WO2020199818A1 - 一种利用分选密度梯度的气固流化床干法分选工艺 - Google Patents

一种利用分选密度梯度的气固流化床干法分选工艺 Download PDF

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WO2020199818A1
WO2020199818A1 PCT/CN2020/077335 CN2020077335W WO2020199818A1 WO 2020199818 A1 WO2020199818 A1 WO 2020199818A1 CN 2020077335 W CN2020077335 W CN 2020077335W WO 2020199818 A1 WO2020199818 A1 WO 2020199818A1
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density
separation
gas
fine particles
fluidized bed
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PCT/CN2020/077335
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English (en)
French (fr)
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赵跃民
祝京旭
周晨阳
付芝杰
骆振福
段晨龙
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中国矿业大学
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Priority to US17/598,890 priority Critical patent/US11484913B2/en
Publication of WO2020199818A1 publication Critical patent/WO2020199818A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B4/00—Separating solids from solids by subjecting their mixture to gas currents
    • B07B4/08—Separating solids from solids by subjecting their mixture to gas currents while the mixtures are supported by sieves, screens, or like mechanical elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B7/00—Selective separation of solid materials carried by, or dispersed in, gas currents
    • B07B7/01—Selective separation of solid materials carried by, or dispersed in, gas currents using gravity
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B11/00—Arrangement of accessories in apparatus for separating solids from solids using gas currents
    • B07B11/02—Arrangement of air or material conditioning accessories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B11/00—Arrangement of accessories in apparatus for separating solids from solids using gas currents
    • B07B11/04—Control arrangements

Definitions

  • the invention relates to a mineral processing method, belonging to the technical field of dry beneficiation, in particular to a gas-solid fluidized bed dry separation process using a separation density gradient.
  • Coal is one of the most important basic energy sources in the world, and has a significant role in promoting the development of the world economy.
  • the huge consumption and output of coal have brought severe challenges to the living environment and ecological security of the people.
  • Environmental problems such as "smog” and “acid rain” have aroused widespread concern from the government and the people.
  • Coal preparation is the basis of clean coal utilization and plays an important role in improving the quality of coal products and the pre-treatment and upgrading of coal before combustion.
  • the gas-solid fluidized bed dry separation technology has attracted the attention of scholars from China, Canada, Japan, India, Australia and other countries.
  • the gas-solid fluidized bed dry separation technology mainly uses magnetite minerals as the heavier substance, which forms a fluid with a certain density under the action of airflow, and separates the minerals to be selected according to the density to form light products and heavy products. It has a simple process , The advantages of high sorting accuracy provide an important way for the processing and utilization of coal sorting.
  • the traditional gas-solid fluidized bed sorting machine uses two kinds of particles with similar aerodynamic diameters to mix to adjust the sorting density, and a single sorting density is formed in the sorting system. Due to the complex density composition of the minerals to be selected, minerals close to the sorting density are prone to mismatching, which reduces the sorting efficiency and reduces the quality of the product.
  • Chinese invention patent application CN1161884 discloses a method and device for separating three products with a double-density layer air-dense-medium fluidized bed, which is mainly used to achieve the purpose of producing three different minerals, but it is not difficult to find that low density and
  • the adjustment of high density mainly depends on selecting the density and size of the particles, without considering the use of the bulk expansion characteristics of the particles to optimize the adjustment of the sorting density;
  • the fluidized bed used in the sorting is a conical inclined surface design with an inclination angle of 60° ⁇ 80° , It will increase the possibility of forming a spouted bed, which is not conducive to the sorting of minerals;
  • the sorting density is mainly divided into a high-density sorting area formed by heavy and large particles and a low-density sorting area formed by light and small particles.
  • the density gradient has Certain limitations.
  • the purpose of the present invention is to overcome the shortcomings of the prior art and provide a gas-solid fluidized bed dry separation system using a separation density gradient. Coarse particles and fine particles are selected as the separation medium, and coarse and fine particles are used for fluidization.
  • the formed density gradient strengthens the separation of minerals and improves the efficiency of mineral separation.
  • the present invention provides a gas-solid fluidized bed dry separation process using a separation density gradient.
  • coarse particles and fine particles are selected as the separation medium
  • the aerodynamic diameter of the coarse particles is greater than the aerodynamic diameter of the fine particles, and the ratio of the aerodynamic diameter of the coarse particles to the fine particles is not greater than 10; the coarse particles are placed in a gas-solid fluidized bed for dry separation.
