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WO2016037379A1 - 一种褐煤干燥提质的方法及装置 - Google Patents

一种褐煤干燥提质的方法及装置 Download PDF

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Publication number
WO2016037379A1
WO2016037379A1 PCT/CN2014/086751 CN2014086751W WO2016037379A1 WO 2016037379 A1 WO2016037379 A1 WO 2016037379A1 CN 2014086751 W CN2014086751 W CN 2014086751W WO 2016037379 A1 WO2016037379 A1 WO 2016037379A1
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WO
WIPO (PCT)
Prior art keywords
lignite
cylindrical heater
pressure
low
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2014/086751
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English (en)
French (fr)
Inventor
孙栋
蔡剑毅
郭元强
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hulunbuir Hongyi Coal Science And Technology Development Co Ltd
Original Assignee
Hulunbuir Hongyi Coal Science And Technology Development Co Ltd
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Filing date
Publication date
Priority claimed from CN201420524470.3U external-priority patent/CN204111710U/zh
Priority claimed from CN201410464341.4A external-priority patent/CN104194856A/zh
Application filed by Hulunbuir Hongyi Coal Science And Technology Development Co Ltd filed Critical Hulunbuir Hongyi Coal Science And Technology Development Co Ltd
Publication of WO2016037379A1 publication Critical patent/WO2016037379A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/06—Methods of shaping, e.g. pelletizing or briquetting
    • C10L5/08—Methods of shaping, e.g. pelletizing or briquetting without the aid of extraneous binders
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • 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
    • F26B21/06—Controlling, e.g. regulating, parameters of gas supply
    • F26B21/10—Temperature; Pressure
    • 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
    • F26B3/06—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 flowing through the materials or objects to be dried

Definitions

  • the invention relates to the field of processing and utilization of lignite, in particular to a device and a method for drying and processing lignite.
  • lignite is very large on the earth, but it has high water content, low unit heat value, easy self-ignition, easy powdering, low mechanical strength and thermal stability, which is not conducive to direct transportation and utilization.
  • countries around the world have done a lot of research on reducing lignite moisture, thereby increasing unit heat value and improving coal quality.
  • Mainly 1. High energy consumption, relying on a large amount of coal to evaporate a large amount of water in raw coal; 2. Environmentally friendly carbon emissions are large and polluting; 3. Finished powder is severe, mechanical strength and thermal stability are lower than that of raw coal. It is not conducive to transportation; 4, the equipment is complex, the cost is high, the production cost is high, and it is difficult to use in large-scale industrialization.
  • the present invention provides a method and apparatus for drying and upgrading lignite.
  • the brown coal moisture after drying by the method and the device is significantly reduced, the unit heat value is increased, the particle volume is reduced, the water absorption is less, the mechanical hardness and thermal stability are increased, and the powdering and weathering are greatly reduced.
  • Most of the vaporization heat of the water in the drying process is recycled, the energy consumption is low, the equipment cost is low, the production cost is low, the environmental protection is easy to control, and it is easy to mass-produce.
  • a device for dry upgrading of lignite comprising: means for generating low pressure superheated steam or generating low pressure superheated gas, and a cylindrical heater connected to the apparatus; said means for generating low pressure superheated steam comprising a boiler, said generating low pressure
  • the device for superheating gas comprises a gas booster, a gas storage tank and a heat exchanger connected in sequence, and the cylindrical heater is connected to the boiler or the heat exchanger through a set of intake air combination tubes; a first material pusher is disposed, and the cylindrical heater is provided with a feed pipe, a discharge pipe and one or more exhaust valves, and a wind shutoff device is arranged on the feed pipe and the drop pipe;
  • the air intake combined tube includes a plurality of spaced apart branch pipes connected to the body of the cylindrical heater.
  • a lignite drying and upgrading device as described above, further comprising a coal bar forming machine having a feeding end connecting the blanking tube on the cylindrical heater, and a taper a discharge end, the narrow mouth of the tapered discharge end is a discharge port;
  • a second material pusher is disposed in the coal rod forming machine.
  • the intake manifold further comprises a manifold connecting a plurality of branch pipes, wherein the manifold is connected to the heat exchanger through an intermediate pipe, and the distance between the adjacent branches is 10 cm. -30cm .
