CN111189060A - Method for conveying pulverized coal by oxygen-enriched air - Google Patents

Method for conveying pulverized coal by oxygen-enriched air Download PDF

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Publication number
CN111189060A
CN111189060A CN202010120354.5A CN202010120354A CN111189060A CN 111189060 A CN111189060 A CN 111189060A CN 202010120354 A CN202010120354 A CN 202010120354A CN 111189060 A CN111189060 A CN 111189060A
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air
pipeline
nitrogen
oxygen
pressure
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CN111189060B (en
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邓国亮
齐砚勇
何森林
杨正军
韦霆
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Hangzhou Turning Energy Technology Development Co ltd
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Hangzhou Turning Energy Technology Development Co ltd
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    • 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
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/007—Supplying oxygen or oxygen-enriched air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/008—Feeding devices for pulverulent fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/10—Supply line fittings
    • F23K2203/104—Metering devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/20—Feeding/conveying devices
    • F23K2203/201—Feeding/conveying devices using pneumatic means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention discloses a method for conveying pulverized coal by oxygen-enriched air, wherein the pulverized coal reaches a metering scale for metering from a pulverized coal bin through a feeder and a sealed isolation protection bin in sequence, the oxygen-enriched air produced by an air source device is adjusted in real time by a control system according to the quality data of the pulverized coal, and is correspondingly controlled in concentration, temperature and pressure, and is conveyed to the metering scale at a corresponding conveying air speed, and is conveyed to combustion equipment after being mixed with the pulverized coal; nitrogen produced by the air source device is introduced into the flow-assisting and purging system and is respectively sent into a cone blanking pipe of the pulverized coal bunker, the sealed isolation protection bin for flow assistance, the expansion joint and the metering scale for purging, and the control system controls the flow-assisting and purging start-stop, frequency, pressure and self-protection. By effectively and reasonably controlling the conveying parameters and increasing safety protection measures, on the basis of fully ensuring the uniformity and stability of metering and conveying, the operation and maintenance cost of compressed air is saved, the energy consumption and pollutant emission are reduced, and the risks of heating and spontaneous combustion explosion in metering and conveying pulverized coal by oxygen-enriched air are greatly reduced.

Description

Method for conveying pulverized coal by oxygen-enriched air
Technical Field
The invention relates to the technical field of industrial kilns and air separation, in particular to a method for conveying pulverized coal by oxygen-enriched air.
Background
At present, human energy consumption is near 4/5, which is obtained by combustion, and the problems of energy and environmental pollution are greatly concerned. Various high-efficiency and low-pollution combustion technologies are developed, wherein oxygen-enriched combustion is an efficient combustion technology, the oxygen content in combustion air is increased by the oxygen-enriched combustion, the combustion condition can be greatly improved, the combustion efficiency is improved, and the pollution emission is reduced. In recent years, research and application of oxygen-enriched and oxy-fuel combustion technology in the glass industry of foreign developed countries have been gradually popularized, and are called as "creative technology of resources". China is mainly applied to glass melting furnaces and metal smelting and cannot be popularized in the cement industry of households with large energy consumption. With the maturity of oxygen production technology and the continuous reduction of oxygen enrichment cost, the method can be further popularized and applied in the high-temperature and high-coal-consumption cement industrial kiln industry.
Coal is used as a main fuel source at present, the metering and conveying of pulverized coal are an important link in production, at present, pressurized air is mainly used as a conveying medium, the stability and safety in conveying are basically guaranteed, but a large amount of conveying gas with normal temperature and moisture is required to be brought in during conveying, heat absorption and evaporation are required, high-temperature combustion air is reduced, the combustion temperature and efficiency of the pulverized coal are greatly reduced, and the energy consumption is increased. With the development of the oxygen-enriched combustion technology, the problems can be effectively solved by using oxygen-enriched air to convey the coal powder, but the conveying safety risk is inevitably increased.
Disclosure of Invention
The invention aims to provide a method for conveying pulverized coal by oxygen-enriched air, which aims to overcome the defects of the prior art.
