WO2020199817A1 - 提高颗粒流化质量和分选密度稳定性的方法及配套装置 - Google Patents

提高颗粒流化质量和分选密度稳定性的方法及配套装置 Download PDF

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WO2020199817A1
WO2020199817A1 PCT/CN2020/077333 CN2020077333W WO2020199817A1 WO 2020199817 A1 WO2020199817 A1 WO 2020199817A1 CN 2020077333 W CN2020077333 W CN 2020077333W WO 2020199817 A1 WO2020199817 A1 WO 2020199817A1
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gas
particles
fluidized bed
density
separation
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PCT/CN2020/077333
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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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    • 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
    • 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
    • B07B7/00—Selective separation of solid materials carried by, or dispersed in, gas currents

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  • the invention relates to a mineral processing method and belongs to the technical field of dry beneficiation, in particular to a method and a supporting device for improving the fluidization quality of particles and the stability of the separation density.
  • Coal sorting and processing is an indispensable and important link in the process of coal production and efficient utilization. It is the basis and prerequisite for achieving clean coal utilization, energy saving, emission reduction, and sustainable and healthy development.
  • my country's coal sorting technology is still dominated by wet sorting, and the sorting process requires a lot of water resources.
  • my country's lignite resources are rich, and it is difficult to use traditional wet technology due to its easy silting characteristics. Therefore, the development of dry separation technology is of great significance to reduce water consumption and improve the utilization of coal resources.
  • the gas-solid fluidization separation technology relies on the medium under the action of gas to form a fluid-like bed with a certain density to realize the separation of coal gangue.
  • Scholars from various countries have conducted detailed research on fluidized dry coal preparation technology, put forward corresponding fluidized separation theory, developed gas-solid fluidized bed separation systems of different scales, and have gradually applied to industrialization and large-scale production. In practice, it provides an important way for the processing and utilization of coal sorting.
  • the traditional gas-solid fluidized bed sorting machine uses the mixing of light and heavy particles with close aerodynamic diameters, usually using -0.3+0.15mm magnetite powder and -1mm fine coal powder as the aggravating material, relying on low-density coal
  • the addition of powder can effectively reduce the overall density of the bed in the sorting machine and realize the control of the sorting density.
  • the magnetite powder and coal powder particles used are relatively coarse, and large-sized bubbles are easily formed during fluidization, the bed expansion degree is low, and the bed density fluctuates greatly, which restricts its sorting performance to a certain extent.
  • the traditional gas-solid fluidized bed beneficiation technology is difficult to achieve the separation of -6mm fine coal, and there is an urgent need for an efficient dry separation technology suitable for the separation of fine coal.
  • the purpose of the present invention is to overcome the shortcomings of the prior art and provide a method and a supporting device for improving the fluidization quality of particles and the stability of the sorting density.
  • Coarse particles and fine particles are selected as the sorting medium, and the introduction of fine particles is effective Decreasing the average particle size of the particles in the fluidized bed can improve the fluidization performance of coarse particles; the reduction of particle size makes the particles show the characteristics of uniform bulk expansion, which helps to improve the expansion of the emulsified phase; the bubble size increases with the particle size The reduction also shows a decreasing trend, increasing the overall expansion height of the bed, reducing the fluctuation of the separation density, helping to improve the stability of the separation density, and solving the problem of the stability of the separation density in the existing gas-solid fluidized bed Difficulties in the separation of low-performance and fine-grained minerals.
  • the present invention provides a method for improving the fluidization quality of particles and the stability of the separation density.
  • coarse particles and fine particles are selected as the separation medium, and The coarse particles and the fine particles are fully mixed to form a sorting bed with a certain density under the action of the air flow.
  • the expansion height of the bed is adjusted to realize the control of the sorting density;
  • the particle size is not more than 500 ⁇ m, the fine particle size is not more than 45 ⁇ m, and the aerodynamic diameter ratio of the coarse particles to the fine particles is not less than 5.
  • the size of the coarse particles is uniform or non-uniform
  • the size of the fine particles is uniform or non-uniform
  • the density of the coarse particles and the fine particles are consistent or inconsistent.