  • a method for drying and upgrading brown coal which comprises the steps of: injecting an incoming low-pressure superheated gas or low-pressure superheated steam into a cylindrical heater to heat the lignite injected into the cylindrical heater, the entering
  • the pressure of the low-pressure superheated gas or the low-pressure superheated steam is between 0.1 MPa and above, and the temperature is between 105 ° C and 400 ° C; the pressure in the cylindrical heater is maintained at 0.1 MPa or more, and the cylindrical heater is provided with
  • the exhaust valve is opened when the pressure in the cylindrical heater is greater than the pressure of the incoming low pressure superheated gas or low pressure superheated steam; the heated lignite is discharged from the cylindrical heater.
  • the lignite discharged from the cylindrical heater is used to accelerate the evaporation of water to obtain a finished product; or the lignite discharged from the cylindrical heater enters a coal rod forming machine and is tapped by a coal rod forming machine The end is extruded to form a coal rod to produce a finished product.
  • the invention adopts a cylindrical heater with a propeller, and pressurizes the cylindrical heater through a boiler, or a gas storage tank and a heat exchanger, so that lignite naturally evaporates most of the water after processing, and the processing cost is consumed.
  • the energy can be low and the unit heat value of lignite is increased.
  • the lignite raw coal has poor strength and is easily weathered and powdered.
  • Other normal or negative pressure dry lignite powder has a very high powdering rate, basically no mechanical strength and thermal stability, and the product can only be used as a low-grade fuel.
  • the present invention controls the pressure and temperature in the cylindrical heater through the exhaust valve and the air closing device, and the mechanical strength and thermal stability of the lignite can reach more than 70%.
  • the fuel it can be used as a steam, coal chemical industry. Raw coal in other fields.
  • the invention has the advantages of simple process, safe production, low equipment cost, low production cost, and easy large-scale industrial production and promotion.
  • Figure 1 is a schematic view of the structure of the lignite drying and upgrading apparatus of the present invention (providing low pressure superheated gas);
  • FIG. 2 is a schematic structural view 2 of the apparatus for drying and upgrading brown coal according to the present invention (providing low-pressure superheated steam).
  • a lignite dry upgrading device as shown in FIG. 1 includes a device for generating low pressure superheated steam or generating low pressure superheated gas, a set of intake manifold 4 and a cylindrical heater 5, and may further include a coal rod Forming machine 12.
  • the apparatus for generating low-pressure superheated gas includes a gas booster 1, a gas storage tank 2, and a heat exchanger 3 which are sequentially connected, and the cylindrical heater 5 is connected to the heat exchanger 3 through the intake manifold 4.
  • the gas booster 1 can be generally referred to as an air compressor or a gas booster pump
  • the heat exchanger 3 can be a device that can heat the gas and has a certain pressure resistance performance, such as coal burning, steam combustion, and electric heating.
  • the apparatus for generating low-pressure superheated steam includes a boiler 17, and the cylindrical heater 5 is connected to the boiler 17 through an intake manifold.
  • the cylindrical heater 5 is a cylindrical container having a certain withstand voltage.
  • a first material propeller 7 driven by the first motor 8 is disposed therein, and the first material propeller 7 may be a auger type auger or a vane type auger.
  • the cylindrical heater 5 is provided with a feed pipe 10, a discharge pipe 11, and one or more exhaust valves, and the exhaust valve may be disposed only on the body of the cylindrical heater 5, or It is disposed on the drop tube 11 of the cylindrical heater 5.
  • the body of the cylindrical heater 5 is provided with two exhaust valves 6A, 6B.
  • the discharge pipe 11 of the cylindrical heater 5 is simultaneously provided with an exhaust valve 6C for setting the pressure value in the cylindrical heater 5 as needed, and automatically opening the exhaust gas under an overpressure condition.
  • the feeding tube 10 and the blanking tube 11 of the cylindrical heater 5 are respectively provided with first and second closing devices 9A, 9B, and the first and second closing devices 9A, 9B can be closed. The device can prevent the airflow from escaping when the material passes, thereby ensuring a positive pressure environment inside the cylinder heater 5.
