WO2015176570A1 - 一种发电机组高水分、低热值褐煤干燥和水回收方法及其装置 - Google Patents

一种发电机组高水分、低热值褐煤干燥和水回收方法及其装置 Download PDF

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WO2015176570A1
WO2015176570A1 PCT/CN2015/073512 CN2015073512W WO2015176570A1 WO 2015176570 A1 WO2015176570 A1 WO 2015176570A1 CN 2015073512 W CN2015073512 W CN 2015073512W WO 2015176570 A1 WO2015176570 A1 WO 2015176570A1
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coal
drying
nitrogen
steam
gas
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PCT/CN2015/073512
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English (en)
French (fr)
Inventor
赵旭
窦岩
詹仲福
谭永鹏
史晋文
申涛
令永功
杨巍
张岩
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天华化工机械及自动化研究设计院有限公司
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Priority to EP15795478.5A priority Critical patent/EP3147614B1/en
Priority to JP2016568817A priority patent/JP6343033B2/ja
Priority to US15/312,908 priority patent/US10365040B2/en
Publication of WO2015176570A1 publication Critical patent/WO2015176570A1/zh

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
    • F26B21/005—Drying-steam generating means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C21/00—Disintegrating plant with or without drying of the material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/34—Other details of the shaped fuels, e.g. briquettes
    • C10L5/36—Shape
    • C10L5/366—Powders
    • C—CHEMISTRY; METALLURGY
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    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K3/00—Feeding or distributing of lump or pulverulent fuel to combustion apparatus
    • F23K3/02—Pneumatic feeding arrangements, i.e. by air blast
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B20/00—Combinations of machines or apparatus covered by two or more of groups F26B9/00 - F26B19/00
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/22—Controlling the drying process in dependence on liquid content of solid materials or objects
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/04—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour circulating over or surrounding the materials or objects to be dried
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2270/00—Specifically adapted fuels
    • C10L2270/04—Specifically adapted fuels for turbines, planes, power generation
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    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/02—Combustion or pyrolysis
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    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/08—Drying or removing water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/143—Injection, e.g. in a reactor or a fuel stream during fuel production of fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/145—Injection, e.g. in a reactor or a fuel stream during fuel production of air
    • C—CHEMISTRY; METALLURGY
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    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/146—Injection, e.g. in a reactor or a fuel stream during fuel production of water
    • C—CHEMISTRY; METALLURGY
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    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/28—Cutting, disintegrating, shredding or grinding
    • C—CHEMISTRY; METALLURGY
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    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/46—Compressors or pumps
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/52—Hoppers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/545—Washing, scrubbing, stripping, scavenging for separating fractions, components or impurities during preparation or upgrading of a fuel
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    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/547—Filtration for separating fractions, components or impurities during preparation or upgrading of a fuel
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    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/58—Control or regulation of the fuel preparation of upgrading process
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    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/60—Measuring or analysing fractions, components or impurities or process conditions during preparation or upgrading of a fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2201/00—Pretreatment of solid fuel
    • F23K2201/10—Pulverizing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2201/00—Pretreatment of solid fuel
    • F23K2201/20—Drying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/006—Fuel distribution and transport systems for pulverulent fuel

Definitions

  • the invention relates to a high-moisture, low-calorie lignite drying and water recovery method for a generator set and a device thereof.
  • the device can increase the calorific value of high-moisture lignite, meet the power generation requirements, and recover the water in the lignite as a supplementary water source for the power plant, reducing water consumption and saving energy.
  • the milling system of the traditional coal-fired power plant uses a coal mill (conventional medium-speed coal mill and fan coal mill) to pass the hot flue gas of 150-300 °C after the coal-fired boiler economizer for milling and drying. And then blown into the boiler for combustion use.
  • this method has a low degree of dryness and cannot directly achieve high-moisture lignite to meet power generation requirements, and it is impossible to recover moisture in lignite.
  • the coal burning system and the milling system of the above-mentioned conventional coal-fired power plant are two independent units, and the dried coal is transported to the coal bunker of the milling system through a scraping machine, a belt conveyor, a bucket lifter and the like, and the existing problems thereof Yes:
  • the temperature of the pulverized coal after drying reaches 60-80 °C, and a large amount of dust and steam are generated during the transportation process.
  • a large amount of dust and steam are generated during the transportation process.
  • due to the large amount of fine powder and low moisture it is easy to generate a large amount of dust by belt or scraper conveying. It not only pollutes the environment, but also has a poor operating environment, and the fine coal powder is easy to catch fire naturally, and even serious accidents such as flash explosion may occur, which affects the stable use of the conveying equipment.
  • the hot coal with the temperature of 60-80 °C passes through the conveying link, and the coal temperature is reduced to 30-60 °C before entering the coal-pulverized mechanism powder.
  • the heat carried by the hot coal is wasted, according to the calculation of the waste. The heat accounts for 5-20% of the energy required by the milling system.
  • the present invention provides a high-moisture, low-calorie lignite drying and water recovery device for a generator set, including a steam tube rotary dryer, a washing and cooling tower, Coal mill, first bag type dust collector, second bag type dust collector, steam condenser, weighing buffer tank, water ring vacuum pump, venturi ejector pump, wet coal bunker, nitrogen heater and pulverized coal collecting tank;
  • the input end of the steam tube rotary dryer is connected to the wet coal bunker, the upper end of the other end is connected to the first bag type dust remover, and the lower part is connected to the weighing buffer bin, the upper part of the first bag type dust remover and the a washing and cooling tower is connected, the weighing buffer tank is connected to the coal mill, one side of the coal mill is connected to the nitrogen heater, and the top of the coal mill is connected to the second bag type dust collector, the second bag type
  • the upper part of the dust collector is connected to the washing and cooling tower, the other side is connected to the inlet of the nitrogen heater, and the lower part of the second bag type dust collector is connected to the pulverized coal collecting tank; the upper part of the first bag type dust remover and the washing A cooling tower is connected, and a lower portion is connected to the pulverized coal collecting tank; one side of the washing cooling tower is connected to the nitrogen heater.
  • the above-mentioned generator set high moisture, low calorific value lignite drying and water recovery device the bottom of the wash cooling tower is connected to the first wash circulation pump and the second wash circulation pump, and the top thereof is connected to the steam condenser.
  • the above-mentioned generator set high moisture, low calorific value lignite drying and water recovery device the top of the steam condenser is connected with a water ring vacuum pump, the middle portion of the steam condenser is provided with a cooling water inlet, and the upper part and the bottom part are respectively provided with cooling water
  • the water return is connected to the bottom of the condensate recovery tank.
  • the above-mentioned generator set high moisture, low calorific value lignite drying and water recovery device, a carrier gas heater is connected to the other side of the washing and cooling tower, and the carrier gas heater is connected to the input end of the steam tube rotary dryer .
  • the above-mentioned generator set high moisture, low calorific value lignite drying and water recovery device the pulverized coal collection tank is connected to the venturi ejector through a second metering rotary valve, and the venturi ejector side is connected to the conveying fan and conveyed
  • the fan is connected to the coal-fired boiler 25 and the other side is open to the atmosphere.
  • the above-mentioned high-moisture, low-calorie lignite drying and water recovery device of the generator set has a rotary joint at the end of the steam tube rotary dryer, the upper part of which is connected with the pumping cylinder of the steam turbine, and the lower part is connected with the condensate storage tank.
  • the above-mentioned generator set high moisture, low calorific value lignite drying and water recovery device the condensate storage tank is connected to a condensate pump, and the condensate pump is connected to a condenser, and the condenser is connected to the deaerator, the division The oxygen generator is connected to the boiler drum.