The invention adopts the following technical scheme:
a method for conveying pulverized coal by oxygen-enriched air comprises a gas source device, a pulverized coal bin, a feeder, a sealed and isolated protection bin, a pressure-equalizing self-protection device, a flow-assisting purging system and a metering scale,
the device comprises a pulverized coal bunker, a conical blanking pipe, a blanking device, a sealing isolation protection bin and a metering scale, wherein the conical blanking pipe, the blanking device, the sealing isolation protection bin and the metering scale are sequentially connected;
the sealed isolation protection bin is provided with a first temperature sensor, a first pressure gauge and a pressure-equalizing self-protection device;
an oxygen-enriched air outlet of the air source device is connected to the metering scale through a first pipeline, the first pipeline is provided with a first flow regulating valve, a second temperature sensor, a first flowmeter and a second pressure gauge, and the metering scale is connected to the combustion equipment through a second pipeline;
a nitrogen outlet of the gas source device is connected to a flow-assisting purging system through a third pipeline, the third pipeline is provided with a second flow regulating valve, a third pressure gauge and a second flow meter, and the flow-assisting purging system is respectively connected to a conical blanking pipe, an expansion joint, a sealed isolation protection bin and a metering scale of the pulverized coal bin;
the first valve, the second valve, the first flow regulating valve, the second flow regulating valve, the first pressure gauge, the second pressure gauge, the third pressure gauge, the first flow meter, the second flow meter, the first temperature sensor, the second temperature sensor, the air source device, the blanking device, the flow-assisting purging system, the pressure-equalizing self-protection device and the metering scale are all connected into a control system, and the control system realizes automatic control;
the coal powder sequentially passes through a feeder and a sealed isolation protection bin from a coal powder bin to reach a metering scale for metering, oxygen-enriched air produced by an air source device is adjusted in real time by a control system according to the quality data of the coal powder to correspond to concentration, temperature and pressure, and the corresponding conveying air speed is controlled to be conveyed to the metering scale through a first pipeline, mixed with the coal powder and conveyed to combustion equipment through a second pipeline; nitrogen produced by the air source device is introduced into the flow-assisting and purging system through a third pipeline, and then is respectively sent into a conical blanking pipe and a sealed isolation protection bin of the pulverized coal bin for flow-assisting protection, and is sent into an expansion joint and a metering scale for purging, and the flow-assisting and purging start-stop, frequency, pressure and self-protection are controlled by the control system.
Further, the gas source device comprises a compression module, a precooling module, a purification module and a rectification module, wherein the compression module comprises an air filter and an air compressor, the precooling module comprises precooling equipment, the purification module comprises a molecular sieve adsorber and a heater, and the rectification module comprises a main heat exchanger, an expander, a subcooler, a rectification tower and a main condensation evaporator;
an air filter for filtering dust and mechanical impurities in the raw air;
the air compressor is used for compressing the filtered raw material air to a set pressure;
the precooling equipment is used for precooling the filtered and compressed raw material air;
the molecular sieve adsorber is used for purifying the filtered, compressed and precooled raw material air;
the main heat exchanger is used for cooling the filtered, compressed, precooled and purified raw material air; used for reheating oxygen-enriched air, reheating nitrogen, reheating part of the oxygen-enriched air and reheating the expanded nitrogen;
the rectifying tower is used for rectifying the raw material air after filtering, compressing, precooling, purifying and cooling at low temperature to separate the raw material air into liquid air and nitrogen;
the subcooler is used for subcooling the liquid air and reheating the oxygen-enriched air and the expanded nitrogen;
the main condensation evaporator is used for exchanging heat between liquid air and nitrogen, the liquid air is vaporized into oxygen-enriched air, and the nitrogen is condensed into liquid nitrogen;
the expansion machine is used for expanding and refrigerating the nitrogen after partial reheating;
a heater for heating the nitrogen to regenerate the molecular sieve adsorber;
the process for producing the oxygen-enriched air product and the nitrogen by-product is as follows:
firstly, filtering raw material air by an air filter to remove dust and mechanical impurities, and then compressing the air to a set pressure by an air compressor; precooling the product by precooling equipment, and then purifying the product in a molecular sieve adsorber;
step two, part of the purified raw material air is used as instrument air, and the rest part of the purified raw material air enters a main heat exchanger to be cooled and then enters a rectifying tower to participate in rectification;
step three, separating the air into liquid air and nitrogen after the air is rectified by a rectifying tower, allowing the liquid air to enter a main condensation evaporator after being supercooled by a cooler and throttled by a throttle valve to exchange heat with the nitrogen, vaporizing the liquid air into oxygen-enriched air, and allowing the oxygen-enriched air to enter an oxygen-enriched air buffer tank from a cooling box after being reheated by the cooler and a main heat exchanger so as to provide an oxygen-enriched air product; part of nitrogen is introduced into a main condensation evaporator to exchange heat with liquid air, the nitrogen is condensed into liquid nitrogen, the liquid nitrogen is introduced into the top of a rectifying tower to be used as reflux liquid, the rest of nitrogen enters a main heat exchanger, part of nitrogen is reheated and then discharged out of a cooling box to provide a nitrogen byproduct, the rest of nitrogen enters an expander to be expanded and refrigerated, the part of expanded nitrogen is reheated by a cooler and the main heat exchanger to be used as regeneration gas, the regeneration gas is heated by a heater and then introduced into a molecular sieve adsorber, and the rest of nitrogen is discharged.
Furthermore, the flow-assisting purging system comprises a first buffer tank, a second buffer tank and a third buffer tank, wherein the first buffer tank is provided with a nitrogen inlet and a nitrogen outlet, the nitrogen inlet is connected with a third pipeline, the nitrogen outlet is connected with a fourth pipeline, the fourth pipeline is provided with a third flow regulating valve, a fourth pressure gauge and a third flow meter, and the fourth pipeline is divided into two branch pipes, namely a first nitrogen outlet and a second nitrogen outlet, through a reducing tee; the first nitrogen outlet is connected with a second cache tank through a fifth pipeline, a fourth flow regulating valve, a fifth pressure gauge and a fourth flow meter are arranged on the fifth pipeline, the second cache tank is respectively sent to a conical part blanking pipe and a sealed isolation protection bin of the pulverized coal bin through a sixth pipeline and a seventh pipeline, and a pressure reducing valve is arranged on the seventh pipeline; and the second nitrogen outlet is connected with a third cache tank through an eighth pipeline, the eighth pipeline is provided with a fifth flow regulating valve, a sixth pressure gauge and a fifth flow meter, and the third cache tank is respectively connected to the expansion joint and the metering scale through a ninth pipeline and a tenth pipeline.