  • the intake air combination pipe 4 includes a plurality of spaced apart branch pipes 4A for connecting the body of the cylindrical heater 5 and a main pipe 4B, and the main pipe 4B is connected to heat exchange through an intermediate pipe 4C.
  • Device 3 The branch pipe 4A, the main pipe 4B, and the intermediate pipe 4C are all pipes having a certain pressure resistance.
  • the distance between adjacent branch pipes 4A of the present invention is set to be 10 cm to 30 cm to balance and save the amount of gas or steam injected.
  • a coal bar forming machine 12 having a feed pipe 11 connected to the cylindrical heater 5 may be added.
  • the material end, and a tapered discharge end 13, the narrow mouth portion of the tapered discharge end 13 which is reduced in diameter from the inside to the outside is the discharge port 14.
  • the coal bar forming machine 12 is provided with a second material pusher 16 driven by a second motor 15, which is a auger type auger.
  • the method for drying and upgrading the lignite of the present invention by using the above-mentioned lignite drying and upgrading device is as follows:
  • the gas air, carbon dioxide, or the like which can be used as a non-fuel gas for heat conduction
  • the gas booster 1 pressurized by the gas booster 1 to 0.1 MPa or more, preferably 0.3 MPa to 0.5 MPa.
  • the thermal stability of the lignite processed by the subsequent process is better, but the process requirements and cost of the equipment are higher.
  • the pressurized gas is heated by the heat exchanger 3 to 105 ° C to 400 ° C, preferably 150 ° C to 250 ° C to generate a low pressure superheated gas. Because lignite is heated by hot air above 105 °C, a series of chemical reactions begin to occur. The reaction between 150 °C and 250 °C is relatively fast and complete. When it exceeds 250 °C, a small amount of volatiles will escape the polluted tail gas, and when it exceeds 400 °C. Some lignites are too long in the heating chamber, and may be ignited due to the loss of most of the water, and the safety is lowered.
  • the low-pressure superheated gas generated in the above steps 1 and 2 can also be replaced by low-pressure superheated steam, which can be generated by the pressure heating of the boiler 17, and the generated low-pressure superheated steam should be pressurized to 0.1 MPa or more, preferably 0.3. Between MPa and 0.5 MPa, the temperature is raised to between 105 ° C and 400 ° C, preferably between 150 ° C and 250 ° C.
  • Step 3 the hot air heated by the heat exchanger 3 or the low-pressure superheated steam generated by the boiler 17 is sprayed into the body of the cylindrical heater 5 through a plurality of branch pipes 4A to heat the input into the cylindrical heater 5 Lignite inside.
  • the raw coal enters the cylindrical heater 5 from the feed pipe 10, and the pressure of the cylindrical heater 5 is maintained at 0.1 MPa or more, preferably 0.3-0.5 MPa, and is advanced by the first material pusher 7 while being subjected to Heating of the hot air and hot steam entering the intake manifold 4.
  • the heated lignite directly evaporates part of the water from the surface and the inside, and simultaneously produces a series of changes in the nature of the positive pressure environment, resulting in tight molecular structure, reduced volume, increased mechanical strength and thermal stability, hydrophilicity, The oxophilicity is reduced and a portion of the heat and carbon dioxide are released, which indirectly evaporates a portion of the moisture in the lignite.
  • Lignite starts to react at 105 ° C, and the pressure is stronger than 0.1 MPa. The higher the temperature in the range of 105 ° C - 250 ° C, the faster the reaction, and the excess of 250 ° C will cause the volatiles to escape and convert to dry distillation.
  • the pressure set in the cylindrical heater 5 should be maintained at 0.1 MPa or more, preferably between 0.3 MPa and 0.5 MPa. However, due to the intake of the intake manifold 4 and a portion of the steam and carbon dioxide generated by the lignite, the pressure in the cylindrical heater 5 is increased, and when the pressure set in the cylindrical heater 5 is exceeded, three The exhaust valves 6A, 6B, and 6C disposed on the cylindrical heater 5 are automatically opened for exhausting, and the exhausted gas is a low-temperature gas, and the temperature is lower than 100 ° C, and a large amount of condensation is carried out, and is atomized by a positive pressure. Moisture, and then discharge the gas to the next step of environmental protection.