  • the present invention also provides a high moisture, low calorific value lignite drying and water recovery method for a generator set, comprising the following steps:
  • Step 1 Drying first, crushing the wet coal, passing through the wet coal bunk and entering the steam tube rotary dryer. After heating and drying under heating steam and dry carrier gas for a certain period of time, a certain proportion of water is obtained. Coal particles B and a drying gas F at a certain temperature; the dry tail gas is sent to the first bag type dust remover for dust removal, and the tail gas D and the coal powder T containing water vapor are obtained, and the coal powder is directly sent to the collecting tank, and at the same time The tail gas D is sent to the washing cooling tower;
  • Step 2 secondary drying, milling, the coal particles B are sent to a buffer bin and then sent to a coal mill, under a predetermined condition for milling for a predetermined time, to obtain dried coal powder C; After the nitrogen gas P is heated to a predetermined temperature by the nitrogen heater, a part of the nitrogen gas P is sent to the coal mill, the coal particles B are dried and powdered to obtain the coal powder C; and another part of the nitrogen gas P passes through the sealing fan.
  • the tail gas G discharged from the top of the coal mill is sent to the second bag type dust collector for collection, and the coal powder C and the exhaust gas H after dust removal are obtained, wherein the coal powder C is directly sent to the coal powder
  • the collection tank is collected, a part of the exhaust gas H is sent back to the nitrogen heater to be heated to a preset temperature, and then input to the coal mill, and another part of the exhaust gas H is sent to the washing cooling tower for treatment;
  • Step 3 Cooling and dehumidifying the exhaust gas D and the exhaust gas H in the washing and cooling tower, forming a bottom liquid J at the bottom of the washing cooling tower, and performing the vacuum flashing and cooling of the bottom liquid J to obtain the steam, and then input the steam condenser after dehumidification. Condensation, clean water M has been formed, and the clean water M is sent to the condensed water recovery tank for storage, while the non-condensable gas that cannot be condensed is discharged into the air;
  • Step 4 a part of the nitrogen gas E discharged from the side of the washing cooling tower is input into the carrier gas heater, and after heating, is input to the input end of the steam tube rotary dryer for use as a dry carrier gas; another part of the nitrogen gas is input to the nitrogen gas for heating. In the device, it is heated and input into the coal mill, and used as a medium for drying and milling, and a nitrogen closed circulation system has been formed;
  • Step 5 The pulverized coal T and the pulverized coal C are mixed in the pulverized coal collecting tank and then input into the venturi ejector pump, and mixed with the air, and the boiler 25 is burned;
  • the high moisture and low calorific value lignite drying and water recovery method of the generator set in the first step, the moisture content of the wet coal is 25% to 62%, and the wet coal is broken into a diameter of 20 mm or less.
  • the above-mentioned high-moisture, low-calorie lignite drying and water recovery method of the generator set further includes, in step 1, the wet coal entering the steam tube rotary dryer from the wet coal bunk through the metering belt scale and the rotary sealing valve.
  • the above-mentioned high-moisture, low-calorie lignite drying and water recovery method of the generator set is in the first step, the hot steam pressure of the heating steam is 0.3-2.0 MPa, the temperature is 120-360 ° C, and the temperature of the dry carrier gas is less than 120 ° C.
  • the carrier gas of the dry carrier gas is 15000-35000 Nm3/h, and the heating drying time is 30-60 minutes.
  • the above-mentioned high-moisture, low-calorie lignite drying and water recovery method of the generator set is in step one, the coal particles
  • the moisture content of B is 15% or less, and the temperature of the drying gas F is 90-110 °C.
  • the high-moisture and low-calorie lignite drying and water recovery method of the generator set is sent to the first bag type dust remover under the condition of a pressure of 200-500 Pa and a temperature of 90-110 ° C in the first step.
  • the high-moisture and low-calorie lignite drying and water recovery method of the generator set further includes: after the coal particles B are sent into the buffer bin, the weighting device disposed in the middle of the buffer tank and the lower metering rotary valve are metered and then sent. Into the coal mill.
  • the high moisture and low calorific value lignite drying and water recovery method of the generator set is in the second step, the preset condition is hot air pressure of 2000-6000 Pa, temperature of 180-200 ° C, preset time of 6-25 S, coal powder C
  • the moisture content is 2 to 5% or less.
  • step two the high-moisture and low-calorie lignite drying and water recovery method of the generator set is carried out in step two, the nitrogen gas P is heated to 180-200 ° C by a nitrogen heater, and 90% of the nitrogen gas P is sent to the coal mill, 10%. The nitrogen gas P is sent to the coal mill for sealing through a sealed fan.
  • step two the high-moisture, low-calorie lignite drying and water recovery method of the generator set is carried out in step two, 15% of the exhaust gas H is sent back to the nitrogen heater and heated to 180-200 ° C, and then input into the coal mill, and 85% of the Exhaust gas H is sent to a wash cooling tower for treatment.
  • the temperature of the bottom liquid J is 80 to 90 °C.
  • the high moisture and low calorific value lignite drying and water recovery method of the generator set in the third step, the bottom liquid J after the flash cooling and cooling enters the distributor of the washing and cooling tower through the liquid level control system, and is reversed again with the exhaust gas D and the exhaust gas H.
  • the cooling medium of the condenser is circulating cooling water, after the water vapor in the exhaust gas D and the exhaust gas H is recovered, the remaining nitrogen gas E is returned to the primary and secondary drying cycles.
  • the temperature of the nitrogen gas E discharged from the side of the washing and cooling tower is 45 to 65 ° C, wherein 35% of the nitrogen gas is fed into the carrier gas heater.
  • the temperature of the nitrogen gas E discharged from the side of the washing and cooling tower is 45 to 65 ° C, wherein 35% of the nitrogen gas is fed into the carrier gas heater.
  • 65% of nitrogen E is input into the nitrogen heater, heated to 180 ⁇ 200 ° C and then input into the coal mill
  • a nitrogen closed loop system has been formed, and a loss of nitrogen circulation of 5% or less is supplemented by the outside of the system;
  • coal The powder T and the pulverized coal C are mixed in the pulverized coal collecting tank, discharged through a metering rotary valve, and then entered into the venturi ejector pump, and mixed with the air, and the boiler 25 is burned.
  • the above-mentioned genset high moisture, low calorific value lignite drying and water recovery method The heating medium of the carrier gas preheater, the steam rotary dryer and the nitrogen heater are all extracted from the steam turbine.
  • the high moisture lignite is dried by a steam tube rotary dryer, and the lignite having a moisture content of up to 61.3% can be fully loaded to generate electricity, which can meet the requirements of the coal-fired power plant, and the inferior coal that cannot be used can be converted into a power capable of generating electricity.
  • Coal can make effective use of low-quality coal and broaden the space for resource utilization.
  • the invention can recover 95% of the water in the high-moisture lignite, and is turned into clean water by washing, flashing, dehumidifying and condensing, and is used as a supplementary water circulation of the power plant, thereby saving precious water resources.
  • the heat source of the invention adopts steam turbine extraction, and utilizes the cold source loss of the system (that is, the latent heat of condensation after using high-pressure high-temperature steam to work), which not only greatly reduces the energy consumption of the drying system, but also greatly reduces the power generation of the generator set. Power consumption coal consumption.