  • the coarse particles are the main medium in the gas-solid fluidized bed
  • the fine particles are the additional medium
  • the volume fraction control range of the fine particles is 0-50%
  • the volume fraction control range of the fine particles is preferably 0%. ⁇ 20%
  • the added content is determined according to the requirement of sorting density.
  • the coarse particles are mainly magnetic materials, preferably magnetite powder, which is convenient for separation and recovery; the fine particles are mainly one or several components of the mineral to be selected, which is convenient for obtaining and preparing.
  • the operating gas velocity in the sorting process is higher than the minimum fluidization gas velocity of coarse particles and lower than the terminal velocity of fine particles.
  • the density adjustment range of the separation bed is 1.0-2.6 g/cm 3
  • the optimal separation density is 1.3-2.0 g/cm 3 .
  • the height of the separation bed is not higher than 100 cm, preferably in the range of 30 to 70 cm.
  • the present invention also provides a matching device for improving the fluidization quality of particles and the stability of the sorting density, which includes an air supply device, a gas-solid fluidized bed body, a material level height test device, a scraper conveyor device, a density measurement device and Dust removal device; the gas-solid fluidized bed body is arranged above the air supply device, the bottom surface of the gas-solid fluidized bed body is provided with an air inlet, and the upper left of the gas-solid fluidized bed body is provided with a mineral feed inlet to be selected, and the gas-solid flow
  • the upper right of the fluidized bed body is provided with a medium particle feeding port, the upper part of one side of the gas-solid fluidized bed body is provided with a light product discharge port, and the lower part of the other side of the gas-solid fluidized bed body is provided with a heavy product discharge port.
  • the air supply device includes an induced air duct and an air distribution chamber.
  • the induced air duct is provided with a number of regulating valves, the induced air duct is arranged below the air distribution chamber, and the air distribution chamber is arranged below the body of the gas-solid fluidized bed.
  • the air duct is connected with the air inlet of the air distribution chamber through the regulating valve, the air outlet of the air distribution chamber is connected with the air inlet at the bottom of the gas-solid fluidized bed body, the air supply device is responsible for introducing gas into the fluidized bed, the material level height test device It is arranged outside the body of the gas-solid fluidized bed, the scraper conveyor device is arranged inside the body of the gas-solid fluidized bed, and the density measuring device is arranged outside the body of the gas-solid fluidized bed, and is collected by interconnected pressure signals It consists of a system and a computer.
  • the dust removal device is arranged above the body of the gas-solid fluidized bed. It has the functions of evenly distributing air, transporting floating objects, transporting sinking objects, and measuring the height and density of the material. They are independent of each other. run.
  • the supporting device of the gas-solid fluidized bed dry separation system is mainly used for the separation of coal, and the particle size of the minerals that can be separated is not more than 300mm, preferably 0.5-100mm.
  • the supporting devices of the gas-solid fluidized bed dry separation system do not interfere with each other and operate independently to ensure the stability of the mineral separation process; coarse particles and fine particles are selected as the separation medium to ensure the separation of coarse and fine particles Fully mixed to form a sorting bed with a certain density under the action of airflow.
  • the introduction of fine particles improves the fluidization performance of the particles, promotes the bulk expansion of the particle phase, reduces the size of bubbles, and improves the separation density.
  • Stability In the supporting device of the gas-solid fluidized bed dry separation system, fine or coarse particle media will be continuously or intermittently added and taken out.
  • the present invention selects coarse particles and fine particles as the separation medium.
  • the average particle size of the particles in the fluidized bed can be effectively reduced, and the coarse particles can be improved.
  • the expansion height reduces the fluctuation of the sorting density, helps to improve the stability of the sorting density, improves the precision of mineral sorting, and realizes the efficient sorting 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.
  • Figure 1 is a schematic diagram of the method for improving the fluidization quality of particles and the stability of the sorting density of the present invention.
  • Figure 2 is a supporting device for improving particle fluidization quality and separation density stability in the gas-solid fluidized bed dry separation system of the present invention.
  • 1 induced air duct 1 induced air duct, 2 regulating valve, 3 air distribution chamber, 4 product discharge ports, 5 material level height test device, 6 mineral feed ports to be selected, 7 fluidized bed body, 8 scraper conveyor Device, 9 dust removal device, 10 medium particle, 11 medium particle feed port, 12 light product discharge port, 13 pressure signal acquisition system, 14 computer.