Furthermore, the volumes of the first cache tank, the second cache tank and the third cache tank are from large to small.
Furthermore, the sealed isolation protection bin is provided with a first temperature sensor, a first pressure gauge and a pressure-equalizing self-protection device, the pressure-equalizing self-protection device comprises an equalizing pressure pipeline, one end of the equalizing pressure pipeline is connected to the upper part of the sealed isolation protection bin, the other end of the equalizing pressure pipeline is connected to dust collection equipment, a third valve control opening degree is arranged on the equalizing pressure pipeline, and the pressure of the sealed isolation protection bin is controlled to be micro negative pressure; and starting a nitrogen cooling self-protection program when the temperature value of the first temperature sensor exceeds the alarm value.
The system further comprises a standby fan, the first pipeline is connected into an eleventh pipeline through a first tee joint, the eleventh pipeline is connected with the standby fan, the eleventh pipeline is provided with a fourth valve, and the fourth valve is connected into a control system.
And the third pipeline is connected into a twelfth pipeline through a second tee joint, the twelfth pipeline is connected with the standby air compression system, the twelfth pipeline is provided with a fifth valve, and the fifth valve is connected into the control system.
Furthermore, the oxygen-enriched air product produced by the air source device has the concentration of 27-45 percent, the temperature of 0-30 ℃, the pressure of 20-100 KPa and the dew point of-70 ℃, and the control system adjusts the concentration, the temperature and the pressure in real time according to the quality data of the pulverized coal and controls the corresponding conveying air speed of 20-30 m/s.
Furthermore, the purity of the nitrogen byproduct produced by the gas source device is more than 99.9 percent, the temperature is 15 +/-5 ℃, the pressure is 0.4 +/-0.05 MPa, and the dew point reaches-70 ℃.
Furthermore, the flow assisting pressure of a conical blanking pipe of the pulverized coal bunker is 0.4-0.6 MPa, the flow assisting pressure of the sealed isolation protection bunker is 0.2-0.4 MPa, and the blowing pressure of the metering scale and the expansion joint is 0.2-0.3 MPa.
The invention has the beneficial effects that:
1. the method for conveying the coal dust by the oxygen-enriched air solves the problems of high energy consumption and poor economical efficiency by using the pressurized air as a conveying medium. By effectively and reasonably controlling the conveying parameters and increasing safety protection measures, the operation and maintenance cost of compressed air is saved on the basis of fully ensuring the uniformity and stability of metering and conveying, the energy consumption and pollutant discharge are reduced, the risks of heating and spontaneous combustion explosion in metering and conveying pulverized coal by oxygen-enriched air are greatly reduced, and the double values of high economic benefit and high safety are achieved.
2. The air source device can produce oxygen-enriched air products and nitrogen byproducts. The oxygen-enriched air product is dry (the dew point reaches-70 ℃), high in pressure (energy-saving, no fan is needed for air supply), high in concentration, small in concentration, pressure and temperature fluctuation, and accurate and convenient to adjust; the oxygen-enriched air product can adjust the concentration, temperature, pressure and conveying air speed of conveying oxygen-enriched air in real time according to the change of the pulverized coal, and eliminates the conditions of heating and spontaneous combustion of the pulverized coal in the conveying process. The nitrogen byproduct has high purity (more than 99.9 percent), is dried (the dew point reaches-70 ℃), has high pressure and convenient pressure adjustment, and is introduced into the flow-assistant purging system to reach certain pressure on the basis of not increasing the production cost of an air source device, so that the flow-assistant purging pressure is met, and the stable and safe conveying is ensured together.
3. The invention replaces the compressed air generated by the air compressor with the nitrogen byproduct generated by the air source device to be used as the gas of the flow-assistant purging system, saves the electric power and the maintenance cost of the air compressor, and realizes the purpose of changing the nitrogen byproduct generated by the air source device into valuable. And the nitrogen byproduct is dry, the temperature is suitable, the purity is high, secondary impurity removal, drying, oil-water separation and the like are not needed, and a set of drying, impurity removal and oil-water separation system and corresponding use and maintenance cost are saved.
4. The invention utilizes the nitrogen byproduct to clean and purge the weighing scale, effectively avoids the failure and improper maintenance of a compressed air system, and avoids the use fault and equipment damage to the scale body, and simultaneously reduces the manual maintenance. The expansion joint is purged by using the nitrogen byproduct, and the purging of the dry inert gas is more thorough, so that the problem of combustible gas formed by deposition and oxidation of the pulverized coal is solved. The nitrogen byproduct is introduced into the conical blanking pipe and the sealed isolation protection bin of the pulverized coal bin and used for circular blowing flow aiding, the phenomena of arching, condensation and accumulation generated by the side walls of the pulverized coal bin and the sealed isolation protection bin are completely eradicated, the coal blanking is smoother, the metering is more stable and accurate, and the phenomenon that a circular blowing system is out of work due to compressed air is also eradicated.
