WO2015100708A1 - 一种干燥设备及干燥方法 - Google Patents

一种干燥设备及干燥方法 Download PDF

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Publication number
WO2015100708A1
WO2015100708A1 PCT/CN2014/001182 CN2014001182W WO2015100708A1 WO 2015100708 A1 WO2015100708 A1 WO 2015100708A1 CN 2014001182 W CN2014001182 W CN 2014001182W WO 2015100708 A1 WO2015100708 A1 WO 2015100708A1
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Prior art keywords
drying
bed section
moving bed
constant
fluidized
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PCT/CN2014/001182
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English (en)
French (fr)
Inventor
李胜
史勇春
蒋斌
梁国林
窦刚
贾世阳
万象明
高俊荣
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山东科院天力节能工程有限公司
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Priority claimed from CN201410004853.2A external-priority patent/CN104764296B/zh
Priority claimed from CN201410004887.1A external-priority patent/CN104764299B/zh
Priority claimed from AU2014202422A external-priority patent/AU2014202422A1/en
Application filed by 山东科院天力节能工程有限公司 filed Critical 山东科院天力节能工程有限公司
Publication of WO2015100708A1 publication Critical patent/WO2015100708A1/zh

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    • 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
    • F26B3/08—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 so as to loosen them, e.g. to form a fluidised bed
    • F26B3/084—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 so as to loosen them, e.g. to form a fluidised bed with heat exchange taking place in the fluidised bed, e.g. combined direct and indirect heat exchange
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K1/00—Preparation of lump or pulverulent fuel in readiness for delivery to combustion apparatus
    • 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

Definitions

  • the invention relates to a drying device and a drying method, in particular to a fluidized moving bed steam drying device and a drying method.
  • Conventional equipment and methods for drying high humidity materials employ: A) hot flue gas as a heat source to directly heat the material, or B) hot steam as a heat source to indirectly heat the material. Due to the high volatile content of the material or the influence of the inlet air temperature, the material with low ignition point (such as lignite) is easy to ignite and burn, and there is a safety hazard; the latter adopts indirect heating, the heat value of steam is high, and the process is safe and reliable. However, the latter needs to consume high calorific value fuels and has high economic costs.
  • the drying process is divided into two stages, namely, a constant-speed drying stage from the drying of the original moisture content to its critical moisture content and drying from its critical moisture content to the target moisture content of the product.
  • Slow down drying stage When the wet material adopts the technical scheme of CN101581533A in the constant-speed drying stage, the drying efficiency is higher; but in the slow-drying drying stage, since the drying rate mainly depends on the migration rate of moisture inside the material, if the technical scheme of CN101581533A is continued, due to the wet material The state of motion has little effect on the rate of dehydration.
  • the materials to be dried such as lignite are maintained in a "fluidized" state through higher energy consumption, resulting in a problem of high energy consumption per unit of production.
  • the object of the present invention is to overcome the deficiencies of the prior art described above, and to provide a drying apparatus and a drying method, which combines the characteristics of the drying process of most wet materials into a constant-speed drying and a slow-down drying stage, and adopts fluidized movement.
  • the bed dryer is divided into a constant-speed dry fluidized bed section and a reduced-speed dry moving bed section.
  • the constant-speed dry fluidized bed section wets the wet material to a critical moisture content in a fluidized form, and then slows down the moving bed section. Deeply dewatering wet materials to low moisture products in a more energy efficient manner.
  • the drying apparatus of the present invention is designed such that:
  • a drying apparatus comprising: a sequentially connected feeder, a fluidized moving bed dryer, a discharger, the fluidized moving bed dryer comprising a constant speed dry fluidized bed section and a reduced speed drying moving bed section,
  • the feeder is connected to the constant-speed dry fluidized bed section, the slow-moving dry moving bed section is connected to the unloader; the constant-speed dry fluidized bed section and the deceleration drying movement
  • At least one set of heat exchangers for heating the materials are respectively disposed in the bed section; a flow rate and pressure for adjusting the flow rate and pressure of the fluidizing gas are arranged between the constant-speed dry fluidized bed section and the deceleration drying moving bed section.
  • a gas distributor through which the fluidizing gas enters the constant velocity dry fluidized bed section.
  • the drying device is provided with at least a primary dust collector, the dust collector is connected to an upper portion of the drying device, and the waste heat steam generated by the constant-speed dry fluidized bed section and the reduced-speed dry moving bed section is After the dust collector is dedusted, a part of the waste heat steam is returned to the gas distributor through a circulating pressurizing device, and a part of the waste heat is taken out of the system.
  • the dust remover is one or more of a series combination of a cyclone, a baghouse, an electrostatic precipitator, and a wet scrubber.
  • a material looser for loosening the material in the bed is provided between the deceleration drying moving bed section and the unloader, and the material looser makes saturated or superheated steam or nitrogen or other inert gas.