  • Step 4 If the raw coal to be processed is mainly lump coal having a large particle size, after the heated lignite is discharged from the blanking pipe 11 of the cylindrical heater 5, most of the water condensed on the surface of the lignite particles will naturally evaporate. And use the fan to blow air, strengthen the air flow on the surface of lignite, can accelerate the evaporation of water, until the coal temperature is reduced, it is the finished product.
  • the heated lignite is discharged from the blanking pipe 11 of the cylindrical heater 5, and then enters the coal bar forming machine 12, and is advanced by the second pusher 16.
  • the diameter of the discharge port 14 of the discharge end 13 is reduced, and the pulverized coal is extruded to form a coal rod which is discharged through the discharge port 14.
  • the condensed water on the surface of the pulverized coal is used as a lubricant for extrusion molding.
  • the change in the yield and strength can be adjusted by changing the length and compression ratio of the discharge end 13, and the prepared coal rod will naturally evaporate most of the water after being cooled. At the same time, the strength is increased and the powder is substantially eliminated.

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Abstract

一种褐煤干燥提质的装置，包括产生低压过热气体或蒸汽的装置、进气组合管（4）和圆筒式加热器（5）。圆筒式加热器（5）设有第一物料推进器（7）、进料管（10）、出料管（11）及一个以上的排气阀（6A、6B、6C），进料管（10）和出料管（11）上设有关风装置（9A、9B），出料管（11）可连接有一煤棒成型机（12）。利用该装置实施的褐煤干燥提质的方法步骤是通过气体增压机（1）将储气罐（2）内的气体加压至0.1MPa以上后经过换热器（3）加温到105℃-400℃；加温后的热气分段喷入圆筒式加热器（5）内加热褐煤，并使圆筒式加热器（5）内的压力保持在0.1MPa以上，排气阀（6A、6B、6C）在圆筒式加热器（5）内的压力大于储气罐（2）内的气体压力时开启，加热后的褐煤从出料管（11）排出。经该方法和装置干燥后的褐煤的机械硬度和热稳定性升高。干燥过程环保、水耗能低且设备造价低，易于大批量生产。

Description

一种褐煤干燥提质的方法及装置 技术领域
本发明涉及褐煤的加工利用领域，尤其是涉及指一种褐煤干燥加工的装置及方法。
背景技术