5. The system used by the invention is additionally provided with the sealed isolation protection bin, so that the uniform stability of pulverized coal blanking is improved, and meanwhile, the safety risk that high-temperature coal feeding air is prevented from flowing into the pulverized coal bin from the metering scale, and is contacted with a large amount of pulverized coal in the pulverized coal bin for a long time to accumulate spontaneous combustion explosion is realized.
6. The system used by the invention is additionally provided with the pressure equalizing pipe connected with the dust collecting equipment at the upper part of the sealed isolation protection bin, so that the pressure of the sealed isolation protection bin is equalized, the coal uniformity and stability under the sealed isolation protection bin are ensured, and meanwhile, the flow of gas extracted from the sealed isolation protection bin is controlled by the valve, and the high-temperature air fleeed by the scale body is discharged in time. Meanwhile, the pressure equalization and dust collection are integrated, and the structure is simpler and more effective. The sealed isolation protection cabin is also provided with a temperature self-protection program, and the temperature value of the first temperature sensor exceeds an alarm value to start the nitrogen cooling self-protection program.
7. The flow-assistant purging system is connected into the standby compressed air system by the tee joint, and is automatically switched to the compressed air system when the nitrogen fails, so that the system can be ensured to run more stably.
8. The coal feeding system is connected with the standby fan by the tee joint, and when oxygen-enriched air fails and is overhauled, the system is automatically switched to the standby fan, so that the system can be ensured to run more stably.
Drawings
FIG. 1 is a schematic structural diagram of a system for conveying pulverized coal by oxygen-enriched air according to the present invention.
Fig. 2 is a schematic structural diagram of a gas source device.
Fig. 3 is a schematic diagram of a flow aid purging system.
The device comprises a gas source device 1, a pulverized coal bunker 2, a feeder 3, a sealed isolation protection bunker 4, a flow-assisting purging system 5, a metering scale 6, a first valve 7, an expansion joint 8, a second valve 9, a first temperature sensor 10, a first pressure gauge 11, a balanced pressure pipeline 12, a dust collecting device 13, a third valve 14, a first pipeline 15, a fifth valve 16, a first flow regulating valve 17, a second temperature sensor 18, a first flowmeter 19, a second pressure gauge 20, a second pipeline 21, a combustion device 22, a third pipeline 23, a second flow regulating valve 24, a third pressure gauge 25, a second flowmeter 26, a standby fan 27, a first tee joint 28, an eleventh pipeline 29, a fourth valve 30, a standby air compression system 31, a second tee joint 32 and a twelfth pipeline 33;
the system comprises an air filter 101, an air compressor 102, a precooling device 103, a molecular sieve adsorber 104, a heater 105, a main heat exchanger 106, an expander 107, a subcooler 108, a rectifying tower 109, a main condensing evaporator 110, a cold box 111 and an oxygen-enriched air buffer tank 112;
the system comprises a first buffer tank 501, a second buffer tank 502, a third buffer tank 503, a fourth pipeline 504, a third flow regulating valve 505, a fourth pressure gauge 506, a reducing tee 507, a fifth pipeline 508, a fourth flow regulating valve 509, a fifth pressure gauge 510, a fourth flow meter 511, a sixth pipeline 512, a seventh pipeline 513, a pressure reducing valve 514, an eighth pipeline 515, a fifth flow regulating valve 516, a sixth pressure gauge 517, a fifth flow meter 518, a ninth pipeline 519, a tenth pipeline 520 and a third flow meter 521.
Detailed Description
The invention is explained in more detail below with reference to exemplary embodiments and the accompanying drawings. The following examples are provided only for illustrating the present invention and are not intended to limit the scope of the present invention.
A method for conveying pulverized coal by oxygen-enriched air, the system used in conveying is shown in figure 1, and comprises an air source device 1, a pulverized coal bin 2, a blanking device 3, a sealing isolation protection bin 4, a pressure-equalizing self-protection device, a flow-assisting purging system 5 and a metering scale 6,
the conical blanking tube of the coal powder bin 2, the blanking device 3, the sealed isolation protection bin 4 and the metering scale 6 are sequentially connected, a first valve 7 is arranged between the conical blanking tube of the coal powder bin 2 and the blanking device 3, an expansion joint 8 is arranged between the blanking device 3 and the sealed isolation protection bin 4, and a second valve 9 is arranged between the sealed isolation protection bin 4 and the metering scale 6;
the sealed isolation protection bin 4 is provided with a first temperature sensor 10, a first pressure gauge 11 and a pressure-equalizing self-protection device; the pressure-equalizing self-protection device comprises a pressure-equalizing pipeline 12, one end of the pressure-equalizing pipeline 12 is connected to the upper part of the sealed isolation protection bin 4, the other end of the pressure-equalizing pipeline 12 is connected to the dust collecting equipment 13, and a third valve 14 is arranged on the pressure-equalizing pipeline 12;
an oxygen-enriched air outlet of the air source device 1 is connected to the metering scale 6 through a first pipeline 15, the first pipeline 15 is provided with a first flow regulating valve 17, a second temperature sensor 18, a first flow meter 19 and a second pressure gauge 20, and the metering scale 6 is connected to a combustion device 22 through a second pipeline 21;
a nitrogen outlet of the gas source device 1 is connected to the flow-assisting and purging system 5 through a third pipeline 23, the third pipeline 23 is provided with a second flow regulating valve 24, a third pressure gauge 25 and a second flow meter 26, and the flow-assisting and purging system 5 is respectively connected to a conical blanking pipe, an expansion joint 8, a sealed and isolated protection bin 4 and a metering scale 6 of the pulverized coal bin 2;
the first valve 7, the second valve 9, the first flow regulating valve 17, the second flow regulating valve 24, the first pressure gauge 11, the second pressure gauge 20, the third pressure gauge 25, the first flow meter 19, the second flow meter 26, the first temperature sensor 10, the second temperature sensor 18, the air source device 1, the blanking device 3, the flow-assisting purging system 5, the third valve 14 of the pressure-equalizing self-protection device and the metering scale 6 are all connected into a control system, and automatic control is realized by the control system.