  • the low-speed drying moving bed section is entered by means of pulsed air inflow, and the material layer in the moving bed section is moved from bottom to top through the dryer to play the role of loosening the material in the moving bed section of the dryer.
  • the heat exchanger provides a heat source from saturated or superheated steam, and the heat exchanger is connected to the boiler feed water system or its equipment. After the heat exchange, the condensed water generated in the heat exchanger flows to the boiler feed water system. Or use it according to the process requirements.
  • the feeder is disposed at an upper portion of the drying device, the reduced-speed drying moving bed segment is disposed under the constant-speed dry fluidized bed section, and the unloader is disposed at a bottom of the drying device
  • the material to be dried is moved from top to bottom by gravity.
  • the moisture content of the wet material after drying in the constant-speed dry fluidized bed section has a certain upper or lower offset of its critical water content or its critical water content, and the offset range is 20% of its critical moisture content.
  • the lower portion of the reduced-speed drying moving bed section is provided with a pipeline through saturated or superheated steam or nitrogen or wet material moisture or inert gas for system shutdown, emergency treatment or fluidization adjustment. Move the internal temperature of the bed dryer.
  • the drying method of the present invention comprises the following steps:
  • Step A the wet material to be dried enters the fluidized moving bed dryer through the feeder;
  • Step B feeding the steam heat source into the heat exchanger in the constant-speed dry fluidized bed section of the fluidized moving bed dryer, and the heat exchanger in the slow-moving moving bed section;
  • step C the fluidized gas is sent into the fluidized moving bed dryer, and the wet material particles are in a fluidized state and indirect heat exchange with the steam in the heat exchanger in the constant-speed drying fluidized bed section, and the wet material is controlled.
  • Step D the wet material particles entering the reduced-speed drying moving bed section continue to exchange heat with the steam in the heat exchanger, and are dried to the product satisfying the required moisture;
  • step E the product is discharged from the drying device by the unloader.
  • the steam fed to the heat exchanger in the constant-speed dry fluidized bed section in the step B is 0.01-10 MPa (G) of saturated or superheated steam, and is sent to the reduced-speed dry moving bed section.
  • the steam of the heat exchanger is 0.01-10 MPa (G) of saturated or superheated steam.
  • the pulsed gas in the step D first passes through the material looser, so that saturated or superheated steam or nitrogen or other inert gas enters the slow-moving and moving moving bed section by pulsed air inlet. Loose material helps the material fall.
  • step C the frequency of the frequency converter of the circulating pressurizing device is adjusted or the valve on the air outlet of the circulating pressurizing device is adjusted to control the amount of circulating fluidizing gas entering the constant-speed dry fluidized bed section. Ensure that the material in the constant-speed dry fluidized bed section is stable Fluidization.
  • the whole superheated steam drying process is an oxygen-free environment, safe and reliable, continuous operation, and can be seamlessly connected with the supporting process of the original power plant.
  • Figure 1 is a schematic view of the structure of the present invention.
  • the drying apparatus 1 of the present invention comprises: a sequentially connected feeder 10, a fluidized moving bed dryer 12, and a discharger 14.
  • the feeder 10 is disposed at an upper portion of the drying apparatus 1, and the unloader 14 is disposed at the bottom of the drying apparatus 1 to facilitate movement of the material to be dried from top to bottom by gravity.
  • the fluidized moving bed dryer 12 includes a constant speed dry fluidized bed section 120 and a reduced speed dry moving bed section 122, and the reduced speed dry moving bed section 122 is disposed below the constant speed dry fluidized bed section 120.
  • the feeder 10 is connected to the constant-speed dry fluidized bed section 120, and the slow-drying moving moving bed section 122 is connected to the unloader 14.
  • At least one set of heat exchangers 124 for heating the materials is disposed in the constant-speed dry fluidized bed section 120 and the reduced-speed dry moving bed section 122, respectively.
  • the heat exchanger 124 is provided with a heat source by steam, and the branch connecting the heat source inlet of each set of heat exchangers can determine whether there is a device for adjusting parameters such as steam flow, pressure or temperature according to design requirements, and the heat exchanger 124 and The boiler feed water system of the drying equipment 1 is connected to it or connected by equipment. After heat exchange, the condensed water generated in the heat exchanger 124 flows to the boiler feed water system or according to the process requirements, and the branches or branches of the condensed water generated by each group of the heat exchangers 124 are discharged.
  • the main pipe can be arbitrarily set according to the design requirements, such as a trap group.
  • the drying device further includes a dust remover 11, a circulating pressurizing device 13, and an air guiding device 15.
  • a dust remover 11 can be one level or multiple stages.
  • the upper portion of the fluidized moving bed dryer 12 is connected to a dust remover 11 (preferably a first stage dust remover), and the dust remover 11 (preferably a final stage dust remover) is also connected to the circulating pressurizing device 13 and the air introducing device 15, respectively.