众所周知，褐煤在地球上赋存量非常巨大，但水份高，单位热值低，易自燃，易粉化，机械强度和热稳定性低，不利于直接运输和利用。多年来，世界各国对于降低褐煤水份，从而提高单位热值，提高煤质进行了大量的研究，但还没有成熟的技术流程，存在诸多弊端。主要有：1、耗能高，靠大量的燃煤去蒸发原煤中大量的水份；2、环保碳排放大，污染大；3、成品粉化严重，机械强度、热稳定性比原煤更低，不利于运输；4、设备复杂、造价高、生产成本高，难于大型工业化运用。
发明内容
针对现有技术存在的问题，本发明提供一种褐煤干燥提质的方法及装置。经该方法和装置干燥后的褐煤水份降低显著，单位热值升高，且颗粒体积缩小，水份回吸少，机械硬度和热稳定性升高，粉化、风化大大降低。干燥过程水的汽化热大部分回收利用，耗能低且设备造价低，生产成本低，环保易于控制，易于大批量生产。
为实现上述目的，本发明技术方案为：
一种褐煤干燥提质的装置，包括产生低压过热蒸汽或产生低压过热气体的装置，和一连接该装置的圆筒式加热器；所述产生低压过热蒸汽的装置包括一锅炉，所述产生低压过热气体的装置包括依序相接气体增压机、储气罐和换热器，圆筒式加热器通过一组进气组合管连接锅炉或换热器；所述的圆筒式加热器内设有第一物料推进器，且该圆筒式加热器上设有进料管、出料管及一个以上的排气阀，于所述的进料管和落料管上设有关风装置；所述的进气组合管包括有多个间隔设置的支管，所述支管连接在圆筒式加热器的本体上。
如前所述的一种褐煤干燥提质的装置，还包括一煤棒成型机，该煤棒成型机具有一连接圆筒式加热器上的落料管的进料端，和一呈锥状的出料端，该锥状的出料端的窄口部为出料口； 所述煤棒成型机内设有第二物料推进器。
如前所述的一种褐煤干燥提质的装置，所述进气组合管还包括一连接多个支管的总管，该总管通过一中间管连接换热器，且相邻支管的间隔距离为10cm-30cm 。
如前所述的一种褐煤干燥提质的装置，所述排气阀设置在圆筒式加热器的本体上， 还设置在圆筒式加热器的落料管上。
一种褐煤干燥提质的方法，其实施步骤是：向圆筒式加热器内分段喷入进入的低压过热气体或低压过热蒸汽，以加热投入圆筒式加热器内的褐煤，所述进入的低压过热气体或低压过热蒸汽的压力在0.1MPa以上、且温度在105℃-400℃之间；所述圆筒式加热器内的压力保持在0.1MPa以上，圆筒式加热器上设有的排气阀在圆筒式加热器内的压力大于进入的低压过热气体或低压过热蒸汽的压力时开启；加热后的褐煤从圆筒式加热器排出。从圆筒式加热器排出的褐煤用风机以加速其水份蒸发，制得成品；或从圆筒式加热器排出的褐煤进入一煤棒成型机，并经煤棒成型机的锥状出料端挤压形成煤棒，制得成品。
上述技术方案的有益之处在于：
第一，节能。本发明采用具有推进器的圆筒式加热器，通过锅炉，或储气罐和换热器对圆筒式加热器进行加压加热，使褐煤在加工后自然蒸发掉大部分水份，加工耗能低，提高了褐煤的单位热值。
第二，提高运用范围。褐煤原煤强度差，易风化粉化。其它常压或负压干燥的褐煤粉化率极高，基本无机械强度和热稳定性，产品只能用作低级燃料。但本发明通过排气阀和关风装置对圆筒式加热器内的压力和温度进行控制，褐煤的机械强度和热稳定性都可达到70%以上，除了燃料外，可用作造汽、煤化工等其它领域的原料煤。
第三，本发明工艺简单、生产安全、设备造价低、生产成本低，易于大型工业化生产和推广。
附图说明
此处所说明的附图用来提供对本发明的进一步理解，构成本发明的一部分，本发明的示意性实施例及其说明用于解释本发明，并不构成对本发明的不当限定。在附图中：
图1是本发明褐煤干燥提质的装置的结构示意图一（提供低压过热气体）；
图2是本发明褐煤干燥提质的装置的结构示意图二（提供低压过热蒸汽）。
具体实施方式
为了使本发明所要解决的技术问题、技术方案及有益效果更加清楚、明白，以下结合附图和实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅用以解释本发明，并不用于限定本发明。
如图1所示的一种褐煤干燥提质的装置，包括产生低压过热蒸汽或产生低压过热气体的装置，一组进气组合管4和一圆筒式加热器5，还可包括有一煤棒成型机12。