The coal powder sequentially passes through the blanking device 3 and the sealed isolation protection bin 4 from the coal powder bin 2 to reach the metering scale 6 for metering, and the oxygen-enriched air produced by the air source device 1 is sent to the metering scale 6 through the first pipeline 15, is mixed with the coal powder and then is conveyed to the combustion equipment 22 through the second pipeline 21. The oxygen-enriched air is adjusted in real time by the control system according to the quality data of the pulverized coal to correspond to the concentration, the temperature and the pressure, and controls the corresponding conveying wind speed. According to the volatile content, the water content, the heat value and the fineness data of the conveyed pulverized coal, parameters of the concentration, the pressure, the wind speed and the temperature of the oxygen-enriched air are correspondingly calculated and matched, and the conditions of heating and spontaneous combustion of the pulverized coal in the conveying process are eliminated through accurate adjustment and matching of the parameters. The high volatile content, high heat value, low water content and small fineness are suitable for correspondingly reducing the oxygen-enriched concentration, if the oxygen-enriched concentration needs to be ensured, the conveying pressure and the air speed are strictly controlled, and meanwhile, the temperature of the oxygen-enriched air is properly reduced. On the contrary, parameters such as conveying temperature, air speed, pressure and the like are matched and increased in conveying of the pulverized coal with low heat value, low volatile content, high water content and coarse fineness. The present invention is not specifically illustrated by those skilled in the art based on calculations made by those skilled in the art. The byproduct nitrogen produced by the air source device 1 is introduced into a flow-assisting and purging system 5 through a third pipeline 23 and then is respectively sent into a cone blanking pipe of the pulverized coal bunker 2, a sealing isolation protection bin 4 is used for flow-assisting protection, the byproduct nitrogen is sent into an expansion joint 8 and a metering scale 6 is used for purging, the flow-assisting and purging start-stop, frequency, pressure and self-protection are controlled by a control system, the self-protection comprises pressure-equalizing self-protection and temperature self-protection, the opening degree of the pressure-equalizing self-protection is controlled by a third valve 14, the pressure of the sealing isolation protection bin 4 is controlled to be micro-negative pressure, and the temperature self-protection specifically is that a temperature value of a.
The gas source device 1 is shown in fig. 2 and comprises a compression module, a pre-cooling module, a purification module and a rectification module, wherein the compression module comprises an air filter 101 and an air compressor 102, the pre-cooling module comprises pre-cooling equipment 103, the purification module comprises a molecular sieve adsorber 104 and a heater 105, and the rectification module comprises a main heat exchanger 106, an expander 107, a subcooler 108, a rectification tower 109 and a main condensation evaporator 110;
an air filter 101 for filtering dust and mechanical impurities in the raw air;
an air compressor 102 for compressing the filtered raw material air to a set pressure;
the pre-cooling device 103 is used for pre-cooling the filtered and compressed raw material air;
a molecular sieve adsorber 104 for purifying the filtered, compressed and precooled raw material air to remove moisture and CO2、C2H2And the like;
a main heat exchanger 106 for cooling the filtered, compressed, precooled and purified raw material air; used for reheating oxygen-enriched air, reheating nitrogen, reheating part of the oxygen-enriched air and reheating the expanded nitrogen;
the rectifying tower 109 is used for rectifying the raw material air after filtration, compression, precooling, purification and cooling at low temperature to separate the raw material air into liquid air and nitrogen;
the subcooler 108 is used for subcooling the liquid air and reheating the oxygen-enriched air and the expanded nitrogen;
the main condensation evaporator 110 is used for exchanging heat between liquid air and nitrogen, wherein the liquid air is vaporized into oxygen-enriched air, and the nitrogen is condensed into liquid nitrogen;
the expansion machine 107 is used for expanding and refrigerating the nitrogen after partial reheating;
a heater 105 for heating the nitrogen to regenerate the molecular sieve adsorber 104.