  • the waste heat steam generated by the constant-speed dry fluidized bed section 120 and the reduced-speed dry moving bed section 122 is dusted by the dust remover 11, and a part is returned to the gas distributor 1200 through the circulating pressurizing device 13, and a part of the waste heat is returned to the gas distributor 1200.
  • the wind unit 15 leads to the system.
  • the dust remover 11 may be one or a combination of one or more of a cyclone, a baghouse, an electrostatic precipitator, and a wet scrubber.
  • a material loosening device 1220 for loosening the material in the bed is provided between the deceleration drying moving bed section 122 and the unloader 14, and the material loosening device 1220 makes saturated or superheated steam or nitrogen or other
  • the inert gas enters the deceleration drying moving bed section 122 in a pulsed air inlet manner, and passes through the material layer in the deceleration drying moving bed section 122 from bottom to top to loosen the deceleration drying moving bed.
  • the role of the material in segment 122 is the role of the material in segment 122.
  • a lower portion of the reduced-speed drying moving bed section is provided with a pipeline 1221 that is saturated or superheated with steam or nitrogen or wet material moisture or inert gas for system shutdown, emergency processing or adjustment of fluidized movement.
  • Bed dryer internal temperature is saturated or superheated with steam or nitrogen or wet material moisture or inert gas for system shutdown, emergency processing or adjustment of fluidized movement.
  • the drying method of the present invention is:
  • the drying method of the present invention divides the fluidized moving bed dryer 12 into different bed sections by controlling the residence time of the wet material in different bed sections (the wet material is dried in a constant speed dry fluidized bed section 120 close to critical)
  • the amount of water if it happens to be its critical water content or up and down within 20% of its critical moisture content, then enters the deceleration drying moving bed section 122 to continue drying), and the product that is finally dried to acceptable moisture is discharged through the unloader 14 Equipment 1, the moisture of the wet material removed in the process is in the form of waste heat steam, which is discharged from the upper part of the drying equipment 1 in the state of superheated steam, and is divided into two paths after dust removal, one way is taken out by the air guiding device 15, and the other is cyclically pressurized.
  • the device 13 returns to the gas distributor 1200 of the constant velocity dry fluidized bed section 120.
  • the waste heat steam will mainly enter the wet material flow state in the constant-speed dry fluidized bed section 120 as a fluidizing gas.
  • the wet material is indirectly exchanged with the steam in the heat exchanger 124 of the constant-speed drying fluidized bed section 120, and the wet time is controlled by controlling the residence time of the wet material in the fluidized bed section of the dryer. It is dried close to the critical moisture content, such as just within its critical water content or up and down within 20% of its critical moisture content, and then enters the reduced speed drying moving bed section 122 to continue drying.
  • the control enters the constant-speed dry fluidized bed.
  • the amount of waste heat steam in section 120 is such that the amount of waste heat steam is always maintained within the fluidized bed operating range, thereby ensuring that the material in the constant-speed dry fluidized bed section 120 maintains a stable fluidization; entering the reduced-speed drying moving bed section 122
  • the wet material therein continues to indirectly exchange heat with the steam in the bed-integrated heat exchanger 124, and is finally discharged to the bottom of the drying apparatus 1 by the unloader 14 after being dried to the qualified moisture required by the product.
  • saturated or superheated steam or nitrogen or wet material moisture or inert gas is introduced into the pipeline 1221 provided in the lower part of the slow-moving moving moving bed section for system shutdown, emergency treatment or adjustment.
  • Fluidized moving bed dryer internal temperature is introduced into the pipeline 1221 provided in the lower part of the slow-moving moving moving bed section for system shutdown, emergency treatment or adjustment.
  • the material loosening device is used to loosen the material in the bed of the reduced-speed drying moving bed segment 122, which will be saturated or overheated.
  • the steam or nitrogen or other inert gas passes through the material loosener 1220, it enters the slow-drying moving moving bed section 122 by pulsed air, and passes through the material of the slow-moving moving moving bed section 122 from bottom to top, pulse gas.
  • it mainly serves to loosen and slow down the material in the moving bed section 122 and take away the moisture.
  • the lignite raw coal containing 30%-60% of water is crushed and sieved to form lignite particles having a particle diameter of less than 6 mm, and the lignite particles are fed into the feeder 10 and then sent to the fluidized moving bed dryer 12 through the feeder 10.
  • a 0.01-10 MPa (G) saturated or superheated steam heat source is fed into the heat exchanger 124 in the constant-speed dry fluidized bed section 120, and a 0.01-10 MPa (G) saturated or superheated steam heat source is sent to the reduced speed drying.
  • the heat exchanger 124 of the moving bed section 122, the branch connecting the steam inlet of each set of heat exchangers 124 can be determined according to design requirements whether there is a device for adjusting parameters such as steam flow, pressure or temperature, and the heat exchanger 124 and the drying device 1 External boiler feed water system or it is connected by equipment. After heat exchange, the condensed water generated in the heat exchanger 124 flows to the boiler feed water system or According to the process requirements, the branches of the condensed water generated by each group of heat exchangers 124 or the manifolds of the branches can be arbitrarily set according to design requirements, such as a trap group.