  • coarse particles and fine particles are selected as the separation medium to ensure that the coarse particles and fine particles are fully mixed, and form a certain density under the action of airflow.
  • introduction of fine particles improves the fluidization performance of the particles, promotes the bulk expansion of the particle phase, reduces the size of bubbles, and improves the stability of the sorting density.
  • the coarse particles are the main medium in the gas-solid fluidized bed
  • the fine particles are the additional medium
  • the volume fraction of the fine particles is controlled within a range of 0-50%
  • the added content is determined according to the requirements of the sorting density.
  • the size of the coarse particles is not greater than 500 ⁇ m, the size of the fine particles is not greater than 45 ⁇ m, and the aerodynamic diameter ratio of the coarse particles to the fine particles is not less than 5.
  • the aerodynamic diameter is directly related to the sedimentation behavior of particles and reflects the hydrodynamic characteristics of coarse and fine particles.
  • the aerodynamic diameter is defined as a sphere with a unit density (1g/cm 3 ), which is used in still air. When moving at a low Reynolds number, the diameter when the final sedimentation velocity is the same as the actual particle.
  • the size of the coarse particles is uniform or non-uniform
  • the size of the fine particles is uniform or non-uniform
  • the density of the coarse particles and the fine particles are consistent or inconsistent.
  • the coarse particles are the main medium in the gas-solid fluidized bed
  • the fine particles are the additional medium
  • the volume fraction control range of the fine particles is 0-50%
  • the volume fraction control range of the fine particles is preferably 0%. ⁇ 20%
  • the added content is determined according to the requirement of sorting density.
  • the coarse particles are mainly magnetic materials, and magnetite powder is preferentially selected, which is convenient for separation and recovery; the fine particles are mainly composed of one or several components of the mineral to be selected, which is convenient for obtaining and preparing.
  • the supporting device of the gas-solid fluidized bed dry separation system for improving the particle fluidization quality and the stability of the separation density in the present invention includes a gas-solid fluidized bed body 7, an air supply device, and a material level.
  • Test device 5 scraper conveyor device 8, density measuring device and dust removal device 9.
  • the gas-solid fluidized bed body 7 is arranged above the air supply device, the bottom surface of the gas-solid fluidized bed body 7 is provided with an air inlet, and the gas-solid fluidized bed body 7 is provided with a mineral feed inlet 6 to be selected at the upper left.
  • the gas-solid fluidized bed body 7 is provided with a medium particle feeding port 11 on the upper right side to guide the medium particles into the fluidized bed body; the upper side of the gas-solid fluidized bed body 6 is provided There is a light product discharge port 12 to guide the separated light product to be discharged from the fluidized bed body; the gas-solid fluidized bed body 7 is provided with a heavy product discharge port 4 on the other side of the body to guide the heavy product after separation The fluidized bed body is discharged.
  • the air supply device includes an induced air duct 1 and an air distribution chamber 3.
  • a number of regulating valves 2 are arranged on the induced air duct 1.
  • the induced air duct 1 is arranged under the air distribution chamber 3, and the air distribution chamber 3 is arranged in the gas-solid fluidization.
  • Below the bed body 7, the induced air duct is connected with the air inlet of the air distribution chamber through the regulating valve, the air outlet of the air distribution chamber is connected with the air inlet at the bottom of the gas-solid fluidized bed body, and the air supply device is responsible for introducing gas into the fluidized bed.
  • the air supply device can use a series of gases such as air, carbon dioxide, nitrogen, etc., preferably air as the fluid of the fluidizing medium particles; 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.
  • gases such as air, carbon dioxide, nitrogen, etc.
  • the material level height testing device 5 is arranged on the outer wall surface of the gas-solid fluidized bed body 7 and is responsible for monitoring the height of the fluidized bed medium particles.
  • the scraper conveyor device 8 is arranged inside the gas-solid fluidized bed body 7 and is responsible for transporting the sorted light products and heavy products to the corresponding discharge ports.
  • the density measuring device is arranged outside the gas-solid fluidized bed body 7 and is composed of a pressure signal acquisition system 13 and a computer 14 connected to each other, and is responsible for monitoring the density of the fluidized bed sorter.
  • the dust removal device 9 is arranged above the gas-solid fluidized bed body 7 and is responsible for collecting fine dust generated during the sorting process and ensuring a clean and tidy sorting environment.