  • the invention integrates the drying system and the milling system into one, and the steam tube rotary dryer and the coal mill are arranged in a one-to-one manner, that is, the outlet of the steam tube rotary dryer is directly connected to the coal mill through the buffer tank, and after drying. After the coal powder is buffered, it enters the coal milling mechanism powder, which not only saves the heat lost during the coal powder transportation process, but also eliminates the intermediate long-distance transportation link between the traditional drying system and the coal grinding system, shortening the process and effectively avoiding the transportation and transportation dust pollution. , waste and spontaneous combustion.
  • the invention eliminates the complicated transportation link in the middle, and is replaced only by the buffer bin and the metering rotary valve, and at the same time simplifies the dry front coal preparation system, which saves the coal bunker construction investment of the original milling system and greatly reduces the production cost.
  • the invention utilizes the drying function of the traditional milling system, and divides the drying system into two stages, one is steam pipe rotary drying, the second is drying system of the milling system, and the moisture of high moisture brown coal can be reduced to 2 to 5 %, greatly improving the calorific value of lignite.
  • the coal drying system of the invention can realize the circulating drying of the inert gas, and the washing cooling tower recovers the water vapor in the dry tail gas into clean water, and the discharged nitrogen gas is returned to the first-stage drying system and the second-stage drying and milling system after heating, and becomes Drying carrier gas and secondary drying and milling heat source make the drying system realize closed circuit circulation and reduce energy consumption.
  • the oxygen content of the drying system is completely controllable, and the exhaust gas after drying (including a large amount of water vapor) is directly discharged after dust collection. Into the atmosphere, the heat and steam contained in the exhaust gas are recycled. The dry tail gas is no longer discharged into the atmosphere, and the power plant coal drying system is safer and more environmentally friendly.
  • the invention has small investment, low energy consumption, high economic value and is easy to implement.
  • Figure 1 is a process flow diagram of the present invention in which the dashed box is a conventional generator set.
  • a high-moisture, low-calorie lignite drying and water recovery device for a generator set mainly includes a steam tube rotary dryer 9, a washing and cooling tower 6, a coal mill 14, a first bag filter 21, Second bag type dust collector 23, condenser 19, weighing buffer chamber 12, water ring vacuum pump 18, venturi ejector
  • the input end of the steam tube rotary dryer 9 is connected to the wet coal bunker 3 through the metering belt weigher 7 and the rotary sealing valve 8, and the other end of the other end is connected with a first bag type dust remover 21, and the lower part is provided with a weighing buffer bin 12.
  • the upper side of the first bag filter 21 is connected to the washing and cooling tower 6 through the second circulating air 20; the weighing buffer tank 12 is connected to the coal mill 14 through the first metering rotary valve 13; one side of the coal mill 14 passes The nitrogen heater 11 is connected to the fourth circulation fan 10, the other side is connected to the sealing fan 15, the top of the coal mill 14 is provided with a second bag type dust collector 23, and the upper side of the second bag type dust collector 23 is passed through the second cycle.
  • the fan 24 is connected to the washing and cooling tower 6, the other side is connected to the inlet of the nitrogen heater 11 through the fifth circulating fan 16, and the lower portion is connected to the pulverized coal collecting tank 27 through the second double-layer electric flapping valve 26; the first bag type dust removing
  • the upper portion of the device 21 is connected to the washing and cooling tower 6 through the first circulating fan 20, and the lower portion is connected to the pulverized coal collecting tank 27 through the first double-layer electric flapping valve 22;
  • the third side of the washing and cooling tower 6 passes through the third circulating fan 2 and the carrier gas Heater 1 is connected, and the other side passes through the fourth circulating air 10 and the nitrogen heater 11 is connected, and has a washing circulation pump 4 and a second washing circulation pump 5 at the bottom thereof, the top of which is connected to the steam condenser 17; the top of the steam condenser 17 is connected to the water ring vacuum pump 18, and the middle portion of the steam condenser 17 is provided with cooling water.
  • the inlet has a cooling water return port at the upper part and the bottom part, and a condensed water recovery tank 19 connected to the bottom;
  • the carrier gas heater 1 is connected to the input end of the steam tube rotary dryer 9;
  • the pulverized coal collecting tank 27 is rotated by the second metering
  • the valve 28 is connected to the venturi ejector 29;
  • the venturi ejector 29 is connected to the delivery fan 30,
  • the delivery fan 30 is connected to the coal-fired boiler 25, and the other side is connected to the atmosphere;
  • at the end of the steam tube rotary dryer 9 The upper end of the rotary joint 32 is connected to the pumping cylinder of the steam turbine 35, the lower portion is connected to the condensate storage tank 33, the condensate storage tank 33 is connected to the condensate pump 34, the condensate pump 34 is connected to the condenser 36, and the condenser 36 is connected.
  • the deaerator 37 is connected, and the deaerator 37 is connected to
  • the carrier gas heater 1 functions to heat the steam new liquid and the low pressure steam, and deliver it to the steam tube rotary dryer 9.
  • the wet coal bunker 3 is used to supply a hopper of a steam tube rotary dryer 9 wet brown coal.
  • the functions of the two washing and circulating pumps are to store the bottom liquid stored in the washing and cooling tower 6 under the action of the pump, and the circulation is sent to the flashing section of the top of the washing and cooling tower 6 for vacuum flashing; the function of the washing and cooling tower 6 is
  • the circulating fan is sent to the steam water containing the steam, the nitrogen tail gas and the top of the tower to be cooled and lowered in the tower, and the steam is reversely contacted in the tower for cooling and dehumidification.
  • the metering belt weigher 7 functions to pass the wet coal silo 3 wet coal through metering, and is supplied to the steam tube rotary dryer 9 by the rotary sealing valve 8.
  • the function of the rotary seal valve 8 is to input the wet coal metered by the metering belt scale 7 into the steam tube rotary dryer 9 relatively tightly.
  • the steam tube rotary dryer 9 is an inclined rotary cylinder.
  • a plurality of tubes are arranged in the cylinder, and the tubes are arranged in a concentric circle manner according to a concentric circle of 2 to 7 layers, steam is taken inside the tube, coal is taken outside the tube, a coal particle inlet and a carrier gas inlet are arranged at the input end, and a coal particle outlet and an exhaust gas are arranged at the output end.
  • the nitrogen heater 11 is used to feed the washing cooling tower 6 with a low pressure nitrogen gas for heating.
  • the function of the buffer tank 12 is to adjust and equalize the coal particles dried by the steam tube rotary dryer 9 through the metering rotary valve into the coal mill 14.
  • the function of the two metering rotary valves is to feed the buffer bin 12 to the coal mill 14 after weighing the dry coal.
  • the coal mill 14 grinds the coal particles dried by the steam tube rotary dryer 9 into fine coal powder.
  • the sealing fan 15 functions to filter nitrogen gas and feed it to the coal mill 14.
  • the two bag filters filter the dry tail gas and pulverized coal containing water vapor, and the pulverized coal is sent to the collecting tank.
  • the dry exhaust gas contains nitrogen, water vapor and a small amount of air and is sent to the washing and cooling tower 6 by the circulating fan.
  • the function of the cooler 17 is to wash the flashing section of the cooling tower 6 for vacuum flashing, and the flashed steam K is dehumidified and then sucked into the condenser 17 by the water ring vacuum pump 18 to be condensed to become ⁇ 40.
  • the clean water M at °C is directly sent to the condensed water recovery tank 19 for storage.
  • the water ring vacuum pump 18 is used to flash the water vapor from the top of the wash cooling tower to the suction condenser 17 for condensation.
  • the condensed water recovery tank 19 is for storing the condensed water of the cooler 17.