  • Waste heat steam from the circulating pressurizing device 13 in a superheated steam state is passed into a gas distributor 1200 between the constant-speed dry fluidized bed section 120 and the decelerating dry moving bed section 122, the waste heat steam being provided
  • the constant velocity dry fluidized bed section 120 which primarily enters the fluidized moving bed dryer 12 as a fluidizing medium, maintains fluidization of the wet material entering the constant velocity dry fluidized bed section.
  • the wet lignite particles in the constant-speed dry fluidized bed section 120 are indirectly exchanged with the steam in the heat exchanger 124 in a fluidized state by controlling the wet lignite particles in the constant-speed dry fluidized bed section 120.
  • the wet material is dried close to the critical water content.
  • the wet lignite particles can be just placed in the constant-speed dry fluidized bed section 120.
  • saturated or superheated steam or nitrogen or wet material moisture or inert gas is introduced into the pipeline 1221 provided in the lower portion of the slow-moving moving moving bed section 122 for system shutdown, emergency treatment or
  • the internal temperature of the fluidized moving bed dryer 12 is adjusted, such as when the wet lignite particles are fed into the fluidized moving bed dryer 12 through the feeder 10 at the initial start of the system, to the fluidized moving bed dryer 12 via line 1221.
  • the internal air in the fluidized moving bed dryer 12 is displaced into the system by passing saturated or superheated steam or nitrogen or an inert gas to obtain an oxygen-free drying environment to prevent the lignite particles fed into the fluidized moving bed dryer 12.
  • the material-dissolving moving bed section 122 is provided with a material loosening device 1220, saturated or superheated steam or nitrogen or other inert gas.
  • the steam formed by the fluidized gas, the loose gas, and the moisture removed by the lignite particles together form waste heat steam, which is discharged from the upper portion of the drying device 1 in a superheated steam state, and is removed by the dust remover 11 and then passed through the circulating pressurizing device 13