  • the supporting devices of the gas-solid fluidized bed dry separation system do not interfere with each other and operate independently to ensure the stability of the mineral separation process; coarse particles and fine particles are selected as the medium particles 10, and the size of the coarse particles is different.
  • the size of the fine particles is greater than 500 ⁇ m, the size of the fine particles is not greater than 45 ⁇ m, and the aerodynamic diameter ratio of the coarse particles to the fine particles is not greater than 25 to ensure that the coarse particles and the fine particles are fully mixed, and the particles with a certain density are formed under the action of the airflow.
  • the introduction of fine particles improves the fluidization performance of the particles, promotes the bulk expansion of the particle phase, reduces the size of bubbles, and improves the stability of the separation density.
  • fine particles or coarse particles are continuously or intermittently added and taken out.
  • the supporting device of the gas-solid fluidized bed dry separation system is mainly used for the separation of coal, and the mineral particle size that can be separated is not greater than 300mm, preferably 0.5-100mm; the gas-solid fluidized bed dry separation system In the separation system, the density adjustment range of the separation bed is 1.0 ⁇ 2.6g/cm 3 , and the optimal separation density is 1.3 ⁇ 2.0g/cm 3 ; in the gas-solid fluidized bed dry separation system, The height of the sorting bed is not higher than 100 cm, preferably in the range of 30 to 70 cm.
  • the required sorting density is 1800kg/m 3 .
  • the volume fraction of ultra-fine coal powder is about 10%, and the static accumulation height of media particles is 30 cm.
  • the coal samples are preliminarily screened, and coal samples of 6-50 mm are used as candidate minerals. Introduce the required coarse and fine medium particles into the fluidized bed body through the medium particle feed port, and adjust the air supply device (induction duct, regulating valve and air distribution chamber) to control the sorting gas speed to be approximately greater than the critical flow gas velocity 0.4cm / s, under the action of the gas in the media particles, the formation density of about 1800kg / m 3 of fluidized bed, the bed pressure drop fluctuation variance of about 70, the maximum bubble diameter of about 2cm,
  • the sorting environment of the bed is relatively stable.
  • the raw coal enters the fluidized bed body through the feed port of the mineral to be selected, and is affected by the overall density of the fluidized bed of medium particles.
  • the clean coal and gangue of the mineral to be selected are stratified according to the bed density, which is less than 1800kg/m 3
  • the clean coal floats to the upper part of the fluidized bed body to become clean coal, and the clean coal whose bed density is greater than 1800kg/m 3 floats to the lower part of the fluidized bed body to become gangue, and the clean coal and gangue are transported to light
  • the product discharge port and the heavy product discharge port complete the separation of coal.
  • the density measuring device is composed of a pressure signal acquisition system and a computer, and is responsible for monitoring the density of the fluidized bed sorting machine; the material level height testing device is responsible for monitoring the height of the fluidized bed medium particles; The dust removal device is responsible for collecting the fine dust generated in the sorting process and ensuring the cleanliness of the sorting environment.