  • the function of the two double-layer electric flap valves is to quickly discharge the baghouse pulverized coal into the pulverized coal collection tank 27 by electric control.
  • the pulverized coal collection tank 27 functions to collect the second baghouse 23 water vapor, nitrogen gas and coal powder.
  • the function of the venturi ejector pump 29 is to mix the pressurized air with the pulverized coal and then inject it into the boiler through the nozzle for combustion.
  • the conveying fan 30 functions to discharge the purified exhaust gas into the atmosphere.
  • the present invention establishes secondary drying of lignite. That is, the steam tube rotary dryer 9 is one-stage drying, the coal mill 14 is two-stage drying, the first-stage dry heat source is 0.3-2.0 MPa, the temperature is 120-360 ° C, and the second-stage dry heat source is 150-200 ° C hot nitrogen.
  • the primary drying heat source is the steam extraction of the steam turbine 35, and after the heat transfer, it becomes the condensate, and then is sent back to the deaerator 37 to form a closed loop of the dry heat source; after the secondary drying heat source is dried, powdered, dusted, washed, etc., The fourth circulating fan 10 is sent back to the nitrogen heater 11 to form a closed loop of the drying and milling heat source.
  • the present invention is in the coal mill 14, the first circulating fan 20, the second circulating fan 24, the circulating fan III2, the circulating fan IV10, the circulating fan V16, the sealing fan 15, the vacuum pump 18, the first washing circulation pump
  • a flow meter is provided on both the 4 and the second wash circulation pump 5. Further, a metering and weighing device is provided in the steam tube rotary dryer 9, the coal mill 14, and the inlet of the venturi ejector pump 29.
  • the carrier gas heater 1 and the nitrogen heater 11 are liquid-air type fin tube heaters or tube heat exchangers heated by hot water.
  • the washing and cooling tower 6 is any one of a packed tower, a tray tower or a spray tower.
  • the bag filter I21 and the bag filter II23 are high-efficiency dust collectors for off-line nitrogen backflushing.
  • Drying carrier gas (loading capacity: 15000-35000 Nm3/h) at a pressure of 0.3 to 2.0 MPa, a temperature of 120 to 360 ° C, and a temperature of 120 to 360 ° C, that is, after drying for 30 to 60 minutes under the condition of nitrogen N, respectively, the moisture after drying is ⁇ 15% of coal particles B and dry tail gas F with a temperature of 90-110 ° C; coal particles B are sent to the buffer tank 12, and the dry tail gas F is sent into the first bag filter 21 at a pressure of -200-500 Pa, temperature 90. Dedusting is carried out under conditions of -110 ° C to obtain tail gas D containing water vapor and pulverized coal T. The pulverized coal T is directly sent to the collecting tank 27, and the exhaust gas D contains nitrogen gas, water vapor and a small amount of air and is sent to the washing by the first circulating fan 20. After the cooling tower 6, the first-stage drying process is completed;
  • coal particles B are sent into the buffer tank 12, they are metered by the weighing device provided in the middle of the buffer tank 12 and the lower metering rotary valve 13 and sent to the coal mill 14, at a hot air pressure of 2000 to 6000 Pa and a temperature of 180.
  • the tail gas H contains water vapor and nitrogen; the pulverized coal C is directly sent to the pulverized coal collection tank 27; 15% of the exhaust gas H is directly sent back to the nitrogen heater by the fifth circulation fan 16