  • the fine particles are placed above the coarse particles, and the coarse and fine particles are completely separated under the initial conditions; under the action of the air flow, the coarse and fine particles begin to fluidize to form a high In the density sorting zone and the low-density sorting zone, coarse particles and fine particles are mixed at the contact interface to form an intermediate density sorting zone; the minerals to be sorted are fed from the upper part of the gas-solid fluidized bed dry sorting system, and pass through the low density in turn
  • the sorting area, middle density sorting area and high density sorting area complete the sorting of minerals.
  • the size of the coarse particles and the fine particles are not higher than 500 ⁇ m, and the size of the coarse particles is larger than the size of the fine particles, the size of the coarse particles is uniform or non-uniform, and the size of the fine particles is uniform or non-uniform,
  • the density of the coarse particles is not less than that of the fine particles, and the size and density of the coarse particles and the fine particles are determined according to the requirements of the sorting density.
  • the initial heights of the coarse particles and the fine particles are both 20-100 cm; more preferably, the initial heights of the coarse particles and the fine particles are both 20-50 cm.
  • the minimum fluidization velocity of the coarse particles is greater than the minimum fluidization velocity of the fine particles, and the terminal velocity of the coarse particles is greater than the terminal velocity of the fine particles.
  • the operating gas velocity is higher than the minimum fluidization velocity of coarse particles and lower than the terminal velocity of fine particles, and the operating gas velocity is 60% of the difference between the terminal velocity of fine particles and the minimum fluidization velocity of coarse particles .
  • the particle size of the mineral to be sorted is not greater than 300 mm, and more preferably, the particle size of the mineral to be sorted is 0.5-100 mm.
  • the density adjustment range of the separation bed is 1.0 ⁇ 2.6g/cm 3 , more preferably, the density adjustment range of the separation bed is 1.3 ⁇ 2.0g/cm 3 .
  • the fluid of the fluidizing medium particles can be a series of gases such as air, carbon dioxide, nitrogen, etc., preferably air.
  • the present invention strengthens the separation of minerals through the density gradient (high density, intermediate density, low density) formed by the fluidization of coarse and fine particles, which can improve the accuracy of separation. , Realize the efficient dry separation of coal.
  • the device of the present invention does not use water, has simple operation and maintenance, no pollution, low investment and operating costs, and has significant economic and social benefits.
  • Fig. 1 is a schematic diagram of a gas-solid fluidized bed dry separation system using a separation density gradient to enhance mineral separation according to the present invention.
  • Figure 1 1-fine particles; 2-coarse particles; 3-low-density sorting area; 4-middle-density sorting area; 5-high-density sorting area.
  • the aerodynamic diameter of the coarse particles 2 is larger than the air of the fine particles 1.
  • Dynamic diameter the ratio of the aerodynamic diameter of the coarse particles 2 to the fine particles 1 is not greater than 10 (the aerodynamic diameter is directly related to the sedimentation behavior of the particles, and reflects the hydrodynamic characteristics of coarse particles and fine particles ,
  • the aerodynamic diameter is defined as the diameter of a sphere with a unit density (1g/cm 3 ), when moving in still air at a low Reynolds number, it reaches the same final settling velocity as the actual particle diameter);
  • the coarse particles 2 Placed at the bottom of the gas-solid fluidized bed dry separation system the fine particles 1 are placed above the coarse particles 2, and the coarse particles 2 and the fine particles 1 are completely separated under the initial conditions; Under the action, the coarse particles 2 and fine particles 1 begin to fluidize to form a high-density sorting zone 5 and a low-density sorting zone 3.
  • the coarse particles 2 and fine particles 1 are in a mixed state at the contact interface, forming an intermediate density sorting zone 4.
  • the sorting density of the low-density sorting area 3 is less than the density required for the sorting of the minerals to be selected, the sorting density of the intermediate-density sorting area 4 is close to the density required for the sorting of the minerals to be selected, and the high density
  • the sorting density of the sorting zone 5 is greater than or equal to the required density of the minerals to be sorted; the minerals to be sorted are fed from the upper part of the gas-solid fluidized bed dry sorting system, and pass through the low-density sorting zone 3, the middle density sorting in turn
  • the selection zone 4 and the high-density separation zone 5 the minerals with low density float on the upper part of the gas-solid fluidized bed dry process system and are called light products, and the dense minerals sink into the gas-solid fluidized bed dry process system.
  • the middle and lower parts are called heavy products, which complete the separation of minerals.