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Abstract

提供了一种提高颗粒流化质量和分选密度稳定性的方法及配套装置，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，并使粗颗粒和细颗粒充分混合，在气流的作用下形成具有一定密度的分选床层，粗颗粒尺寸不大于500μm，细颗粒尺寸不大于45μm，粗颗粒与细颗粒的空气动力学直径比例不小于5。该配套装置包括气固流化床机体（7）、供风装置、料位高度测试装置（5）、刮板输送机装置（8）、密度测量装置和除尘装置（9）。通过细颗粒的引入改善介质颗粒的流化质量，减小气泡尺寸，提高分选密度的稳定性，可提高矿物分选的精度，实现煤炭的高效分选。该装置不用水，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。

Description

提高颗粒流化质量和分选密度稳定性的方法及配套装置 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，具体涉及一种提高颗粒流化质量和分选密度稳定性的方法及配套装置。
背景技术
煤炭分选加工是煤炭生产和高效利用过程中不可缺少的一个重要环节，是实现煤炭清洁利用、节能减排和可持续健康发展的基础和前提。我国煤炭分选技术仍然以湿法分选为主，分选过程需要消耗大量的水资源。此外，我国褐煤资源丰富，由于其易泥化的特点，难以采用传统的湿法技术。因此，开展干法分选技术对减少水资源消耗，提高煤炭资源的利用具有十分重要的意义。
气固流态化分选技术依靠介质在气体的作用下，形成具有一定密度的似流体床层，实现对煤炭的矸石的分离。各国学者对流态化干法选煤技术进行了详细地研究，提出了相应的流态化分选理论，研制了不同规模的气固流化床分选系统，已经逐步应用于工业化和大型化生产实践当中，为煤炭分选的加工利用提供了一条重要途径。
传统的气固流化床分选机利用空气动力学直径接近的轻重两种颗粒混合，通常采用-0.3+0.15mm的磁铁矿粉与-1mm细粒煤粉作为加重质，依靠低密度煤粉的添加，可以有效降低分选机内床层的整体密度，实现对分选密度的调控。然而，采用的磁铁矿粉和煤粉颗粒较粗，流化时易形成尺寸大的气泡，床层膨胀程度较低，床层密度波动较大，一定程度上制约了其分选性能。此外，传统的气固流化床选矿技术难以实现对-6mm细粒煤的分选，迫切需要一种适用于细粒煤分选的高效干法分选技术。
发明内容
本发明的目的是克服已有技术的不足，提供一种提高颗粒流化质量和分选密度稳定性的方法及配套装置，选取粗颗粒和细颗粒作为分选介质，通过细颗粒的引入，有效降低流化床中颗粒的平均粒度，可以改善粗颗粒的流化性能；颗粒尺寸的减小，颗粒呈现均匀散式膨胀的特征，有助于提高乳化相的膨胀；气泡尺寸随着颗粒尺寸的减小也呈现减小的趋势，提高床层的整体膨胀高度，降低了分选 密度的波动，有助于提高分选密度的稳定性，解决现有气固流化床选矿中分选密度稳定性低和细粒矿物分选的难题。
为了实现上述目的，本发明提供一种提高颗粒流化质量和分选密度稳定性的方法，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，并使粗颗粒和细颗粒充分混合，在气流的作用下形成具有一定密度的分选床层，通过调节所述细颗粒的含量，调节床层膨胀高度，实现对分选密度的控制；所述的粗颗粒尺寸不大于500μm，所述细颗粒尺寸不大于45μm，所述粗颗粒与细颗粒的空气动力学直径比例不小于5。
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，所述粗颗粒与细颗粒密度一致或不一致。
所述的粗颗粒为气固流化床中的主要介质，所述的细颗粒为附加介质，所述细颗粒的体积分数控制范围为0～50％，优选细颗粒的体积分数控制范围为0～20％，依据分选密度的需求确定添加含量。
所述粗颗粒主要以磁性物为主，优选磁铁矿粉，便于分离回收；所述细颗粒主要以待选矿物的一种或几种组分为主，便于获取和制备。
分选过程中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，最佳分选密度为1.3～2.0g/cm 3。
所述的气固流化床干法分选系统中，分选床层高度不高于100cm，优选范围30～70cm。