  • the inlet of 11 is mixed with the nitrogen gas E sent back by the fourth circulation fan 10, and then heated to 180 to 200 ° C, and directly sent to the coal mill. 14 used in which 85% of the exhaust blower 24 H is fed to the second circulation washing treatment after the cooling tower 6, to complete the secondary drying, milling process.
  • the non-condensable gas stored in the tank 19 is emptied by the water ring vacuum pump 18; after the flashing and cooling, the bottom liquid J of 40 to 60 ° C enters the distributor of the washing and cooling tower 6 through the liquid level control system, and again with the exhaust gas G Reverse contact with exhaust gas H, cooling and dehumidification, forming a closed loop system; the cooling medium of the condenser 17 is circulating cooling water; after recovering the water vapor in the exhaust gas G and the exhaust gas H, the remaining nitrogen gas E returns to the primary and secondary drying recycle.
  • the heating mediums of the carrier gas preheater 1, the steam rotary dryer 9, and the nitrogen heater 11 are all extracted from the steam turbine 35, and are sent through the rotary joint 32 and the condensate storage tank 33, pressurized by the condensate pump 34, and sent back.
  • Deaerator 37 The heating mediums of the carrier gas preheater 1, the steam rotary dryer 9, and the nitrogen heater 11 are all extracted from the steam turbine 35, and are sent through the rotary joint 32 and the condensate storage tank 33, pressurized by the condensate pump 34, and sent back.
  • Deaerator 37 The heating mediums of the carrier gas preheater 1, the steam rotary dryer 9, and the nitrogen heater 11 are all extracted from the steam turbine 35, and are sent through the rotary joint 32 and the condensate storage tank 33, pressurized by the condensate pump 34, and sent back. Deaerator 37.

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Abstract

一种发电机组高水分、低热值褐煤干燥及水回收方法及其装置。该装置包括蒸汽管回转干燥机（9）、洗涤冷却塔（6）、磨煤机（14）、第一袋式除尘器I（21）、第二袋式除尘器II（23）、蒸汽冷凝器（17）、称重缓冲仓（12）、水环真空泵（18）、文丘里引射泵（29）、湿煤仓（3）、氮气加热器（11）以及煤粉收集罐（27）。25%-62%高水分褐煤经干燥装置干燥后，能够达到燃煤电厂的使用要求，并且能够回收高水分褐煤中95%的水分，回收的水分通过洗涤、闪蒸、除湿、冷凝后变成洁净水，作为电厂补充使用。该装置将干燥系统与制粉系统融合为一体，干燥机（9）和磨煤机（14）一对一配置，通过缓冲仓（12）直接衔接，节省了煤粉转运过程中散失的热量，省去了传统干燥系统和磨煤系统的中间长距离输送环节，有效避免了输送转运粉尘污染、浪费和自燃现象，同时简化干燥前端备煤系统，降低了生产成本。

Description

一种发电机组高水分、低热值褐煤干燥和水回收方法及其装置 技术领域
本发明涉及一种发电机组高水分、低热值褐煤干燥和水回收方法及其装置。该装置通过增设褐煤干燥及水回收系统，使得高水分褐煤热值得到提高，达到发电要求，并能回收褐煤中的水作为电厂补充水源，减少水耗，节省了能源。
背景技术
传统燃煤电厂的制粉系统，采用磨煤机(常规有中速磨煤机和风扇磨煤机)通入燃煤锅炉省煤器后的150～300℃的热烟气进行制粉和干燥，然后吹入锅炉燃烧使用。可是，这种方式干燥程度低，无法直接使高水分褐煤达到发电要求，而且无法回收褐煤中的水分。
上述传统燃煤电厂煤干燥系统与制粉系统为两个独立的单元，干燥后的煤通过刮板机、皮带机、斗提机等输送设备输送至制粉系统的煤仓，其存在的问题是：
(1)干燥后的煤粉温度达60～80℃，在输送过程中产生大量粉尘和蒸汽，而其中由于细粉较多，且水分较低，采用皮带或刮板输送等均容易产生大量粉尘，不仅污染环境，操作环境较差，而且细煤粉极易自然着火，甚至会发生闪爆等严重事故，影响输送设备的稳定使用。
(2)干燥后温度达60～80℃的热煤通过输送环节，煤温降低至30～60℃后才进入磨煤机制粉，干燥后热煤携带的热量被浪费，根据计算该部分浪费的热量占制粉系统所需能量的5～20％。
(3)采用煤干燥产生的干燥尾气经除尘后直接排入大气，未对尾气中含有的热量和水蒸汽回收利用。
发明公开
针对传统燃煤电厂褐煤干燥与制粉存在的问题，本发明提供一种发电机组高水分、低热值褐煤干燥和水回收装置，包括蒸汽管回转干燥机、洗涤冷却塔、 磨煤机、第一袋式除尘器、第二袋式除尘器、蒸汽冷凝器、称重缓冲仓、水环真空泵、文丘里引射泵、湿煤仓、氮气加热器以及煤粉收集罐；
其中，该蒸汽管回转干燥机的输入端与湿煤仓相接，其另一端上部连连接该第一袋式除尘器，下部连接该称重缓冲仓，该第一袋式除尘器上部与该洗涤冷却塔相连，该称重缓冲仓与该磨煤机相连，该磨煤机的一侧与该氮气加热器相连，该磨煤机顶部连接该第二袋式除尘器，该第二袋式除尘器上部与该洗涤冷却塔相连，另一侧与该氮气加热器的入口相连，该第二袋式除尘器的下部与该煤粉收集罐相连；该第一袋式除尘器上部与该洗涤冷却塔相连，下部与该煤粉收集罐相连；该洗涤冷却塔的一侧与该氮气加热器相连。
上述的发电机组高水分、低热值褐煤干燥和水回收装置，该洗涤冷却塔的底部连接第一洗涤循环泵和第二洗涤循环泵，其顶部与蒸汽冷凝器相连。
上述的发电机组高水分、低热值褐煤干燥和水回收装置，该蒸汽冷凝器的顶部与一水环真空泵相连，该蒸汽冷凝器的中部设有冷却水进口，其上部和底部分别设有冷却水回水口，底部与冷凝水回收罐相连。
上述的发电机组高水分、低热值褐煤干燥和水回收装置，一载气加热器与该洗涤冷却塔的另一侧与相连，同时该载气加热器与该蒸汽管回转干燥机的输入端相连。
上述的发电机组高水分、低热值褐煤干燥和水回收装置，该煤粉收集罐通过第二计量旋转阀与该文丘里引射器相连，该文丘里引射器一侧与输送风机相连，输送风机与燃煤锅炉25相连，另一侧与大气相通。
上述的发电机组高水分、低热值褐煤干燥和水回收装置，在蒸汽管回转干燥机尾端设有一旋转接头，其上部与汽轮机的抽汽缸相连，下部与凝液储罐相连。
上述的发电机组高水分、低热值褐煤干燥和水回收装置，该凝液储罐与一凝液泵相连，该凝液泵与凝汽器相连，该凝汽器与除氧器相连，该除氧器与锅炉汽包连接。