  • the size of the coarse particles and the fine particles are not higher than 500 ⁇ m, and the size of the coarse particles is larger than the size of the fine particles, the size of the coarse particles 2 is uniform or non-uniform, and the size of the fine particles 1 is uniform or non-uniform.
  • the density of the coarse particles 2 is not less than that of the fine particles 1, and the size and density of the coarse particles and the fine particles are determined according to the requirements of the sorting density.
  • the initial heights of the coarse particles 2 and the fine particles 1 are both 20-100 cm; more preferably, the initial heights of the coarse particles 2 and the fine particles 1 are both 20-50 cm.
  • the minimum fluidization velocity of the coarse particles 2 is greater than the minimum fluidization velocity of the fine particles 1, and the terminal velocity of the coarse particles 2 is greater than the terminal velocity of the fine particles 1.
  • the fluid of the fluidizing medium particles can be a series of gases such as air, carbon dioxide, nitrogen, etc., preferably air; in the actual separation process, the operating gas velocity is higher than the minimum fluidizing gas velocity of coarse particles and lower than the terminal velocity of fine particles.
  • the operating gas velocity is selected to be approximately 60% of the difference between the terminal velocity of fine particles and the minimum fluidization velocity of coarse particles.
  • the particle size of the minerals that can be sorted in the present invention is not more than 300mm, preferably 0.5-100mm; the density adjustment range of the gas-solid fluidized bed sorting system is 1.0-2.6g/cm 3 , and the optimal sorting density is 1.3-2.0g /cm 3 .
  • High-density sorting is required for coal samples, and the sorting density is required to be greater than 1900kg/m 3 .
  • the density of coarse particles formed by the airflow is about 2100kg/m 3 , which is called the high-density sorting zone; the fine particles are in the airflow.
  • the density formed by the action is about 1800kg/m 3 , which is called the low-density sorting zone; the density formed by the contact interface of the two particles is about 1900kg/m 3 , which is called the intermediate density sorting zone.