本发明还提供一种提高颗粒流化质量和分选密度稳定性的配套装置，其包括供风装置、气固流化床机体、料位高度测试装置、刮板输送机装置、密度测量装置和除尘装置；所述气固流化床机体设置在供风装置上方，气固流化床机体底表面设置有进风口，气固流化床机体左上方设有待选矿物给料口，气固流化床机体右上方设有介质颗粒给料口，气固流化床机体一侧上部设有轻产物排料口，气固流化床机体另一侧下部设有重产物排料口，所述供风装置包括引风管道和布风室，所述引风管道上设置有若干个调节阀，引风管道设置在所述布风室下方，布风室设置在气固流化床机体下方，引风管道通过调节阀与布风室的进风口连通， 布风室的出风口与气固流化床机体底部进风口连通，供风装置负责向流化床引入气体，所述料位高度测试装置设置在气固流化床机体外部，所述刮板输送机装置设置在气固流化床机体内部，所述的密度测量装置设置在气固流化床机体外部，由相互连接的压力信号采集系统和计算机组成，所述的除尘装置设置在气固流化床机体的上方，均匀布风、运输浮物、输送沉物、测量料位高度与密度的功能，相互之间互不接触，独立运行。
所述的气固流化床干法分选系统的配套装置主要用于煤炭的分选，可分选的矿物粒度不大于300mm，优选0.5～100mm。
所述的气固流化床干法分选系统的配套装置互不干扰，独立运行，保证矿物分选过程的稳定性；选取粗颗粒和细颗粒作为分选介质，保证粗颗粒和细颗粒的充分混合，在气流的作用下形成有一定密度的分选床层，通过细颗粒的引入改善颗粒的流化性能，促进颗粒相的散式膨胀，减小气泡的尺寸，从而提高分选密度的稳定性；所述的气固流化床干法分选系统的配套装置中，细颗粒或粗颗粒介质会被连续或间歇地加入和取出。
与传统的气固流化床干法分选技术相比，本发明选取粗颗粒和细颗粒作为分选介质，通过细颗粒的引入，有效降低流化床中颗粒的平均粒度，可以改善粗颗粒的流化性能；颗粒尺寸的减小，颗粒呈现均匀散式膨胀的特征，有助于提高乳化相的膨胀；气泡尺寸随着颗粒尺寸的减小也呈现减小的趋势，提高床层的整体膨胀高度，降低了分选密度的波动，有助于提高分选密度的稳定性，可提高矿物分选的精度，实现煤炭的高效分选。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是本发明的提高颗粒流化质量和分选密度稳定性的方法示意图。
图2是本发明的气固流化床干法分选系统中提高颗粒流化质量和分选密度稳定性的配套装置。
图中，1引风管道、2调节阀、3布风室、4重产物排料口、5料位高度测试装置、6待选矿物给料口、7流化床机体、8刮板输送机装置、9除尘装置、10介质颗粒、11介质颗粒给料口、12轻产物排料口、13压力信号采集系统、14计算机。
具体实施方式
为了更好地理解本发明的一种在气固流化床干法分选系统中提高颗粒流化质量和分选密度稳定性的方法及其配套装置，下面结合实例进行阐述。
如图1所示，在气固流化床干法分选系统中，选取粗颗粒和细颗粒作为分选介质，保证粗颗粒和细颗粒的充分混合，在气流的作用下形成具有一定密度的分选床层，通过细颗粒的引入改善颗粒的流化性能，促进颗粒相的散式膨胀，减小气泡的尺寸，从而提高分选密度的稳定性。
所述的粗颗粒为气固流化床中的主要介质，所述的细颗粒为附加介质，所述细颗粒的体积分数控制范围为0～50％，依据分选密度的需求确定添加含量。通过调节所述细颗粒的含量，调节床层膨胀高度，实现对分选密度的控制。
所述粗颗粒尺寸不大于500μm，所述细颗粒尺寸不大于45μm，粗颗粒与细颗粒的空气动力学直径比例不小于5。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，所述粗颗粒与细颗粒密度一致或不一致。
所述的粗颗粒为气固流化床中的主要介质，所述的细颗粒为附加介质，所述细颗粒的体积分数控制范围为0～50％，优选细颗粒的体积分数控制范围为0～20％，依据分选密度的需求确定添加含量。
所述粗颗粒主要以磁性物为主，优先选择磁铁矿粉，便于分离回收；所述细颗粒主要以待选矿物的一种或几种组分为主，便于获取和制备。
如图2所示，本发明中提高颗粒流化质量和分选密度稳定性的气固流化床干法分选系统的配套装置包括气固流化床机体7、供风装置、料位高度测试装置5、刮板输送机装置8、密度测量装置和除尘装置9。
所述气固流化床机体7设置在供风装置上方，气固流化床机体7底表面设置有进风口，所述气固流化床机体7左上方设有待选矿物给料口6，引导待选矿物给入流化床机体；气固流化床机体7右上方设有介质颗粒给料口11，引导介质颗粒给入流化床机体；气固流化床机体6一侧上部设有轻产物排料口12，引导 分选后的轻产物由流化床机体排出；气固流化床机体7另一侧下部设有重产物排料口4，引导分选后的重产物由流化床机体排出。