为了解决上述问题，本发明还提供一种发电机组高水分、低热值褐煤干燥和水回收方法，包括以下步骤：
步骤一：一级干燥，将湿煤破碎后，经过湿煤仓之后进入蒸汽管回转干燥机内部，在加热蒸汽和干燥载气下加热干燥一定时间后，得到一定水分比例的 煤粒B和一定温度的干燥气体F；将该干燥尾气送入第一袋式除尘器内进行除尘，得到含有水蒸气的尾气D和煤粉T，将煤粉直接送入收集罐，同时将该尾气D送入洗涤冷却塔中；
步骤二：二级干燥、制粉，将该煤粒B送入一缓冲仓之后送入一磨煤机，在一预设条件下进行制粉一预设时间，得到干燥后的煤粉C；将氮气P通过氮气加热器加热至一预设温度之后，一部分的氮气P送入该磨煤机，对该煤粒B进行干燥和制粉，得到煤粉C；另一部分的氮气P通过密封风机送入磨煤机密封使用；将从磨煤机顶部排出的尾气G送入第二袋式除尘器进行收集，得到煤粉C和除尘后的尾气H，其中该煤粉C直接送入煤粉收集罐进行收集，该尾气H的一部分被回送至氮气加热器加热至一预设温度之后，输入磨煤机，而另一部分该尾气H被送入洗涤冷却塔处理；
步骤三：将尾气D和尾气H在洗涤冷却塔内降温除湿，在洗涤冷却塔底部形成塔底液J，将塔底液J进行真空闪蒸降温所得到的水蒸气经过除湿后输入蒸汽冷凝器冷凝，已形成洁净水M，将该洁净水M输送至冷凝水回收罐内储存，同时不能被冷凝的不凝气排入到空气中；
步骤四：将从洗涤冷却塔侧部排出的氮气E的其中一部分输入载气加热器内，经过加热后输入蒸汽管回转干燥机的输入端，作为干燥载气使用；另一部分氮气E输入氮气加热器内，经过加热输入至磨煤机内，作为干燥和制粉的介质使用，已形成氮气密闭循环系统；
步骤五：煤粉T和煤粉C在煤粉收集罐内混合后输入至文丘里引射泵内，并与空气混合后锅炉25进行燃烧；
上述的发电机组高水分、低热值褐煤干燥和水回收方法，在步骤一中，湿煤的水分含量为25％～62％，并且湿煤被破碎成直径小于等于20mm。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤一中还包括湿煤从湿煤仓通过计量皮带秤和旋转密封阀后，进入蒸汽管回转干燥机内部。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤一中，该加热蒸汽的热蒸汽压力为0.3～2.0MPa，温度为120～360℃，干燥载气的温度为小于120℃，同时干燥载气的载气量为15000～35000Nm3/h，加热干燥时间为30-60分钟。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤一中，煤粒 B的水分含量为小于等于15％，干燥气体F的温度为90-110℃。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤一中，将该干燥尾气送入第一袋式除尘器内在压力为200～500Pa、温度90～110℃的条件下进行除尘。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤二中，进一步包括：煤粒B送入缓冲仓后，通过缓冲仓中部设置的称重装置与下部的计量旋转阀计量后再送入磨煤机。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤二中，该预设条件为热风压力为2000～6000Pa、温度为180～200℃，预设时间为6-25S，煤粉C的水分含量为小于等于2～5％。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤二中，将氮气P通过氮气加热器加热至180～200℃，将90％的氮气P送入该磨煤机，将10％的氮气P通过密封风机送入磨煤机密封使用。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤二中，该尾气H的15％被回送至氮气加热器加热至180～200℃之后，输入磨煤机，而85％的该尾气H被送入洗涤冷却塔处理。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤三中，该塔底液J的温度为80～90℃。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤三中，闪蒸降温后的塔底液J通过液位控制系统进入洗涤冷却塔的分配器，再次与尾气D和尾气H逆向接触，降温除湿，形成闭路循环系统，冷凝器的冷却介质为循环冷却水，将尾气D和尾气H的中的水蒸汽回收后，剩余的氮气E返回一级和二级干燥循环使用。
上述的发电机组高水分、低热值褐煤干燥和水回收方法在步骤四中，从洗涤冷却塔侧部排出的氮气E的温度为45～65℃，其中35％的氮气E输入载气加热器内，经过加热至小于等于120℃后输入蒸汽管回转干燥机的输入端，作为干燥载气使用；65％的氮气E输入氮气加热器内，经过加热至180～200℃后输入至磨煤机内，作为干燥和制粉的介质使用，已形成氮气密闭循环系统，氮气循环小于等于5％的损失通过系统外进行补充；
上述的发电机组高水分、低热值褐煤干燥和水回收方法，在步骤五中，煤 粉T和煤粉C在煤粉收集罐内混合后经过一计量旋转阀排出后进入至文丘里引射泵内，并与空气混合后锅炉25进行燃烧。
上述的发电机组高水分、低热值褐煤干燥和水回收方法载气预热器、蒸汽回转干燥机和氮气加热器的加热介质均来自汽轮机抽汽。
本发明与现有技术相比具有以下优点：
1、本发明将高水分褐煤通过蒸汽管回转干燥机干燥后，能够使水分高达61.3％的褐煤满负荷发电，能够满足燃煤电厂的使用要求，使无法应用的劣质煤变为能够发电的动力煤，使劣质煤能够得到有效利用，拓宽了资源利用空间。
2、本发明能够回收高水分褐煤中95％的水分，通过洗涤、闪蒸、除湿、冷凝后变为洁净水，作为电厂补充水循环使用，节省了宝贵的水资源。
3、本发明热源全部采用汽轮机抽汽，利用了系统的冷源损失(即使用了高压高温蒸汽做功后的冷凝潜热)，不但极大降低干燥系统的能耗，而且能够大幅度降低发电机组的供电煤耗。
3、本发明将干燥系统与制粉系统融合为一体，蒸汽管回转干燥机与磨煤机采用一对一方式配置，即蒸汽管回转干燥机出口直接通过缓冲仓与磨煤机相连，干燥后煤粉缓存后进入磨煤机制粉，不但节省了煤粉转运过程中散失的热量，而且省去了传统干燥系统和磨煤系统的中间长距离输送环节，缩短了流程有效避免了输送转运粉尘污染、浪费和自燃现象。
4、本发明省去了中间复杂的输送环节，仅由缓冲仓和计量旋转阀代替，同时简化干燥前端备煤系统，节省了原制粉系统的煤仓建设投资，大大降低了生产成本。
5、本发明利用传统制粉系统具有的干燥功能，将干燥系统分为两级，一级为蒸汽管回转干燥，二级为制粉系统干燥，可将高水分褐煤的水分降至2～5％，极大提高褐煤的热值。
6、本发明煤干燥系统可实现惰性气体循环干燥，洗涤冷却塔将干燥尾气中的水蒸汽回收为洁净水，排放的氮气经加热后返回一级干燥系统和二级干燥、制粉系统，成为干燥载气和二级干燥、制粉热源，使得干燥系统实现闭路循环，能耗降低，同时，干燥系统的氧含量完全可控，干燥后的尾气(含大量水蒸汽)经收尘后直接排入大气，对尾气中含有的热量和水蒸汽回收利用。不再向大气排放干燥尾气，电厂煤干燥系统更安全、更环保。
7、本发明投资小、能耗低、经济价值高，并易于实施。
附图简要说明
图1为本发明的工艺流程图，其中虚线框内为传统发电机组。
其中，附图说明：
1-载气加热器           2-第三循环风机III
3-湿煤仓               4-第一洗涤循环泵
5-第二洗涤循环泵       6-洗涤冷却塔
7-计量皮带秤           8-旋转密封阀
9-蒸汽管回转干燥机     10-第四循环风机IV
11-氮气加热器          12-缓冲仓
13-第一计量旋转阀I     14-磨煤机
15-密封风机            16-第五循环风机V
17-蒸汽冷凝器          18-水环真空泵
19-冷凝水回收罐        20-第一循环风机I
21-第一袋式除尘器I     22-第一双层电动翻板阀I
23-第二袋式除尘器II    24-第二循环风机II
25-燃煤锅炉            26-第二双层电动翻板阀II
27-煤粉收集罐          28-第二计量旋转阀II
29-文丘里引射器        30-输送风机
31-锅炉汽包            32-旋转接头
33-凝液储罐            34-凝液泵
35-汽轮机              36-凝汽器
37-除氧器