  • the coal samples are preliminarily screened, and the coal samples of 6-50 mm are used as the candidate minerals, and the minerals with a density far smaller than the low-density area of the bed float on the upper part of the gas-solid fluidized bed dry process system through the low-density sorting zone; Through the intermediate density sorting zone, the preliminary sorted samples are further sorted, which helps to complete the further separation of coal and gangue; through the high-density sorting zone, dense minerals sink into the gas-solid fluidized bed dry process system The middle and lower parts are called heavy products, which finally realize the complete separation of minerals.
  • Low-density sorting is required for coal samples, and the sorting density is required to be greater than 1300kg/m 3 .
  • the static packing height of the particles is 20 cm respectively.
  • the density of coarse particles formed by the airflow is about 1500kg/m 3 , which is called the high-density sorting zone; the fine particles are in the airflow.
  • the density formed under the action is about 1300kg/m 3 , which is called the low-density sorting zone; the density formed by the contact interface of the two particles is about 1100kg/m 3 , which is called the intermediate density sorting zone.
  • the coal samples are preliminarily screened, and the coal samples of 6-50 mm are used as the candidate minerals, and the minerals with a density far smaller than the low-density area of the bed float on the upper part of the gas-solid fluidized bed dry process system through the low-density sorting zone; Through the intermediate density sorting zone, the preliminary sorted samples are further sorted, which helps to complete the further separation of coal and gangue; through the high-density sorting zone, dense minerals sink into the gas-solid fluidized bed dry process system The middle and lower parts are called heavy products, which finally realize the complete separation of minerals.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
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Abstract

提供了一种利用分选密度梯度的气固流化床干法分选工艺，在气固流化床干法分选系统中，选取粗颗粒（2）和细颗粒（1）作为分选介质，粗颗粒（2）与细颗粒（1）的空气动力学直径比例不大于10；粗颗粒（2）置于气固流化床干法分选系统的底部，细颗粒（1）置于粗颗粒（2）上方，粗颗粒（2）和细颗粒（1）在初始条件下处于完全分离状态；在气流的作用下，所述粗颗粒（2）和细颗粒（1）开始流化，形成高密度分选区（5）和低密度分选区（3），粗颗粒（2）和细颗粒（1）在接触界面呈现混合状态，形成中间密度分选区（4）；待分选矿物由气固流化床干法分选系统上部给入，依次通过低密度分选区（3）、中间密度分选区（4）以及高密度分选区（5），完成矿物的分选。利用粗、细颗粒流化形成的密度梯度强化矿物的分选，提高矿物的分选效率。

Description

一种利用分选密度梯度的气固流化床干法分选工艺 技术领域
本发明涉及矿物加工方法，属于干法选矿技术领域，具体涉及一种利用分选密度梯度的气固流化床干法分选工艺。