所述产生低压过热气体的装置包括依序相接的气体增压机1、储气罐2和换热器3，圆筒式加热器5通过进气组合管4连接换热器3。所述气体增压机1可为一般指空压机或气体增压泵，所述换热器3可以是燃煤、燃汽、电加热等可以使气体升温且有一定耐压性能的设备。
如图2所示，所述产生低压过热蒸汽的装置包括一锅炉17，圆筒式加热器5通过进气组合管连接锅炉17。
如图1、2所示，所述的圆筒式加热器5是有一定耐压的筒状容器， 其内设有一由第一电机8驱动的第一物料推进器7，该第一物料推进器7可以是绞龙式螺旋推进器，也可以是叶片式螺旋推进器。所述圆筒式加热器5上设有进料管10、出料管11及一个以上的排气阀，所述排气阀可以仅设置在圆筒式加热器5的本体上，还可以同时设置在圆筒式加热器5的落料管11上。在本实施例中，圆筒式加热器5的本体上设置有两个排气阀6A、6B, 圆筒式加热器5的落料管11上同时设有一个排气阀6C，以根据需要设定圆筒式加热器5内的压力值，在超压状况下自动开启排气。所述圆筒式加热器5的进料管10和落料管11上还分别设有第一、二关风装置9A、9B，所述的第一、二关风装置9A、9B可为关门器，以在物料通过的时候能阻止气流逸出，从而保证圆筒加热器5内部的正压环境。
所述的进气组合管4包括有多个间隔设置的支管4A，该多个支管4A用于连接圆筒式加热器5的本体和一总管4B，该总管4B通过一中间管4C连接换热器3。所述的支管4A、总管4B和中间管4C均为具有一定耐压能力的管道。本发明相邻支管4A之间的距离设为10cm-30cm，以均衡和节省气体或蒸汽的喷入量。
如果进行加工的原煤主要为粒径低于6mm的粉煤时，可加设一煤棒成型机12，该煤棒成型机12具有一连接圆筒式加热器5上的落料管11的进料端，和一呈锥状的出料端13，该由内向外口径缩小的锥状的出料端13的窄口部为出料口14。所述煤棒成型机12内设有一由第二电机15驱动的第二物料推进器16，该第二物料推进器16为绞龙式螺旋推进器。
利用前述的褐煤干燥提质的装置，本发明褐煤干燥提质的方法，其实施步骤如下：
步骤一，通过气体增压机1将储气罐2内的气体（空气、二氧化碳等可用作导热的非燃料气体）加压至0.1MPa以上，最好是在0.3MPa至0.5MPa之间。当气体压力越高，后续工艺加工出的褐煤热稳定性越好，但是设备的工艺要求和造价越高。
步骤二，加压后的气体经过换热器3加温到105℃-400℃，最好是150℃-250℃，以产生低压过热气体。因为褐煤受到105℃以上的热风加热时，开始产生一系列化学反应，150℃-250℃间反应相对快速和完全，超过250℃时有少量挥发份会逸出污染尾汽，而超过400℃时，有的褐煤在加热室内时间过长，由于水份大部丧失后的可能着火，安全性降低。
上述步骤一、二产生的低压过热气体还可以替代为低压过热蒸汽，所述低压过热蒸汽可通过锅炉17加压加热产生，产生的低压过热蒸汽应加压至0.1MPa以上，最好是在0.3MPa至0.5MPa之间，加温到105℃-400℃，最好是150℃-250℃之间。
步骤三，经换热器3加温后的热气或经锅炉17产生的低压过热蒸汽经多个支管4A分段喷入圆筒式加热器5的本体内，以加热投入圆筒式加热器5内的褐煤。原煤从进料管10进入圆筒式加热器5内，圆筒式加热器5的压力保持在0.1MPa以上，最好是0.3-0.5MPa，经第一物料推进器7往前推进，同时受到进气组合管4进入的热空气和热蒸汽的加热。受到加热的褐煤由表及里直接蒸发出部分水份，同时在正压环境中产生了一系列性质改变的反应，致使分子结构紧密，体积缩小，机械强度和热稳定性增加，亲水力、亲氧性降低且释放出一部分热量和二氧化碳，该部分热量间接蒸发出褐煤中的部分水份。褐煤在105℃，压强大于0.1MPa环境中内表及里开始产生这样的反应。在105℃-250℃范围内温度越高，反应越快速，超过250℃会引起挥发份逸出转变为干馏。产生反应时受到的压强越大，反应越完全，效果越好，但是对圆筒式加热器5、第一物料推进器和第一、二关门器9A、9B的要求越高，造价就越高。由于圆筒式加热器5内保持一定的正压，褐煤中直接蒸发和间接蒸发的水份大部冷凝，在煤颗粒表面释放出汽化热来提高褐煤自身的温度和圆筒式加热器5筒体内的温度。