实现本发明的最佳方式
下面结合附图对本发明的技术方案再作进一步详细的说明：
如图1所示，一种发电机组高水分、低热值褐煤干燥及水回收的装置，主要包括蒸汽管回转干燥机9、洗涤冷却塔6、磨煤机14、第一袋式除尘器21、第二袋式除尘器23、冷凝器19、称重缓冲仓12、水环真空泵18、文丘里引射 泵29、湿煤仓3、氮气加热器11和循环风机和煤粉收集罐27。蒸汽管回转干燥机9的输入端通过计量皮带秤7和旋转密封阀8与湿煤仓3相接，其另一端上部连有第一袋式除尘器21，下部设有称重缓冲仓12，第一袋式除尘器21上部一侧通过第二循环风20与洗涤冷却塔6相连；称重缓冲仓12通过第一计量旋转阀13连有磨煤机14；磨煤机14的一侧通过氮气加热器11与第四循环风机10相连，另一侧与密封风机15相连，磨煤机14顶部设有第二袋式除尘器23；第二袋式除尘器23上部一侧通过第二循环风机24与洗涤冷却塔6相连，另一侧通过第五循环风机16与氮气加热器11入口相连，下部通过第二双层电动翻板阀26与煤粉收集罐27相连；第一袋式除尘器21上部通过第一循环风机20与洗涤冷却塔6相连，下部通过第一双层电动翻板阀22与煤粉收集罐27相连；洗涤冷却塔6一侧通过第三循环风机2与载气加热器1相连，另一侧通过第四循环风10与氮气加热器11相连，其底部设有洗涤循环泵4和第二洗涤循环泵5，其顶部与蒸汽冷凝器17相连；蒸汽冷凝器17顶部与水环真空泵18相连，蒸汽冷凝器17的中部设有冷却水进口，其上部和底部分别设有冷却水回水口，底部与冷凝水回收罐19相连；载气加热器1与蒸汽管回转干燥机9的输入端相连；煤粉收集罐27通过第二计量旋转阀28与文丘里引射器29相连；文丘里引射器29一侧与输送风机30相连，输送风机30与燃煤锅炉25相连，另一侧与大气相通；位于蒸汽管回转干燥机9尾端的旋转接头32上部与汽轮机35的抽汽缸相连，下部与凝液储罐33相连；凝液储罐33与凝液泵34相连，凝液泵34与凝汽器36相连，凝汽器36与除氧器37相连，除氧器37与锅炉汽包31连接。
其中该载气加热器1的作用是蒸汽新液和低压蒸汽进行加热，输送给蒸汽管回转干燥机9。五个循环风机，用于压缩和输送含有水蒸汽、氮气尾气体。该个湿煤仓3用于供给蒸汽管回转干燥机9湿褐煤的料斗。两台洗涤循环泵的其作用是将储存在洗涤冷却塔6塔底液在泵的作用下，循环被送入洗涤冷却塔6顶部闪蒸段进行真空闪蒸；该洗涤冷却塔6的作用是将循环风机送入含有水蒸汽、氮气尾气与塔顶闪蒸降温后的冷却水在塔内汽液逆向接触，进行降温除湿。该计量皮带秤7的作用是将湿煤仓3湿煤通过计量，由旋转密封阀8输入蒸汽管回转干燥机9。该旋转密封阀8的作用是将计量皮带秤7计量的湿煤相对密闭地输入蒸汽管回转干燥机9。该蒸汽管回转干燥机9为倾斜的回转圆筒， 圆筒内布置若干列管，列管按照同心圆方式布置2～7层，管内走蒸汽，管外走煤，输入端设有煤粒入口、载气入口，输出端设有煤粒出口、尾气出口、蒸汽进口和凝液出口。该氮气加热器11用来给洗涤冷却塔6输送低压氮气进行加热的器件。该缓冲仓12的作用是调节均衡由蒸汽管回转干燥机9干燥的煤粒通过计量旋转阀入磨煤机14。二个计量旋转阀的作用是将缓冲仓12称重干燥煤计量后送入磨煤机14。该磨煤机14是将蒸汽管回转干燥机9干燥的煤粒碾磨成细煤粉，该密封风机15的作用是对氮气进行过滤，送入磨煤机14使用。二个袋式除尘器是将含有水蒸气的干燥尾气和煤粉进行过滤，煤粉送入收集罐，干燥尾气中含有氮气、水蒸气和少量空气被循环风机送入洗涤冷却塔6。该冷却器17的作用是洗涤冷却塔6顶部闪蒸段进行真空闪蒸，闪蒸出的水蒸汽K经除湿后，在水环真空泵18抽吸作用下进入冷凝器17进行冷凝，成为～40℃的洁净水M，直接送入冷凝水回收罐19内储存。该水环真空泵18，用来将洗涤冷却塔顶部闪蒸水蒸汽到抽吸冷凝器17进行冷凝。该冷凝水回收罐19，用来贮存冷却器17冷凝水。二个双层电动翻板阀的作用是通过电动控制快速将袋式除尘器煤粉卸入煤粉收集罐27。该煤粉收集罐27的作用是将第二袋式除尘器23水蒸汽、氮气和煤粉予以收集。该文丘里引射泵29的作用是将加压的空气与煤粉混合后，通过喷嘴射入锅炉燃烧。该输送风机30，其作用是将净化的尾气排入大气。
为了满足燃煤电厂对褐煤使用要求，本发明设立褐煤二级干燥。即蒸汽管回转干燥机9为一级干燥，磨煤机14为二级干燥，一级干燥热源为0.3～2.0MPa、温度120～360℃，二级干燥热源为150～200℃的热氮气，一级干燥的热源为汽轮机35的抽汽，传热后变为冷凝液，然后回送除氧器37，形成干燥热源闭路循环；二级干燥热源经干燥、制粉、除尘、洗涤等工序后，经第四循环风机10回送至氮气加热器11，形成干燥、制粉热源的闭路循环。
为了控制褐煤的流量，本发明在磨煤机14、第一循环风机20、第二循环风机24、循环风机III2、循环风机IV10、循环风机V16、密封风机15、真空泵18、第一洗涤循环泵4和第二洗涤循环泵5上均设有流量计。并且在蒸汽管回转干燥机9、磨煤机14、文丘里引射泵29入口的均设置计量、称重装置。
载气加热器1、氮气加热器11为热水加热的液-气型翅片管加热器或列管换热器。
洗涤冷却塔6为填料塔、板式塔或喷淋塔中的任意一种。
袋式除尘器I21、袋式除尘器II23为离线氮气反吹的高效除尘器。
下面结合高水分、低热值褐煤煤粉炉发电系统的干燥制粉及水回收装置所采用的方法，对其步骤分述如下：
(1)将水分25％～62％的湿煤A破碎至≤20mm后，送入湿煤仓3通过计量皮带秤7和旋转密封阀8后，进入蒸汽管回转干燥机9内部，在加热蒸汽压力0.3～2.0MPa、温度120～360℃和温度～120℃干燥载气(载气量：15000～35000Nm3/h)，即在氮气N的条件下进行干燥30～60min后，分别得到干燥后水分≤15％的煤粒B和温度为90～110℃的干燥尾气F；煤粒B送入缓冲仓12，干燥尾气F送入第一袋式除尘器21内，在压力-200～500Pa、温度90～110℃的条件下进行除尘，得到含有水蒸气的尾气D和煤粉T，煤粉T直接送入收集罐27，尾气D含有氮气、水蒸气和少量空气被第一循环风机20送入洗涤冷却塔6后，完成一级干燥过程；
(2)煤粒B送入缓冲仓12后，通过缓冲仓12中部设置的称重装置与下部的计量旋转阀13计量后送入磨煤机14，在热风压力为2000～6000Pa、温度为180～200℃的条件下制粉6～25S后，得到干燥后水分≤2～5％的煤粉C；第四循环风机10鼓入氮气加热器11加热至180～200℃的氮气P，其中90％的热氮气P送入磨煤机14对煤粒B进行干燥和制粉，得到煤粉C，10％的热氮气P通过密封风机15送入磨煤机14密封使用；从磨煤机14顶部排出的经过干燥、制粉后降温至90～110℃的尾气G，尾气G中含有大量煤粉C、水蒸汽、氮气，通过第二循环风机24送入第二袋式除尘器23进行收集，得到煤粉C和除尘后的尾气H，尾气H中含有水蒸汽、氮气；煤粉C直接送入煤粉收集罐27；尾气H的15％被第五循环风机16直接回送至氮气加热器11的入口，与第四循环风机10回送的氮气E混合后加热至180～200℃，直接送入磨煤机14使用，其中85％的尾气H被第二循环风机24送入洗涤冷却塔6处理后，完成二级干燥、制粉过程。
(3)含有氮气、水蒸气和少量空气的尾气D和含有水蒸汽、氮气尾气H被送入洗涤冷却塔6后，与来自洗涤冷却塔6顶部闪蒸段闪蒸降温后的40～60℃冷却水在洗涤冷却塔6内汽液逆向接触，进行降温除湿，把尾气D和尾气H中的大量水蒸汽冷凝下来并积存在洗涤冷却塔6底部，形成塔底液J，温度为 80～90℃；储存在洗涤冷却塔6底部的80～90℃塔底液J在第一洗涤循环泵4和第二洗涤循环泵5的作用下，送入洗涤冷却塔6顶部闪蒸段进行真空闪蒸，闪蒸出40～70℃的水蒸汽K经除湿后，在水环真空泵18抽吸作用下进入冷却器17进行冷凝，成为～40℃的洁净水M，直接送入冷凝水回收罐19内储存，不能冷凝的不凝气通过水环真空泵18排空；闪蒸降温后40～60℃的塔底液J通过液位控制系统进入洗涤冷却塔6的分配器，再次与尾气G和尾气H逆向接触，降温除湿，形成闭路循环系统；冷凝器17的冷却介质为循环冷却水；将尾气G和尾气H的中的水蒸汽回收后，剩余的氮气E返回一级和二级干燥循环使用。
(4)从洗涤冷却塔6侧部排出的经过除湿、降温后氮气E，温度为45～65℃，其中35％通过第三循环风机2加压后氮气N，鼓入载气加热器1内，加热至～120℃后，送入蒸汽管回转干燥机9的输入端，作为干燥载气使用，65％的氮气E通过第四循环风机10加压后氮气P，鼓入氮气加热器11内，加热至180～200℃后，送入磨煤机14内，作为干燥和制粉的介质使用，形成氮气密闭循环系统，氮气循环～5％的损失可通过系统外进行补充。