The process for producing the oxygen-enriched air product and the nitrogen by-product is as follows:
firstly, raw material air is filtered to remove dust and mechanical impurities through an air filter 101 and then enters an air compressor 102 to be compressed to set pressure; then precooling the product by precooling equipment 103 and then purifying the product in a molecular sieve adsorber 104;
step two, the purified raw material air part is used as instrument air (not shown in fig. 2), and the rest part enters the main heat exchanger 106 to be cooled and then enters the rectifying tower 109 to participate in rectification;
step three, the air is rectified by a rectifying tower 109 and then is separated into liquid air and nitrogen, the liquid air is subcooled by a cooler 108 and throttled by a throttle valve and then enters a main condensation evaporator 110 to exchange heat with the nitrogen, the liquid air is vaporized into oxygen-enriched air, and the oxygen-enriched air is reheated by the cooler 108 and a main heat exchanger 106 and then enters a cooling box 111 to enter an oxygen-enriched air buffer tank 112 to provide an oxygen-enriched air product; part of nitrogen is introduced into a main condensation evaporator 110 to exchange heat with liquid air, the nitrogen is condensed into liquid nitrogen, the liquid nitrogen is introduced into the top of a rectifying tower 109 to serve as reflux liquid, the rest of the nitrogen enters a main heat exchanger 106, part of the nitrogen is reheated and then is discharged from a cooling box 111 to provide a nitrogen byproduct through an external pipeline (a third pipeline 23), the rest of the nitrogen is reheated and then enters an expander 107 to be expanded and refrigerated, the expanded nitrogen is reheated through a cooler 108 and the main heat exchanger 106 and then is introduced into a molecular sieve adsorber 104 as regeneration gas after being heated by a heater 105, and the rest of the nitrogen is emptied.
The oxygen-enriched air produced by the air source device 1 has the concentration of 27-45%, the temperature of 0-30 ℃, the pressure of 20-100 KPa and the dew point of-70 ℃, and the concentration, the temperature and the pressure of the oxygen-enriched air are adjusted in real time by a control system according to the quality data of the pulverized coal, and the corresponding conveying wind speed is controlled to be 20-30 m/s.
The purity of the nitrogen byproduct produced by the gas source device 1 is more than 99.9 percent, the temperature is 15 +/-5 ℃, the pressure is 0.4 +/-0.05 MPa, and the dew point reaches-70 ℃.
Preferably, the conveying system further comprises a standby fan 27, the first pipeline 15 is connected to an eleventh pipeline 29 through a first tee joint 28, the eleventh pipeline 29 is connected with the standby fan 27, the eleventh pipeline 29 is provided with a fourth valve 30, and the fourth valve 30 is connected to the control system. When oxygen-enriched air fails and is overhauled, the air is automatically switched to the standby fan 27, and the system is ensured to run more stably.
The flow-aid purging system 5 is shown in fig. 3 and comprises a first buffer tank 501, a second buffer tank 502 and a third buffer tank 503, wherein the volumes of the first buffer tank 501, the second buffer tank 502 and the third buffer tank 503 are from large to small. The first cache tank 501 is provided with a nitrogen inlet and a nitrogen outlet, the nitrogen inlet is connected with the third pipeline 23, a nitrogen byproduct produced by the gas source device 1 is used as gas for the flow-assisting and purging system 5, the nitrogen outlet is connected with the fourth pipeline 504, the fourth pipeline 504 is provided with a third flow regulating valve 505, a fourth pressure gauge 506 and a third flow meter 521, and the fourth pipeline 504 is divided into two branch pipes, namely a first nitrogen outlet and a second nitrogen outlet, through a reducing tee 507; the first nitrogen outlet is connected with the second buffer tank 502 through a fifth pipeline 508, the fifth pipeline 508 is provided with a fourth flow regulating valve 509, a fifth pressure gauge 510 and a fourth flow meter 511, the second buffer tank 502 is respectively sent to a cone blanking pipe of the pulverized coal bunker 2 and the sealed isolated protection bunker 4 through a sixth pipeline 512 and a seventh pipeline 513, and the seventh pipeline 513 is provided with a pressure reducing valve 514; the second nitrogen outlet is connected with the third buffer tank 503 through an eighth pipeline 515, the eighth pipeline 515 is provided with a fifth flow regulating valve 516, a sixth pressure gauge 517 and a fifth flow meter 518, and the third buffer tank 503 is respectively connected with the expansion joint 8 and the metering scale 6 through a ninth pipeline 519 and a tenth pipeline 520.
Preferably, the flow-assisting purging system 5 further comprises a standby air compression system 31, the third pipeline 23 is connected to a twelfth pipeline 33 through a second tee 32, the twelfth pipeline 33 is connected to the standby air compression system 31, the twelfth pipeline 33 is provided with a fifth valve 16, and the fifth valve 16 is connected to the control system. When the nitrogen fails, the system is automatically switched to the standby compressed air system 31, and the system is ensured to run more stably.
The control system controls the flow assisting pressure of a conical blanking pipe of the pulverized coal bunker 2 to be 0.4-0.6 MPa, the flow assisting pressure of the sealed isolation protection bunker 4 to be 0.2-0.4 MPa, and the blowing pressure of the metering scale 6 and the expansion joint 8 to be 0.2-0.3 MPa.