背景技术
煤炭是世界重要的基础能源之一，对世界经济的发展具有重大的推动作用。煤炭巨大的消费量及产量对于国民的生存环境和生态安全带来了严峻的挑战，“雾霾”、“酸雨”等环境问题引发了政府和百姓的普遍关注。
选煤是煤炭清洁利用的基础，对提高煤炭产品质量以及煤炭燃前的预处理提质具有重要的作用。随着水资源日益短缺，气固流化床干法分选技术受到了中国、加拿大、日本、印度、澳大利亚等国家学者的重点关注。气固流化床干法分选技术主要采用磁铁矿物作为加重质，在气流的作用下形成具有一定密度的似流体，按照密度将待选矿物进行分离，形成轻产物和重产物，具有流程简单，分选精度高等优势，为煤炭分选的加工利用提供了一条重要途径。目前，传统的气固流化床分选机采用空气动力学直径接近的两种颗粒混合调节分选密度，分选系统中形成单一的分选密度。由于待选矿物中的密度组成复杂，接近分选密度的矿物容易发生错配现象，降低分选效率，降低产品的质量。中国发明专利申请CN1161884公开了一种用双密度层空气重介流化床进行三产品分选的方法及装置，主要用来实现生产三种不同的矿物的目的，但不难发现，低密度和高密度的调节主要依靠选取颗粒的密度和尺寸，未考虑利用颗粒的散式膨胀特性优化分选密度的调节；分选采用的流化床为锥形斜面设计，倾斜角度为60°～80°，会提高形成喷动床的可能性，不利于矿物的分选；分选密度主要分为重而大颗粒形成的高密度分选区和轻而小的颗粒形成的低密度分选区，密度梯度具有一定的局限性。
发明内容
本发明的目的是克服已有技术的不足，提供一种利用分选密度梯度的气固流化床干法分选系统，选取粗颗粒和细颗粒作为分选介质，利用粗、细颗粒流化形成的密度梯度强化矿物的分选，提高矿物的分选效率。
为了实现上述目的，本发明提供一种利用分选密度梯度的气固流化床干法分 选工艺，在气固流化床干法分选系统中，选取粗颗粒和细颗粒作为分选介质，所述粗颗粒的空气动力学直径大于所述细颗粒的空气动力学直径，粗颗粒与细颗粒的空气动力学直径比例不大于10；所述粗颗粒置于气固流化床干法分选系统的底部，所述细颗粒置于粗颗粒上方，所述粗颗粒和细颗粒在初始条件下处于完全分离状态；在气流的作用下，所述粗颗粒和细颗粒开始流化，形成高密度分选区和低密度分选区，粗颗粒和细颗粒在接触界面呈现混合状态，形成中间密度分选区；待分选矿物由气固流化床干法分选系统上部给入，依次通过低密度分选区、中间密度分选区以及高密度分选区，完成矿物的分选。
优选的，所述的粗颗粒和细颗粒的尺寸均不高于500μm，且粗颗粒尺寸大于细颗粒尺寸，所述粗颗粒的尺寸均一或非均一，所述细颗粒的尺寸均一或非均一，所述粗颗粒密度不小于细颗粒，依据分选密度的需求确定粗颗粒和细颗粒的尺寸和密度。
优选的，所述粗颗粒和细颗粒的初始高度均为20～100cm；更优选的，所述粗颗粒和细颗粒的初始高度均为20～50cm。
优选的，所述粗颗粒的最小流化速度大于细颗粒的最小流化速度，所述粗颗粒的终端末速大于细颗粒的终端末速。
优选的，操作气速高于粗颗粒的最小流化气速，低于细颗粒的终端末速，所述的操作气速为细颗粒终端末速与粗颗粒最小流化速度之差的60％。
优选的，待分选矿物的粒度不大于300mm，更优选的，待分选矿物的粒度为0.5～100mm。
优选的，所述的气固流化床干法分选系统中，分选床层的密度调节范围为1.0～2.6g/cm 3，更优选的，分选床层的密度调节范围为1.3～2.0g/cm 3。
流化介质颗粒的流体可以采用空气、二氧化碳、氮气等一系列气体，优选空气。
与传统的气固流化床干法分选技术相比，本发明通过粗、细颗粒流化形成的密度梯度(高密度、中间密度、低密度)强化矿物的分选可提高分选的精度，实现煤炭的高效干法分选。此外，本发明的装置不用水，操作维护简单、无污染，投资和运行成本低，具有显著的经济和社会效益。
附图说明
图1是本发明的利用分选密度梯度强化矿物分选的气固流化床干法分选系统示意图。
图1中：1-细颗粒；2-粗颗粒；3-低密度分选区；4-中间密度分选区；5-高密度分选区。
具体实施方式
为了更好地理解本发明，下面结合附图和实例进行阐述。
如图1所示，在气固流化床干法分选系统中，选取粗颗粒2和细颗粒1作为分选介质，所述粗颗粒2的空气动力学直径大于所述细颗粒1的空气动力学直径，所述的粗颗粒2与细颗粒1的空气动力学直径比例不大于10(所述的空气动力学直径与颗粒的沉降行为直接相关，是反映粗颗粒与细颗粒的流体力学特征，空气动力学直径的定义为单位密度(1g/cm 3)的球体，在静止空气中作低雷诺数运动时，达到与实际粒子相同的最终沉降速度时的直径)；所述的粗颗粒2置于气固流化床干法分选系统的底部，所述的细颗粒1置于粗颗粒2上方，所述的粗颗粒2和细颗粒1在初始条件下处于完全分离状态；在气流的作用下，所述的粗颗粒2和细颗粒1开始流化，形成高密度分选区5和低密度分选区3，粗颗粒2和细颗粒1在接触界面呈现混合状态，形成中间密度分选区4，所述的低密度分选区3的分选密度小于待选矿物分选要求的密度，所述的中间密度分选区4的分选密度接近待选矿物分选要求的密度，所述的高密度分选区5的分选密度大于或等于待分选矿物分选要求的密度；待分选矿物由气固流化床干法分选系统上部给入，依次通过低密度分选区3、中间密度分选区4以及高密度分选区5，密度小的矿物浮在所述的气固流化床干法系统的上部称为轻产物，密度大的矿物沉入所述的气固流化床干法系统的中下部称为重产物，完成矿物的分选。
所述的粗颗粒和细颗粒的尺寸均不高于500μm，且粗颗粒尺寸大于细颗粒尺寸，所述粗颗粒2的尺寸均一或非均一，所述细颗粒1的尺寸均一或非均一，所述粗颗粒2密度不小于细颗粒1，依据分选密度的需求确定粗颗粒和细颗粒的尺寸和密度。
所述粗颗粒2和细颗粒1的初始高度均为20～100cm；更优选的，所述粗颗粒2和细颗粒1的初始高度均为20～50cm。