  • the other path is led out of the system via the air guiding means 15.
  • the steam in the heat exchanger 124 built in the drying device 1 is condensed water generated by indirect heat exchange to the boiler feed water system or used according to the process requirements.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
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Abstract

一种干燥设备（1）和使用该设备干燥物料的方法。干燥设备（1）包括顺序相连的进料器（10）、流化移动床干燥器（12）和卸料器（14）。流化移动床干燥器（12）包括恒速干燥流化床段（120）和降速干燥移动床段（122）。进料器（10）与恒速干燥流化床段（120）相连，降速干燥移动床段（122）与卸料器（14）相连；恒速干燥流化床段（120）内和降速干燥移动床段（122）内分别设有至少一组用于加热物料的换热器（124）；恒速干燥流化床段（120）和降速干燥移动床段（122）之间设有一用于调节流化气体流速、压力的气体分布器（1200），流化气体通过气体分布器（1200）进入恒速干燥流化床段（120）。

Description

一种干燥设备及干燥方法 技术领域
本发明涉及一种干燥设备及干燥方法，尤其是一种流化移动床蒸汽干燥设备及干燥方法。
背景技术
工业生产中，有很多种类高湿物料需要干燥至较低水分含量，以褐煤为例，无论是燃烧、运输或者是为满足煤化工工艺要求，都经常需要将原始水分为30％-60％的褐煤干燥至终水分为3％-5％的褐煤产品。
常规的干燥高湿物料的设备和方法是采用：A)热烟气作为热源直接加热物料，或B)热蒸汽作为热源间接加热物料。前者由于受物料挥发份高，或受进风温度的影响，对于燃点低的物料(例如褐煤)容易起火燃烧，存在安全隐患；后者采用间接加热，蒸汽的热值高，工艺安全可靠。但是后者需要消耗高热值的燃料，经济成本高。
但是，由于大多数湿物料，如褐煤等，其干燥过程分为两个阶段，即由原始水分含量干燥到其临界含水量的恒速干燥阶段和由其临界含水量干燥至产品目标水分含量的降速干燥阶段。湿物料在恒速干燥阶段采用CN101581533A的技术方案时干燥效率较高；但在降速干燥阶段，由于干燥速率主要取决于水分在物料内部的迁移速率，如果继续CN101581533A的技术方案，由于湿物料的运动状态对其脱水速率影响不大，同时还要将褐煤这类待干燥的物料通过较高能耗维持在“流态化”的状态之下，造成生产单位产品能耗较高的问题。
因此，从干燥方法的安全性、经济性和高效性角度来看，实有必要针对如褐煤这类湿物料的干燥特性规律设计一种新的干燥设备和干燥方法，实现湿物料在恒速干燥阶段的高效快速除水，和在降速干燥阶段的低能耗深度脱水，来降低生产单位产品的能量消耗。
发明内容
本发明的目的是为克服上述现有技术的不足，提供一种干燥设备和干燥方法，结合了大多数湿物料的干燥过程分为恒速干燥和降速干燥阶段的特点，采用的流化移动床干燥器分为恒速干燥流化床段和降速干燥移动床段，恒速干燥流化床段以流态化的形式将湿物料干燥接近至临界含水量后，降速干燥移动床段以较为节能的方式继续将湿物料深度脱水至低水分产品。
为实现上述目的，本发明的干燥设备是这样设计的：
一种干燥设备，其包括：顺序相连的进料器、流化移动床干燥器、卸料器，所述流化移动床干燥器包括恒速干燥流化床段和降速干燥移动床段，所述进料器与所述恒速干燥流化床段相连，所述降速干燥移动床段与所述卸料器相连；所述恒速干燥流化床段内和所述降速干燥移动床段内分别设有至少一组用于加热物料的换热器；所述恒速干燥流化床段和所述降速干燥移动床段之间设有一用于调节流化气体流速、压力的气体分布器，流化气体通过所述气体分布器进入所述恒速干燥流化床段。
作为优选实施方式，所述干燥设备设有至少一级除尘器，所述除尘器与干燥设备上部相连，所述恒速干燥流化床段及降速干燥移动床段产生的废热蒸汽经所述除尘器除尘后，一部分废热蒸汽通过循环加压装置返至所述气体分布器，一部分引出***。
作为优选实施方式，所述除尘器为旋风除尘器、布袋除尘器、静电除尘器和湿式除尘器中的一种或多种串联组合。
作为优选实施方式，所述降速干燥移动床段和所述卸料器之间设有一用于疏松床内物料的物料疏松器，所述物料疏松器使得饱和或过热蒸汽或氮气或其它惰性气体以脉冲进风的方式进入所述降速干燥移动床段，并自下而上穿过干燥机移动床段内的物料层，起到疏松干燥机移动床段内物料的作用。
作为优选实施方式，所述换热器由饱和或过热蒸汽提供热源，所述换热器与锅炉给水***或它用设备相连，经过换热后，换热器内生成的冷凝水流至锅炉给水***或根据工艺要求它用。