Claims (10)

1. A method for conveying pulverized coal by oxygen-enriched air is characterized in that a system used in conveying comprises an air source device, a pulverized coal bin, a blanking device, a sealed and isolated protection bin, a pressure-equalizing self-protection device, a flow-assistant purging system and a metering scale,
the device comprises a pulverized coal bunker, a conical blanking pipe, a blanking device, a sealing isolation protection bin and a metering scale, wherein the conical blanking pipe, the blanking device, the sealing isolation protection bin and the metering scale are sequentially connected;
the sealed isolation protection bin is provided with a first temperature sensor, a first pressure gauge and a pressure-equalizing self-protection device;
an oxygen-enriched air outlet of the air source device is connected to the metering scale through a first pipeline, the first pipeline is provided with a first flow regulating valve, a second temperature sensor, a first flowmeter and a second pressure gauge, and the metering scale is connected to the combustion equipment through a second pipeline;
a nitrogen outlet of the gas source device is connected to a flow-assisting purging system through a third pipeline, the third pipeline is provided with a second flow regulating valve, a third pressure gauge and a second flow meter, and the flow-assisting purging system is respectively connected to a conical blanking pipe, an expansion joint, a sealed isolation protection bin and a metering scale of the pulverized coal bin;
the first valve, the second valve, the first flow regulating valve, the second flow regulating valve, the first pressure gauge, the second pressure gauge, the third pressure gauge, the first flow meter, the second flow meter, the first temperature sensor, the second temperature sensor, the air source device, the blanking device, the flow-assisting purging system, the pressure-equalizing self-protection device and the metering scale are all connected into a control system, and the control system realizes automatic control;
the coal powder sequentially passes through a feeder and a sealed isolation protection bin from a coal powder bin to reach a metering scale for metering, oxygen-enriched air produced by an air source device is adjusted in real time by a control system according to the quality data of the coal powder to correspond to concentration, temperature and pressure, and the corresponding conveying air speed is controlled to be conveyed to the metering scale through a first pipeline, mixed with the coal powder and conveyed to combustion equipment through a second pipeline; nitrogen produced by the air source device is introduced into the flow-assisting and purging system through a third pipeline, and then is respectively sent into a conical blanking pipe and a sealed isolation protection bin of the pulverized coal bin for flow-assisting protection, and is sent into an expansion joint and a metering scale for purging, and the flow-assisting and purging start-stop, frequency, pressure and self-protection are controlled by the control system.
2. The method for conveying pulverized coal by oxygen-enriched air according to claim 1, wherein the air source device comprises a compression module, a precooling module, a purification module and a rectification module, the compression module comprises an air filter and an air compressor, the precooling module comprises precooling equipment, the purification module comprises a molecular sieve adsorber and a heater, and the rectification module comprises a main heat exchanger, an expander, a subcooler, a rectification tower and a main condensation evaporator;
an air filter for filtering dust and mechanical impurities in the raw air;
the air compressor is used for compressing the filtered raw material air to a set pressure;
the precooling equipment is used for precooling the filtered and compressed raw material air;
the molecular sieve adsorber is used for purifying the filtered, compressed and precooled raw material air;
the main heat exchanger is used for cooling the filtered, compressed, precooled and purified raw material air; used for reheating oxygen-enriched air, reheating nitrogen, reheating part of the oxygen-enriched air and reheating the expanded nitrogen;
the rectifying tower is used for rectifying the raw material air after filtering, compressing, precooling, purifying and cooling at low temperature to separate the raw material air into liquid air and nitrogen;
the subcooler is used for subcooling the liquid air and reheating the oxygen-enriched air and the expanded nitrogen;
the main condensation evaporator is used for exchanging heat between liquid air and nitrogen, the liquid air is vaporized into oxygen-enriched air, and the nitrogen is condensed into liquid nitrogen;
the expansion machine is used for expanding and refrigerating the nitrogen after partial reheating;
a heater for heating the nitrogen to regenerate the molecular sieve adsorber;
the process for producing the oxygen-enriched air product and the nitrogen by-product is as follows:
firstly, filtering raw material air by an air filter to remove dust and mechanical impurities, and then compressing the air to a set pressure by an air compressor; precooling the product by precooling equipment, and then purifying the product in a molecular sieve adsorber;
step two, part of the purified raw material air is used as instrument air, and the rest part of the purified raw material air enters a main heat exchanger to be cooled and then enters a rectifying tower to participate in rectification;
step three, separating the air into liquid air and nitrogen after the air is rectified by a rectifying tower, allowing the liquid air to enter a main condensation evaporator after being supercooled by a cooler and throttled by a throttle valve to exchange heat with the nitrogen, vaporizing the liquid air into oxygen-enriched air, and allowing the oxygen-enriched air to enter an oxygen-enriched air buffer tank from a cooling box after being reheated by the cooler and a main heat exchanger so as to provide an oxygen-enriched air product; part of nitrogen is introduced into a main condensation evaporator to exchange heat with liquid air, the nitrogen is condensed into liquid nitrogen, the liquid nitrogen is introduced into the top of a rectifying tower to be used as reflux liquid, the rest of nitrogen enters a main heat exchanger, part of nitrogen is reheated and then discharged out of a cooling box to provide a nitrogen byproduct, the rest of nitrogen enters an expander to be expanded and refrigerated, the part of expanded nitrogen is reheated by a cooler and the main heat exchanger to be used as regeneration gas, the regeneration gas is heated by a heater and then introduced into a molecular sieve adsorber, and the rest of nitrogen is discharged.