所述粗颗粒2的最小流化速度大于细颗粒1的最小流化速度，所述粗颗粒2 的终端末速大于细颗粒1的终端末速。
流化介质颗粒的流体可以采用空气、二氧化碳、氮气等一系列气体，优选空气；实际分选过程中，操作气速高于粗颗粒的最小流化气速，低于细颗粒的终端末速，所述的操作气速选择约为细颗粒终端末速与粗颗粒最小流化速度之差的60％。
本发明可分选的矿物粒度不大于300mm，优选0.5～100mm；所述的气固流化床分选系统密度调节范围为1.0～2.6g/cm 3，最佳分选密度为1.3～2.0g/cm 3。
下面结合煤炭分选实例，详细介绍利用分选密度梯度的气固流化床干法分选工艺的应用过程。
实施例1
针对煤炭样品需要进行高密度分选，分选密度要求大于1900kg/m 3。选择粗磁铁矿粉(平均粒径d p＝100μm,真密度ρ＝4600kg/m 3)与细磁铁矿粉(平均粒径d p＝45μm,真密度ρ＝4600kg/m 3)作为介质颗粒，两种介质颗粒的静止堆积高度为分别为30cm。选择空气为流化介质颗粒所需的气体，通过分选系统的底部给入，粗颗粒在气流的作用下形成的密度约为2100kg/m 3，称为高密度分选区；细颗粒在气流的作用下形成的密度约为1800kg/m 3，称为低密度分选区；两种颗粒接触界面形成的密度约为1900kg/m 3，称为中间密度分选区。煤炭样品经过初步筛分，6～50mm的煤炭样品作为待选矿物，通过低密度分选区，密度远小于床层低密度区的矿物浮在所述的气固流化床干法系统的上部；通过中间密度分选区，初步分选的样品进一步完成分选，有助于完成煤炭和矸石的进一步分离；通过高密度分选区，密度大的矿物沉入所述的气固流化床干法系统的中下部称为重产物，最终实现矿物的完全分选。
实施例2
针对煤炭样品需要进行低密度分选，分选密度要求大于1300kg/m 3。选择石英砂(平均粒径d p＝100μm,真密度ρ＝2600kg/m 3)和石英砂(平均粒径d p＝40μm,真密度ρ＝2600kg/m 3)与作为介质颗粒，两种介质颗粒的静止堆积高度为分别为20cm。选择空气为流化介质颗粒所需的气体，通过分选系统的底部给入，粗颗粒在气流的作用下形成的密度约为1500kg/m 3，称为高密度分选区；细颗粒在气流的作用下形成的密度约为1300kg/m 3，称为低密度分选区；两种颗粒接触界面 形成的密度约为1100kg/m 3，称为中间密度分选区。煤炭样品经过初步筛分，6～50mm的煤炭样品作为待选矿物，通过低密度分选区，密度远小于床层低密度区的矿物浮在所述的气固流化床干法系统的上部；通过中间密度分选区，初步分选的样品进一步完成分选，有助于完成煤炭和矸石的进一步分离；通过高密度分选区，密度大的矿物沉入所述的气固流化床干法系统的中下部称为重产物，最终实现矿物的完全分选。
以上所述仅是本发明的优选实施方式，并不用于限制本发明。应该指出，对于本技术领域的普通技术人员来说，在不脱离本发明原理的前提下，还可以做出若干改进和润饰，这些改进和润饰也应该视为本发明的保护范围。

Claims (10)

  1. 一种利用分选密度梯度的气固流化床干法分选工艺，其特征在于，在气固流化床干法分选系统中，选取粗颗粒和细颗粒作为分选介质颗粒，所述粗颗粒的空气动力学直径大于所述细颗粒的空气动力学直径，粗颗粒与细颗粒的空气动力学直径比例不大于10；所述粗颗粒置于气固流化床干法分选系统的底部，所述细颗粒置于粗颗粒上方，所述粗颗粒和细颗粒在初始条件下处于完全分离状态；在气流的作用下，所述粗颗粒和细颗粒开始流化，形成高密度分选区和低密度分选区，粗颗粒和细颗粒在接触界面呈现混合状态，形成中间密度分选区；待分选矿物由气固流化床干法分选系统上部给入，依次通过低密度分选区、中间密度分选区以及高密度分选区，完成矿物的分选。
  2. 根据权利要求1所述的一种利用分选密度梯度的气固流化床干法分选工艺，其特征在于，所述的粗颗粒和细颗粒的尺寸均不高于500μm，且粗颗粒尺寸大于细颗粒尺寸，所述粗颗粒的尺寸均一或非均一，所述细颗粒的尺寸均一或非均一，所述粗颗粒密度不小于细颗粒密度。
  3. 根据权利要求1所述的一种利用分选密度梯度的气固流化床干法分选工艺，其特征在于，所述粗颗粒和细颗粒的初始高度均为20～100cm。
  4. 根据权利要求3所述的一种利用分选密度梯度的气固流化床干法分选工艺，其特征在于，所述粗颗粒和细颗粒的初始高度均为20～50cm。
  5. 根据权利要求1所述的一种利用分选密度梯度的气固流化床干法分选工艺，其特征在于，所述粗颗粒的最小流化速度大于细颗粒的最小流化速度，所述粗颗粒的终端末速大于细颗粒的终端末速。
  6. 根据权利要求1所述的一种利用分选密度梯度强化矿物分选的气固流化床干法分选系统，其特征在于，操作气速高于粗颗粒的最小流化气速，低于细颗粒的终端末速，所述的操作气速为细颗粒终端末速与粗颗粒最小流化速度之差的60％。
  7. 根据权利要求1所述的一种利用分选密度梯度强化矿物分选的气固流化床干法分选系统，其特征在于，待分选矿物的粒度不大于300mm。
  8. 根据权利要求7所述的一种利用分选密度梯度的气固流化床干法分选工艺，其特征在于：待分选矿物的粒度为0.5～100mm。
  9. 根据权利要求1所述的一种利用分选密度梯度的气固流化床干法分选工 艺，其特征在于，所述的气固流化床干法分选系统中，分选床层的密度调节范围为1.0～2.6g/cm 3。
  10. 根据权利要求9所述的一种利用分选密度梯度的气固流化床干法分选工艺，其特征在于，所述的气固流化床干法分选系统中，分选床层的密度调节范围为1.3～2.0g/cm 3。
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