所述供风装置包括引风管道1和布风室3，引风管道1上设置有若干个调节阀2，引风管道1设置在布风室3下方，布风室3设置在气固流化床机体7下方，引风管道通过调节阀与布风室的进风口连通，布风室的出风口与气固流化床机体底部进风口连通，供风装置负责向流化床内引入气体。所述的供风装置可以采用空气、二氧化碳、氮气等一系列气体，优选空气作为流化介质颗粒的流体；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。
所述料位高度测试装置5设置在气固流化床机体7外侧壁面上，负责监控流化床介质颗粒的高度。
所述刮板输送机装置8设置在气固流化床机体7内部，负责运输分选后的轻产物与重分别至相应的排料口。
所述的密度测量装置设置在气固流化床机体7外部，由相互连接的压力信号采集系统13和计算机14组成，负责监控流化床分选机的密度。
所述的除尘装置9设置在气固流化床机体7的上方，负责收集分选过程中产生的细粒粉尘，保证分选环境的整洁。
所述的气固流化床干法分选系统的配套装置互不干扰，独立运行，保证矿物分选过程的稳定性；选取粗颗粒和细颗粒作为介质颗粒10，所述的粗颗粒尺寸不大于500μm，所述细颗粒尺寸不大于45μm，所述粗颗粒与细颗粒的空气动力学直径比例不大于25，保证粗颗粒和细颗粒的充分混合，在气流的作用下形成有一定密度的分选床层，通过细颗粒的引入改善颗粒的流化性能，促进颗粒相的散式膨胀，减小气泡的尺寸，从而提高分选密度的稳定性。所述的气固流化床干法分选系统的配套装置中，细颗粒或粗颗粒介质会被连续或间歇地加入和取出。
所述的气固流化床干法分选系统的配套装置主要用于煤炭的分选，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，最佳分选密度为1.3～2.0g/cm 3；在所述气固流化床干法分选系统中，分选床层高度不高于100cm，优选范围30～70cm。
下面结合煤炭分选实例，详细介绍一种在气固流化床干法分选系统中提高颗粒流化质量和分选密度稳定性的方法及其配套装置的使用过程。针对提供的煤炭 样品，为有效去除其中的矸石矿物，所需的分选密度为1800kg/m 3。选择磁铁矿粉(平均粒径d p＝75μm,真密度ρ＝4600kg/m 3)与超细煤粉(平均粒径d p＝15μm,真密度ρ＝1500kg/m 3)作为介质颗粒，超细煤粉的体积分数约为10％，介质颗粒的静止堆积高度为30cm。煤炭样品经过初步筛分，6～50mm的煤炭样品作为待选矿物。通过介质颗粒给料口将所需的粗、细两种介质颗粒引入流化床机体，通过调节供风装置(引风管道、调节阀与布风室)将分选气速控制约大于临界流化气速0.4cm/s，介质颗粒在气体的作用下，形成密度约为1800kg/m 3的流化床层，所述床层的压降波动方差约为70，气泡最大直径约为2cm，床层的分选环境较为稳定。原煤通过待选矿物给料口进入流化床机体，受到介质颗粒流化床层整体密度的影响，待选矿物的精煤和矸石按照床层密度进行分层，小于床层密度1800kg/m 3的精煤上浮至流化床机体上部成为精煤，大于床层密度1800kg/m 3的精煤上浮至流化床机体下部成为矸石，通过刮板输送机装置将精煤和矸石分别运输至轻产物排料口与重产物排料口，完成煤炭的分选。分选过程中，所述的密度测量装置由压力信号采集系统和计算机组成，负责监控流化床分选机的密度；所述的料位高度测试装置，负责监控流化床介质颗粒的高度；所述的除尘装置负责收集分选过程中产生的细粒粉尘，保证分选环境的整洁。
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. 一种提高颗粒流化质量和分选密度稳定性的方法，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，并使粗颗粒和细颗粒充分混合，在气流的作用下形成具有一定密度的分选床层，通过调节所述细颗粒的含量，调节床层膨胀高度，实现对分选密度的控制；所述的粗颗粒尺寸不大于500μm，所述细颗粒尺寸不大于45μm，所述粗颗粒与细颗粒的空气动力学直径比例不小于5。
  2. 根据权利要求1所述的一种提高颗粒流化质量和分选密度稳定性的方法，其特征在于，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，所述粗颗粒与细颗粒密度一致或不一致。
  3. 根据权利要求1所述的一种提高颗粒流化质量和分选密度稳定性的方法，其特征在于，所述细颗粒的体积分数控制范围为0～50％，依据分选密度的需求确定添加含量。
  4. 根据权利要求3所述的一种提高颗粒流化质量和分选密度稳定性的方法，其特征在于，所述细颗粒的体积分数控制范围为0～20％。
  5. 根据权利要求1所述的一种提高颗粒流化质量和分选密度稳定性的方法，其特征在于，所述粗颗粒主要是磁性物，所述细颗粒主要是待选矿物的一种或几种组分。