(5)从第一袋式除尘器21和第二袋式除尘器23排入煤粉收集罐27的煤粉T和煤粉C混合后，经计量旋转阀28排出后进入文丘里引射泵29，在输送风机30加压的作用下，将空气送入文丘里引射泵29与煤粉混合后，吹入锅炉25燃烧使用。
(6)载气预热器1、蒸汽回转干燥机9和氮气加热器11的加热介质均来自汽轮机35抽汽，经旋转接头32和凝液储罐33，通过凝液泵34加压后回送除氧器37。

Claims (22)

  1. 一种发电机组高水分、低热值褐煤干燥和水回收装置，其特征在于，包括蒸汽管回转干燥机、洗涤冷却塔、磨煤机、第一袋式除尘器、第二袋式除尘器、蒸汽冷凝器、称重缓冲仓、水环真空泵、文丘里引射泵、湿煤仓、氮气加热器以及煤粉收集罐；
    其中，该蒸汽管回转干燥机的输入端与湿煤仓相接，其另一端上部连连接该第一袋式除尘器，下部连接该称重缓冲仓，该第一袋式除尘器上部与该洗涤冷却塔相连，该称重缓冲仓与该磨煤机相连，该磨煤机的一侧与该氮气加热器相连，该磨煤机顶部连接该第二袋式除尘器，该第二袋式除尘器上部与该洗涤冷却塔相连，另一侧与该氮气加热器的入口相连，该第二袋式除尘器的下部与该煤粉收集罐相连；该第一袋式除尘器上部与该洗涤冷却塔相连，下部与该煤粉收集罐相连；该洗涤冷却塔的一侧与该氮气加热器相连。
  2. 如权利要求1所述的发电机组高水分、低热值褐煤干燥和水回收装置，其特征在于，该洗涤冷却塔的底部连接第一洗涤循环泵和第二洗涤循环泵，其顶部与蒸汽冷凝器相连。
  3. 如权利要求1所述的发电机组高水分、低热值褐煤干燥和水回收装置，其特征在于，该蒸汽冷凝器的顶部与一水环真空泵相连，该蒸汽冷凝器的中部设有冷却水进口，其上部和底部分别设有冷却水回水口，底部与冷凝水回收罐相连。
  4. 如权利要求1所述的发电机组高水分、低热值褐煤干燥和水回收装置，其特征在于，一载气加热器与该洗涤冷却塔的另一侧与相连，同时该载气加热器与该蒸汽管回转干燥机的输入端相连。
  5. 如权利要求1所述的发电机组高水分、低热值褐煤干燥和水回收装置，其特征在于，该煤粉收集罐通过第二计量旋转阀与该文丘里引射器相连，该文丘里引射器一侧与输送风机相连，输送风机与燃煤锅炉25相连，另一侧与大气相通。
  6. 如权利要求1所述的发电机组高水分、低热值褐煤干燥和水回收装置，其特征在于，在蒸汽管回转干燥机尾端设有一旋转接头，其上部与汽轮机的抽汽缸相连，下部与凝液储罐相连。
  7. 如权利要求6所述的发电机组高水分、低热值褐煤干燥和水回收装置，其特征在于，该凝液储罐与一凝液泵相连，该凝液泵与凝汽器相连，该凝汽器与除氧器相连，该除氧器与锅炉汽包连接。
  8. 一种发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，包括以下步骤：
    步骤一：一级干燥，将湿煤破碎后，经过湿煤仓之后进入蒸汽管回转干燥机内部，在加热蒸汽和干燥载气下加热干燥一定时间后，得到一定水分比例的煤粒B和一定温度的干燥气体F；将该干燥尾气送入第一袋式除尘器内进行除尘，得到含有水蒸气的尾气D和煤粉T，将煤粉直接送入收集罐，同时将该尾气D送入洗涤冷却塔中；
    步骤二：二级干燥、制粉，将该煤粒B送入一缓冲仓之后送入一磨煤机，在一预设条件下进行制粉一预设时间，得到干燥后的煤粉C；将氮气P通过氮气加热器加热至一预设温度之后，一部分的氮气P送入该磨煤机，对该煤粒B进行干燥和制粉，得到煤粉C；另一部分的氮气P通过密封风机送入磨煤机密封使用；将从磨煤机顶部排出的尾气G送入第二袋式除尘器进行收集，得到煤粉C和除尘后的尾气H，其中该煤粉C直接送入煤粉收集罐进行收集，该尾气H的一部分被回送至氮气加热器加热至一预设温度之后，输入磨煤机，而另一部分该尾气H被送入洗涤冷却塔处理；
    步骤三：将尾气D和尾气H在洗涤冷却塔内降温除湿，在洗涤冷却塔底部形成塔底液J，将塔底液J进行真空闪蒸降温所得到的水蒸气经过除湿后输入蒸汽冷凝器冷凝，已形成洁净水M，将该洁净水M输送至冷凝水回收罐内储存，同时不能被冷凝的不凝气排入到空气中；
    步骤四：将从洗涤冷却塔侧部排出的氮气E的其中一部分输入载气加热器内，经过加热后输入蒸汽管回转干燥机的输入端，作为干燥载气使用；另一部分氮气E输入氮气加热器内，经过加热输入至磨煤机内，作为干燥和制粉的介质使用，已形成氮气密闭循环系统；
    步骤五：煤粉T和煤粉C在煤粉收集罐内混合后输入至文丘里引射泵内，并与空气混合后锅炉25进行燃烧；
  9. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤一中，湿煤的水分含量为25％～62％，并且湿煤被破碎成 直径小于等于20mm。
  10. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤一中还包括湿煤从湿煤仓通过计量皮带秤和旋转密封阀后，进入蒸汽管回转干燥机内部。
  11. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤一中，该加热蒸汽的热蒸汽压力为0.3～2.0MPa，温度为120～360℃，干燥载气的温度为小于120℃，同时干燥载气的载气量为15000～35000Nm3/h，加热干燥时间为30-60分钟。
  12. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤一中，煤粒B的水分含量为小于等于15％，干燥气体F的温度为90-110℃。
  13. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤一中，将该干燥尾气送入第一袋式除尘器内在压力为200～500Pa、温度90～110℃的条件下进行除尘。
  14. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤二中，进一步包括：煤粒B送入缓冲仓后，通过缓冲仓中部设置的称重装置与下部的计量旋转阀计量后再送入磨煤机。
  15. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤二中，该预设条件为热风压力为2000～6000Pa、温度为180～200℃，预设时间为6-25S，煤粉C的水分含量为小于等于2～5％。
  16. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤二中，将氮气P通过氮气加热器加热至180～200℃，将90％的氮气P送入该磨煤机，将10％的氮气P通过密封风机送入磨煤机密封使用。
  17. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤二中，该尾气H的15％被回送至氮气加热器加热至180～200℃之后，输入磨煤机，而85％的该尾气H被送入洗涤冷却塔处理。
  18. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤三中，该塔底液J的温度为80～90℃。
  19. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤三中，闪蒸降温后的塔底液J通过液位控制系统进入洗涤 冷却塔的分配器，再次与尾气D和尾气H逆向接触，降温除湿，形成闭路循环系统，冷凝器的冷却介质为循环冷却水，将尾气D和尾气H的中的水蒸汽回收后，剩余的氮气E返回一级和二级干燥循环使用。
  20. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤四中，从洗涤冷却塔侧部排出的氮气E的温度为45～65℃，其中35％的氮气E输入载气加热器内，经过加热至小于等于120℃后输入蒸汽管回转干燥机的输入端，作为干燥载气使用；65％的氮气E输入氮气加热器内，经过加热至180～200℃后输入至磨煤机内，作为干燥和制粉的介质使用，已形成氮气密闭循环系统，氮气循环小于等于5％的损失通过系统外进行补充；
  21. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，在步骤五中，煤粉T和煤粉C在煤粉收集罐内混合后经过一计量旋转阀排出后进入至文丘里引射泵内，并与空气混合后锅炉25进行燃烧。
  22. 如权利要求8所述的发电机组高水分、低热值褐煤干燥和水回收方法，其特征在于，载气预热器、蒸汽回转干燥机和氮气加热器的加热介质均来自汽轮机抽汽。
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