圆筒式加热器5内设定的压力应保持在0.1MPa以上，最好是在0.3MPa至0.5MPa之间。但由于进气组合管4的进气和褐煤产生的部分蒸汽和二氧化碳，会致使圆筒式加热器5内的压力升高，当超过圆筒式加热器5内设定的压力时，三个设置在圆筒式加热器5上的排气阀6A、6B、6C会自动开启进行排气，排出的气体为低温气体，温度低于100℃，夹带着大量冷凝后因正压被雾化的水份，再对排出的气体进行下一步排放环保处理。
步骤四，如果进行加工的原煤主要为粒径大的块煤，则加热后的褐煤从圆筒式加热器5的落料管11排出后，冷凝在褐煤颗粒表面的水份会大部分自然蒸发，并用风机进行吹风，加强褐煤表面的空气流动，可以加速其水份蒸发，至煤温降低后即为成品。
如果进行加工的原煤主要为粒径低于6mm的粉煤，则加热后的褐煤从圆筒式加热器5的落料管11排出后，进入煤棒成型机12，由第二推进器16推进到呈锥状的出料端13，由于出料端13的出料口14管径缩小，粉煤受到挤压形成煤棒经出料口14排出。粉煤表面的冷凝水作为挤压成型的润滑剂，通过改变出料端13的长度和压缩比可以调整产量和强度的变化，制成的煤棒经冷却后会自然蒸发大部份水份，同时强度增加，基本消除粉末。
上述说明示出并描述了本发明的优选实施例，如前所述，应当理解本发明并非局限于本文所披露的形式，不应看作是对其他实施例的排除，而可用于各种其他组合、修改和环境，并能够在本文所述发明构想范围内，通过上述教导或相关领域的技术或知识进行改动。而本领域人员所进行的改动和变化不脱离本发明的精神和范围，则都应在本发明所附权利要求的保护范围内。

Claims (10)

  1. 一种褐煤干燥提质的装置，其特征在于：包括产生低压过热蒸汽或产生低压过热气体的装置，和一连接该装置的圆筒式加热器；所述产生低压过热蒸汽的装置包括一锅炉，所述产生低压过热气体的装置包括依序相接气体增压机、储气罐和换热器，圆筒式加热器通过一组进气组合管连接锅炉或换热器；所述的圆筒式加热器内设有第一物料推进器，且该圆筒式加热器上设有进料管、出料管及一个以上的排气阀，于所述的进料管和落料管上设有关风装置；所述的进气组合管包括有多个间隔设置的支管，所述支管连接在圆筒式加热器的本体上。
  2. 权利要求1所述的一种褐煤干燥提质的装置，其特征在于：还包括一煤棒成型机，该煤棒成型机具有一连接圆筒式加热器上的落料管的进料端，和一呈锥状的出料端，该锥状的出料端的窄口部为出料口； 所述煤棒成型机内设有第二物料推进器。
  3. 如权利要求1或2所述的一种褐煤干燥提质的装置，其特征在于：所述进气组合管还包括一连接多个支管的总管，该总管通过一中间管连接换热器，且相邻支管的间隔距离为10cm-30cm 。
  4. 如权利要求1或2所述的一种褐煤干燥提质的装置，其特征在于：所述排气阀设置在圆筒式加热器的本体上， 还设置在圆筒式加热器的落料管上。
  5. 一种褐煤干燥提质的方法，特征在于，其实施步骤是：向圆筒式加热器内分段喷入进入的低压过热气体或低压过热蒸汽，以加热投入圆筒式加热器内的褐煤，所述进入的低压过热气体或低压过热蒸汽的压力在0.1MPa以上、且温度在105℃-400℃之间；所述圆筒式加热器内的压力保持在0.1MPa以上，圆筒式加热器上设有的排气阀在圆筒式加热器内的压力大于进入的低压过热气体或低压过热蒸汽的压力时开启；加热后的褐煤从圆筒式加热器排出。
  6. 如权利要求5所述的一种褐煤干燥提质的方法，特征在于：从圆筒式加热器排出的褐煤用风机以加速其水份蒸发，制得成品。
  7. 如权利要求5所述的一种褐煤干燥提质的方法，特征在于：从圆筒式加热器排出的褐煤进入一煤棒成型机，并经煤棒成型机的锥状出料端挤压形成煤棒，制得成品。
  8. 如权利要求5、6或7所述的一种褐煤干燥提质的方法，特征在于：所述进入的低压过热气体或低压过热蒸汽加压至 0.3MPa-0.5MPa，且加温到150℃-250℃。
  9. 如权利要求5、6或7所述的一种褐煤干燥提质的方法，特征在于：所述圆筒式加热器内的压力保持在0.3-0.5MPa。
  10. 如权利要求8所述的一种褐煤干燥提质的方法，特征在于：所述圆筒式加热器内的压力保持在0.3-0.5MPa。
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