3. The method for conveying pulverized coal by oxygen-enriched air according to claim 1, wherein the flow-assisting purging system comprises a first buffer tank, a second buffer tank and a third buffer tank, the first buffer tank is provided with a nitrogen inlet and a nitrogen outlet, the nitrogen inlet is connected with a third pipeline, the nitrogen outlet is connected with a fourth pipeline, the fourth pipeline is provided with a third flow regulating valve, a fourth pressure gauge and a third flow meter, the fourth pipeline is divided into two branch pipes through a reducing tee, and the branch pipes are respectively a first nitrogen outlet and a second nitrogen outlet; the first nitrogen outlet is connected with a second cache tank through a fifth pipeline, a fourth flow regulating valve, a fifth pressure gauge and a fourth flow meter are arranged on the fifth pipeline, the second cache tank is respectively sent to a conical part blanking pipe and a sealed isolation protection bin of the pulverized coal bin through a sixth pipeline and a seventh pipeline, and a pressure reducing valve is arranged on the seventh pipeline; and the second nitrogen outlet is connected with a third cache tank through an eighth pipeline, the eighth pipeline is provided with a fifth flow regulating valve, a sixth pressure gauge and a fifth flow meter, and the third cache tank is respectively connected to the expansion joint and the metering scale through a ninth pipeline and a tenth pipeline.
4. The method for conveying pulverized coal by oxygen-enriched air as claimed in claim 3, wherein the volumes of the first buffer tank, the second buffer tank and the third buffer tank are from large to small.
5. The method for transporting pulverized coal by oxygen-enriched air according to claim 1, wherein the sealed and isolated protection bin is provided with a first temperature sensor, a first pressure gauge and a pressure-equalizing self-protection device, the pressure-equalizing self-protection device comprises an equalizing pressure pipeline, one end of the equalizing pressure pipeline is connected to the upper part of the sealed and isolated protection bin, the other end of the equalizing pressure pipeline is connected to dust collecting equipment, the equalizing pressure pipeline is provided with a third valve control opening, and the pressure of the sealed and isolated protection bin is controlled to be micro negative pressure; and starting a nitrogen cooling self-protection program when the temperature value of the first temperature sensor exceeds the alarm value.
6. The method for conveying pulverized coal by oxygen-enriched air as claimed in claim 1, further comprising a standby fan, wherein the first pipeline is connected to an eleventh pipeline through a first tee joint, the eleventh pipeline is connected with the standby fan, the eleventh pipeline is provided with a fourth valve, and the fourth valve is connected to the control system.
7. The method for conveying pulverized coal by oxygen-enriched air as claimed in claim 1, further comprising a standby air compression system, wherein the third pipeline is connected to a twelfth pipeline through a second tee joint, the twelfth pipeline is connected with the standby air compression system, the twelfth pipeline is provided with a fifth valve, and the fifth valve is connected to the control system.
8. The method for conveying pulverized coal by oxygen-enriched air as claimed in claim 1, wherein the oxygen-enriched air produced by the air source device has a concentration of 27% -45%, a temperature of 0-30 ℃, a pressure of 20-100 KPa, a dew point of-70 ℃, and a control system for adjusting the concentration, temperature and pressure of pulverized coal in real time according to the quality data of the pulverized coal and controlling the corresponding conveying wind speed of 20-30 m/s.
9. The method for conveying pulverized coal by oxygen-enriched air as claimed in claim 1, wherein the purity of the nitrogen byproduct produced by the air source device is above 99.9%, the temperature is 15 ± 5 ℃, the pressure is 0.4 ± 0.05MPa, and the dew point reaches-70 ℃.
10. The method for conveying pulverized coal by oxygen-enriched air as claimed in claim 1, wherein the flow assisting pressure of a conical blanking pipe of the pulverized coal bin is 0.4-0.6 MPa, the flow assisting pressure of the sealed isolation protection bin is 0.2-0.4 MPa, and the blowing pressure of the metering scale and the expansion joint is 0.2-0.3 MPa.
CN202010120354.5A 2020-02-26 2020-02-26 Method for conveying pulverized coal by oxygen-enriched air Active CN111189060B (en)

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CN110332520A (en) * 2019-08-15 2019-10-15 南宁方力电气有限公司 A kind of coal dust oxygen-enriched combustion system
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JPS5659125A (en) * 1979-10-17 1981-05-22 Denka Consult & Eng Co Ltd Fuel and air separate feed type burner for pneumatically conveyed solid fuel
US20120222593A1 (en) * 2005-12-28 2012-09-06 Jupiter Oxygen Corporation Oxy-fuel combustion with integrated pollution control
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