作为优选实施方式，所述进料器设置在干燥装置的上部，所述降速干燥移动床段设置在所述恒速干燥流化床段之下，所述卸料器设置在干燥装置的底部，便于待干燥的物料借助重力从上向下移动。
作为优选实施方式，经所述恒速干燥流化床段干燥后的湿物料含水量为其临界含水量或与其临界含水量存在一定的上下偏移，偏移范围在其临界含水量的20％以内。
作为优选实施方式，所述降速干燥移动床段下部设有通饱和或过热蒸汽或氮气或湿物料湿分气体或惰性气体的管路，用于***开停车、紧急工况处理或调节流化移动床干燥器内部温度。
本发明的干燥方法包括如下步骤：
步骤A，待干燥的湿物料通过进料器进入流化移动床干燥器；
步骤B，将蒸汽热源送进流化移动床干燥器的恒速干燥流化床段内的换热器，以及降速干燥移动床段内的换热器；
步骤C，将流化气体送入流化移动床干燥器内，湿物料颗粒在流态化状态下与恒速干燥流化床段内的换热器中的蒸汽实现间接换热，控制湿物料颗粒在恒速干燥流化床段内的停留时间，当湿物料被干燥接近至临界含水量时，进入所述降速干燥移动床段继续干燥；
步骤D，进入降速干燥移动床段内的湿物料颗粒继续与换热器中的蒸汽间接换热，被干燥至符合要求水分的产品；
步骤E，将产品由卸料器排出干燥设备。
本领域技术人员可以理解，所述步骤B中送入恒速干燥流化床段内的换热器的蒸汽是0.01-10MPa(G)的饱和或过热蒸汽，送入降速干燥移动床段内的换热器的蒸汽是0.01-10MPa(G)的饱和或过热蒸汽。
本领域技术人员可以理解，所述步骤D中的脉冲气体先通过物料疏松器，使得饱和或过热蒸汽或氮气或其他惰性气体以脉冲进风的方式进入所述降速干燥移动床段，起到疏松物料帮助物料下落的作用。
本领域技术人员可以理解，所述步骤C中调节循环加压装置的变频器频率或者调节循环加压装置出风管路上的阀门，控制进入恒速干燥流化床段的循环流化气体量，保证恒速干燥流化床段内的物料维持稳定的 流态化。
本发明的干燥设备和干燥方法的有益效果在于：
1)干燥设备分为恒速干燥床段和降速干燥床段后，与单纯的内加热流化床干燥机相比，单机处理量更大，动力功耗更低，节能效果显著。
2)整个过热蒸汽干燥过程为无氧环境，安全可靠，连续操作，可与原有电厂的配套工艺无缝连接。
附图说明
图1是本发明的结构示意图。
具体实施方式
下面结合附图和实施例对本发明进一步说明。
请参见图1，本发明的干燥设备1包括：顺序相连的进料器10、流化移动床干燥器12、卸料器14。所述进料器10设置在干燥设备1的上部，所述卸料器14设置在干燥设备1的底部，便于待干燥的物料借助重力从上向下移动。
所述流化移动床干燥器12包括恒速干燥流化床段120和降速干燥移动床段122，所述降速干燥移动床段122设置在所述恒速干燥流化床段120之下，所述进料器10与所述恒速干燥流化床段120相连，所述降速干燥移动床段122与所述卸料器14相连。
所述恒速干燥流化床段120内和所述降速干燥移动床段122内分别设有至少一组用于加热物料的换热器124。所述换热器124由蒸汽提供热源，连接每组换热器热源入口的支路上可根据设计要求确定是否带有调节蒸汽流量、压力或温度等参数的装置，并且所述换热器124与干燥设备1外接的锅炉给水***或它用设备相连。经过换热后，所述换热器124内生成的冷凝水流至锅炉给水***或根据工艺要求它用，排出每组所述换热器124生成的冷凝水的各支路上或各支路汇聚的总管上可根据设计要求任意设置如疏水阀组等装置。
所述恒速干燥流化床段120和所述降速干燥移动床段122之间设有 一用于调节流化气体流速、压力的气体分布器1200，流化气体通过所述气体分布器1200进入所述恒速干燥流化床段120。
优选地，干燥设备还包括除尘器11、循环加压装置13、引风装置15。本领域技术人员可以理解，所述除尘器11可以是一级也可以是多级。流化移动床干燥器12的上部与除尘器11(优选为第一级除尘器)相连，除尘器11(优选为末级除尘器)还分别与循环加压装置13和引风装置15相连。所述恒速干燥流化床段120及降速干燥移动床段122产生的废热蒸汽经所述除尘器11除尘后，一部分通过循环加压装置13返至所述气体分布器1200，一部分通过引风装置15引出***。所述除尘器11可以为旋风除尘器、布袋除尘器、静电除尘器和湿式除尘器中的一种或多种串联组合。
优选地，所述降速干燥移动床段122和所述卸料器14之间设有一用于疏松床内物料的物料疏松器1220，所述物料疏松器1220使得饱和或过热蒸汽或氮气或其他惰性气体以脉冲进风的方式进入所述降速干燥移动床段122，并自下而上穿过所述降速干燥移动床段122内的物料层，起到疏松所述降速干燥移动床段122内物料的作用。
优选地，所述降速干燥移动床段下部设有通饱和或过热蒸汽或氮气或湿物料湿分气体或惰性气体的管路1221，用于***开停车、紧急工况处理或调节流化移动床干燥器内部温度。
本发明的干燥方法为：
