒渣换热器(22)的盘管，用于吸收高温粒渣(6)的热量；尾气处理器(17)的进气口与省煤器(24)的尾气出口连接，尾气处理器(17)的出气口与尾气净化器(18)的进气口连接，尾气净化器(18) 的出气口通过排气风机(19)连接至烟囱(20)，用于尾气的净化和排放。
  7. 根据权利要求6所述的高炉熔渣粒化和余热回收利用装置，其特征是：当盘管内的水汽化并升高到250℃左右时进入锅炉(23)上部汽包内，与锅炉(23)本身生成的蒸汽混合后并入外部管网。
  8. 根据权利要求1所述的高炉熔渣粒化和余热回收利用装置，其特征是：所述的余热回收器为低温热水制备组件；其中，所述低温热水制备组件连接至旋流分离器(8)并回收中高温气体和高温粒渣(6)的热量，制备出70-95℃的低温热水；低温热水制备组件的尾气出口连接有尾气处理组件。
  9. 根据权利要求8所述的高炉熔渣粒化和余热回收利用装置，其特征是：所述的低温热水制备组件包括渣仓(11)、尾气处理器(17)、尾气净化器(18)、排气风机(19)、烟囱(20)、高温输料机21、高温粒渣换热器(22)和锅炉(23)；
    其中，高温输料机21设置在旋流分离器(8)的出料口与高温粒渣换热器(22)的进料口之间，用于将旋流分离器(8)分离出来的高温粒渣(6)输送至高温粒渣换热器(22)的上部；高温粒渣换热器(22)内设有内置循环水的盘管，用于通过该盘管和从下向上升的气流与高温粒渣(6)进行逆向换热；渣仓(11)设置在位于高温粒渣换热器(22)底部的出料口下方，用于接收降温后的粒渣；高温粒渣换热器(22)的顶部设有气流口并连接至锅炉(23)；锅炉(23)和高温粒渣换热器(22)分别与外部管网连接，用于接收纯水，以在所述锅炉(23)内和高温粒渣换热器(22)内进行换热；尾气处理器(17)的进气口与锅炉(23)的尾气出口连接，尾气处理器(17)的出气口与尾气净化器(18)的进气口连接，尾气净化器(18)的出气口通过排气风机(19)连接至烟囱(20)，用于尾气的净化和排放。
  10. 根据权利要求4所述的高炉熔渣粒化和余热回收利用装置，其特征是：所述的尾气处理组件包括尾气处理器(17)、尾气净化器(18)、排气风机(19)和烟囱(20)；其中，尾气处理器(17)的进气口分别通过管道连接至污泥预干组件的出气口、污泥干化器(10)的出气口和渣泥回收组件的出气口，尾气处理器(17)的出气口与尾气净化器(18)的进气口连接，尾气净化器(18)的出气口通过排气风机(19)连接至烟囱(20)。
  11. 一种采用权利要求1所述的高炉熔渣粒化和余热回收利用装置的粒化和余热回收方法，其特征是：包括以下步骤：
    步骤1：高炉熔渣与铁水分离后进入熔渣渣沟，形成的熔渣流(1)经过熔渣控流器(2)控流后流入导流器(7)内；
    步骤2：调节压缩空气流量控制阀(3)和水量控制阀(4)，在气雾喷枪(5)内形成高压气雾并通过喷嘴喷出，使高压气雾冲击流入导流器(7)内的熔渣流(1)，形成中温气体以及表面初步固化的高温粒渣(6)；
    步骤3：中温气体以及表面初步固化的高温粒渣(6)通过导流器(7)混合换热，形成完全固化的高温粒渣(6)和中高温气体并输送至旋流分离器(8)，通过旋流分离器(8)分离高温粒渣(6)和中高温气体；
    步骤4：旋流分离器(8)将中高温气体和高温粒渣(6)输送至余热回收器，中高温气体和高温粒渣(6)的热量通过余热回收器回收并用于污泥干化、高温蒸汽制备、发电或低温热水制备。
  12. 根据权利要求11所述的高炉熔渣粒化和余热回收利用装置的粒化和余热回收方法，其特征是：经所述的气雾粒化喷嘴组件气雾冲击熔渣流(1)形成的中温气体的温度为200-400℃，表面初步固化的高温粒渣(6)的温度为1000-1200℃；经导流器(7)混合后的中高温气体的温度为300-500℃，完全固化的高温粒渣(6)的温度为800-1100℃；经旋流分离器(8)分离后的高温粒渣(6)的温度为700-950℃，中高温气体的温度为350-550℃。