本发明的干燥方法将流化移动床干燥器12分为不同的床段，通过控制湿物料在不同床段内的停留时间(湿物料在恒速干燥流化床段120被干燥接近至临界含水量，如恰好是其临界含水量或上下偏移其临界含水量20％范围以内，然后进入降速干燥移动床段122继续干燥)，最终被干燥至合格水分的产品经卸料器14排出干燥设备1，过程中脱除的湿物料水分以废热蒸汽的形式，呈过热蒸汽状态由干燥设备1上部排出，经除尘后分成两路，一路经引风装置15引出***，另一路经循环加压装置13返至恒速干燥流化床段120的气体分布器1200。废热蒸汽除提供少量热量外，主要作为流化气体将进入恒速干燥流化床段120内的湿物料流态 化，湿物料在流态化状态下与恒速干燥流化床段120内置换热器124中的蒸汽实现间接换热，通过控制湿物料在干燥器流化床段内的停留时间，湿物料被干燥接近至临界含水量，如恰好是其临界含水量或上下偏移其临界含水量20％范围以内，然后进入降速干燥移动床段122继续干燥。在此过程中，通过调节循环加压装置13的变频器频率(当循环加压装置不配带变频器时，可调节加压装置出风管路上的阀门)，来控制进入恒速干燥流化床段120的废热蒸汽量，使该废热蒸汽量始终保持在流化床操作范围内，从而保证恒速干燥流化床段120内的物料维持稳定的流态化；进入降速干燥移动床段122内的湿物料继续与该床段内置换热器124中的蒸汽实现间接换热，最终被干燥至产品要求的合格水分后，由卸料器14从干燥设备1的底部排出。
在此过程中，向降速干燥移动床段下部设有的管路1221中通入饱和或过热蒸汽或氮气或湿物料湿分气体或惰性气体，用于***开停车、紧急工况处理或调节流化移动床干燥器内部温度。
在此过程中，当干燥设备处理的物料不利于在降速干燥移动床段122内移动落料时，采用物料疏松器对降速干燥移动床段122床层内物料进行疏松，将饱和或过热蒸汽或氮气或其它惰性气体通过物料疏松器1220均风后，以脉冲进风的方式进入降速干燥移动床段122，自下而上穿过降速干燥移动床段122内的物料，脉冲气体除提供少量热量外，主要起到疏松降速干燥移动床段122内物料，并带走湿气的作用。
以下是待干燥物料选取褐煤的实施例：
含水30％-60％的褐煤原煤经破碎、筛分后形成粒径小于6mm的褐煤颗粒，褐煤颗粒被送入进料器10内，然后通过进料器10送入流化移动床干燥器12内；将0.01-10MPa(G)的饱和或过热蒸汽热源送进恒速干燥流化床段120内的换热器124，将0.01-10MPa(G)的饱和或过热蒸汽热源送入降速干燥移动床段122的换热器124，连接每组换热器124蒸汽入口的支路上可根据设计要求确定是否带有调节蒸汽流量、压力或温度等参数的装置，并且换热器124与干燥设备1外接的锅炉给水***或它用设备相连。经过换热后，换热器124内生成的冷凝水流至锅炉给水***或 根据工艺要求它用，排出每组换热器124生成的冷凝水的各支路上或各支路汇聚的总管上可根据设计要求任意设置如疏水阀组等装置。来自循环加压装置13的呈过热蒸汽状态的废热蒸汽通入所述恒速干燥流化床段120和所述降速干燥移动床段122之间的气体分布器1200，所述废热蒸汽除提供少量热量外，主要作为流化介质进入流化移动床干燥器12的所述恒速干燥流化床段120，将进入恒速干燥流化床段内的湿物料维持流态化。所述恒速干燥流化床段120内的湿褐煤颗粒在流态化状态下与换热器124中的蒸汽实现间接换热，通过控制湿褐煤颗粒在恒速干燥流化床段120内的停留时间，湿物料被干燥接近至临界含水量，如对于临界含水量为水分重量占比12％-15％左右的不同类型褐煤，可以在恒速干燥流化床段120内恰好将湿褐煤颗粒由初始水分含量干燥至其临界含水量即水分重量占比12％-15％左右，或干燥至上下偏移其临界含水量20％范围以内，即水分重量占比9％-18％左右，然后进入所述降速干燥移动床段122继续干燥，在此过程中，通过调节循环加压装置13的变频器频率(当循环加压装置13不配带变频器时，可调节循环加压装置13出风管路上的阀门)，来控制进入恒速干燥流化床段120的废热蒸汽量，从而保证恒速干燥流化床段120内的物料维持稳定的流态化；进入降速干燥移动床段122内的褐煤颗粒继续与换热器124中的蒸汽实现间接换热，最终被干燥至符合工艺要求的水分重量占比如3％-5％的合格褐煤产品，然后由卸料器14排出干燥设备。在此过程中，向降速干燥移动床段122下部设有的管路1221中通入饱和或过热蒸汽或氮气或湿物料湿分气体或惰性气体，用于***开停车、紧急工况处理或调节流化移动床干燥器12内部温度，如在***初始开车时，在湿褐煤颗粒通过进料器10送入流化移动床干燥器12之前，先经管路1221向流化移动床干燥器12中通入饱和或过热蒸汽或氮气或惰性气体，将流化移动床干燥器12中内部的空气置换出***，来得到无氧干燥环境以防止送入流化移动床干燥器12中的褐煤颗粒发生自燃或***或发生化学反应；或在***停车、紧急工况处理时，经管路1221通入饱和或过热蒸汽或氮气或惰性气体来维持流化移动床干燥器12内部的无氧环境，以防止流化移动床干燥器12中的褐煤颗粒发生自燃或 ***或发生化学反应，或根据工艺需求来调节流化移动床干燥器12内部温度，以避免干燥一些热敏性物料时在干燥过程中发生物料分解或变性等。在此过程中，为使褐煤颗粒在降速干燥移动床段122内移动落料顺畅，所述降速干燥移动床段122内设有物料疏松器1220，饱和或过热蒸汽或氮气或其它惰性气体经所述物料疏松器以脉冲进风的方式进入降速干燥移动床段122内，饱和或过热蒸汽或氮气或其它惰性气体自下而上穿过所述降速干燥移动床段122内的物料，除提供少量热量外，主要起到疏松所述降速干燥移动床段122内物料，并带走湿气的作用。