  13. 根据权利要求11所述的高炉熔渣粒化和余热回收利用装置的粒化和余热回收方法，其特征是，所述的污泥干化的步骤包括：
    步骤4.1.1：污泥池(16)内的含湿污泥通过污泥泵(15)泵送入污泥预干器(14)中；
    步骤4.1.2：污泥预干器(14)将含湿污泥和中高温气体混合并逆向换热，形成半干化污泥；
    步骤4.1.3：污泥预干组件将半干化污泥输送至螺旋混料器(9)内，旋流分离器(8)将高温粒渣(6)输送至螺旋混料器(9)内，半干化污泥和高温粒渣(6)通过螺旋混料器(9)混合成渣泥混合物；
    步骤4.1.4：螺旋混料器(9)将渣泥混合物输送至污泥干化器(10)内，污泥干化器(10)将渣泥混合物干化成干泥粉和渣粒并输送至渣泥回收组件内；
    步骤4.1.5：渣泥回收组件的渣泥分离器(13)将干泥粉与渣粒分离；
    步骤4.1.6：渣泥分离器(13)将干泥粉输送入干泥粉仓(12)暂存；
    步骤4.1.7：渣泥分离器(13)将渣粒输送入渣仓(11)暂存。
    所述方法还包括：利用尾气处理组件净化和排放含湿尾气，包括：尾气处理组件的尾气处理器(17)从污泥预干器(14)、污泥干化器(10)和渣泥分离器(13)收集含湿尾气并预处理后通过尾气净化器(18)深度净化，净化达标后的尾气通过排气风机(19)经烟囱(20)排放；尾气处理器(17)和尾气净化器(18)中收集的微粉通过外部罐车抽出。
  14. 根据权利要求11所述的高炉熔渣粒化和余热回收利用装置的粒化和余热回收方法，其特征是，所述的高温蒸汽的制备步骤包括：
    步骤4.2.1：旋流分离器(8)将高温粒渣(6)输送到高温粒渣输送器(21)，高温粒渣(6)被高温粒渣输送器(21)提升并从高温粒渣换热器(22)的上部入口均匀的送入高温粒渣换热器(22)内，高温粒渣(6)自上而下移动，下降过程中分别与盘管内的冷却水和自下而上的空气逆流接触换热；
    步骤4.2.2：被加热后的蒸汽从高温粒渣换热器(22)顶部排出并送入锅炉(23)，冷却后的粒渣从高温粒渣换热器下部排入渣仓(11)；
    步骤4.2.3：外部管网将纯水送入省煤器(24)，并被锅炉(23)中排出的尾气预热到80℃以上，一部分送入锅炉(23)被继续加热、汽化成200-250℃的蒸汽，另一部分进入高温粒渣换热器(22)的盘管，用于吸收高温粒渣(6)的热量；
    步骤4.2.4：盘管内的水汽化并升高到250℃左右时进入锅炉(23)上部汽包内，与锅炉(23)本身生成的蒸汽混合后并入外部管网。
  15. 根据权利要求11所述的高炉熔渣粒化和余热回收利用装置的粒化和余热回收方法，其特征是，所述的低温热水的制备步骤包括：
    步骤4.3.1：旋流分离器(8)将高温粒渣(6)输送到高温粒渣输送器(21)，高温粒渣(6)被高温粒渣输送器(21)提升并从高温粒渣换热器(22)的上部入口均匀的送入高温粒渣换热器(22)内，高温粒渣(6)自上而下移动，下降过程中分别与盘管内的冷却水和自下而上的空气逆流接触换热；
    步骤4.3.2：被加热后的70-95℃的低温热水从高温粒渣换热器(22)顶部排出并送入锅炉(23)，冷却后的粒渣从高温粒渣换热器下部排入渣仓(11)；
    步骤4.3.3：外部管网将纯水一部分送入锅炉(23)，并被经过锅炉(23)中的气体加热到70-95℃，另一部分进入高温粒渣换热器(22)的盘管，用于吸收高温粒渣(6)的热量；
    步骤4.3.4：盘管内的水吸热升温后进入锅炉(23)上部汽包内，与锅炉(23)本身生成的热水混合后并入外部管网。
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