流化气体、疏松气体、褐煤颗粒脱除的水分形成的蒸汽共同形成废热蒸汽，该废热蒸汽呈过热蒸汽状态由干燥设备1的上部排出，经除尘器11除尘后，一路经循环加压装置13返至恒速干燥流化床段120的气体分布器1200，另一路经引风装置15引出***。干燥设备1内置的换热器124中的蒸汽经间接换热生成的冷凝水去锅炉给水***或根据工艺要求它用。
上述虽然结合附图对本发明的具体实施方式进行了描述，但并非对本发明保护范围的限制，所属领域技术人员应该明白，在本发明的技术方案的基础上，本领域技术人员不需要付出创造性劳动即可做出的各种修改或变形仍在本发明的保护范围以内。

Claims (12)

  1. 一种干燥设备，其包括：顺序相连的进料器、流化移动床干燥器、卸料器，其特征在于：
    所述流化移动床干燥器包括恒速干燥流化床段和降速干燥移动床段，所述进料器与所述恒速干燥流化床段相连，所述降速干燥移动床段与所述卸料器相连；
    所述恒速干燥流化床段内和所述降速干燥移动床段内分别设有至少一组用于加热物料的换热器；
    所述恒速干燥流化床段和所述降速干燥移动床段之间设有一用于调节流化气体流速和压力的气体分布器，流化气体通过所述气体分布器进入所述恒速干燥流化床段。
  2. 如权利要求1所述的干燥设备，其特征在于：所述干燥设备设有至少一级除尘器，所述除尘器与干燥设备上部相连，所述恒速干燥流化床段及降速干燥移动床段产生的废热蒸汽经所述除尘器除尘后，一部分废热蒸汽通过循环加压装置返至所述气体分布器，一部分引出***。
  3. 如权利要求2所述的干燥设备，其特征在于，所述除尘器为旋风除尘器、布袋除尘器、静电除尘器和湿式除尘器中的一种或多种串联组合。
  4. 如权利要求1-3任意一项所述的干燥设备，其特征在于，所述降速干燥移动床段和所述卸料器之间设有一用于疏松床内物料的物料疏松器，所述物料疏松器使得饱和或过热蒸汽或氮气或其它惰性气体以脉冲进风的方式进入所述降速干燥移动床段，并自下而上穿过干燥机移动床段内的物料层，起到疏松干燥机内物料的作用。
  5. 如权利要求1所述的干燥设备，其特征在于，所述换热器由饱和或过热蒸汽提供热源，所述换热器与锅炉给水***或它用设备相连，经过换热后，换热器内生成的冷凝水流至锅炉给水***或根据工艺要求它用。
  6. 如权利要求1所述的干燥设备，其特征在于：所述进料器设置在干燥装置的上部，所述降速干燥移动床段设置在所述恒速干燥流化床段之下，所述卸料器设置在干燥装置的底部，便于待干燥的物料借助重力从上向下移动。
  7. 如权利要求1所述的干燥设备，其特征在于：经所述恒速干燥流化床段干燥后的湿物料含水量为其临界含水量或与其临界含水量存在一定的上下偏移，偏移范围在其临界含水量的20％以内。
  8. 如权利要求1所述的干燥设备，其特征在于：所述降速干燥移动床段下部设有通饱和或过热蒸汽或氮气或湿物料湿分气体或惰性气体的管路，用于***开停车、紧急工况处理或调节流化移动床干燥器内部温度。
  9. 一种干燥方法，其包括如下步骤：
    步骤A，待干燥的湿物料通过进料器进入流化移动床干燥器；
    步骤B，将蒸汽热源送进流化移动床干燥器的恒速干燥流化床段内的换热器，以及降速干燥移动床段内的换热器；
    步骤C，将流化气体送入流化移动床干燥器内，湿物料颗粒在流态化状态下与恒速干燥流化床段内的换热器中的蒸汽实现间接换热，控制湿物料颗粒在恒速干燥流化床段内的停留时间，当湿物料被干燥接近至临界含水量时，进入所述降速干燥移动床段继续干燥；
    步骤D，进入降速干燥移动床段内的湿物料颗粒继续与换热器中的蒸汽间接换热，被干燥至符合要求水分的产品；
    步骤E，将产品由卸料器排出干燥设备。
  10. 根据权利要求9所述的干燥方法，其特征在于：所述步骤B中送入恒速干燥流化床段内的换热器的蒸汽是0.01-10MPa(G)的饱和或过热蒸汽，送入降速干燥移动床段内的换热器的蒸汽是0.01-10MPa(G)的饱和或过热蒸汽。
  11. 根据权利要求9所述的干燥方法，其特征在于：所述步骤D中的饱和或过热蒸汽或氮气或其它惰性气体先通过物料疏松器，使得疏松 气体以脉冲进风的方式进入所述降速干燥移动床段，起到疏松物料帮助物料下落的作用。
  12. 根据权利要求9所述的干燥方法，其特征在于：所述步骤C中调节循环加压装置的变频器频率或者调节循环加压装置出风管路上的阀门，控制进入恒速干燥流化床段的循环流化气体量，保证恒速干燥流化床段内的物料维持稳定的流态化。
PCT/CN2014/001182 2014-01-06 2014-12-26 一种干燥设备及干燥方法 WO2015100708A1 (zh)

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