  6. 根据权利要求5所述的一种提高颗粒流化质量和分选密度稳定性的方法，其特征在于，所述磁性物是磁铁矿粉。
  7. 根据权利要求1所述的一种提高颗粒流化质量和分选密度稳定性的方法，其特征在于，分选过程中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。
  8. 根据权利要求1所述的一种提高颗粒流化质量和分选密度稳定性的方法，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。
  9. 根据权利要求1所述的一种提高颗粒流化质量和分选密度稳定性的方法，其特征在于，所述的气固流化床干法分选系统中，分选床层高度不高于100cm。
  10. 一种权利要求1所述的提高颗粒流化质量和分选密度稳定性的方法的配套装置，其特征在于，其包括气固流化床机体(7)、供风装置、料位高度测试装 置(5)、刮板输送机装置(8)、密度测量装置和除尘装置(9)；所述气固流化床机体(7)设置在供风装置上方，气固流化床机体(7)底表面设置有进风口，气固流化床机体(7)左上方设有待选矿物给料口(6)，气固流化床机体(7)右上方设有介质颗粒给料口(11)，气固流化床机体(7)一侧上部设有轻产物排料口(12)，气固流化床机体(7)另一侧下部设有重产物排料口(4)，所述供风装置包括引风管道(1)和布风室(3)，所述引风管道(1)上设置有若干个调节阀(2)，引风管道(1)设置在所述布风室(3)下方，布风室(3)设置在气固流化床机体(7)下方，引风管道(1)通过调节阀(2)与布风室(3)的进风口连通，布风室(3)的出风口与气固流化床机体(7)底部进风口连通，所述料位高度测试装置(5)设置在气固流化床机体(7)外侧壁面上，所述刮板输送机装置(8)设置在气固流化床机体(7)内部，所述的密度测量装置设置在气固流化床机体(7)外部，由相互连接的压力信号采集系统(13)和计算机(14)组成，所述压力信号采集系统(13)设置在气固流化床机体(7)中部分选区域外侧壁面上，所述的除尘装置(9)设置在气固流化床机体(7)的上方，均匀布风、运输浮物、输送沉物、测量料位高度与密度的功能，相互之间互不接触，独立运行。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114700266A (zh) * 2022-04-08 2022-07-05 中国矿业大学 分选密度预测方法及预测模型构建方法和装置
CN114904778A (zh) * 2022-05-31 2022-08-16 中国矿业大学 一种流化床煤炭分选处理装置及方法

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110328140B (zh) * 2019-03-29 2022-03-08 中国矿业大学 提高颗粒流化质量和分选密度稳定性的方法及配套装置
CN111595722A (zh) * 2020-05-15 2020-08-28 中国矿业大学 一种干法重介质流化床密度在线测试装置及方法
CN114950284B (zh) * 2022-05-19 2023-01-10 台州学院 一种气液鼓泡流化床的气体射流优选方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070193926A1 (en) * 2004-10-12 2007-08-23 Ness Mark A Apparatus and method of separating and concentrating organic and/or non-organic material
CN105214956A (zh) * 2015-10-28 2016-01-06 中国矿业大学 一种浓相气固流化床干法分选系统及工艺
CN107233995A (zh) * 2017-07-12 2017-10-10 六盘水师范学院 一种基于床层分板的自介质气固两相流化床干法选煤机
CN110328140A (zh) * 2019-03-29 2019-10-15 中国矿业大学 提高颗粒流化质量和分选密度稳定性的方法及配套装置

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1058203C (zh) * 1996-04-10 2000-11-08 中国矿业大学 用双密度层空气重介流化床进行三产品分选的方法及其装置
CN2475481Y (zh) * 2001-04-17 2002-02-06 中国矿业大学 磁稳定流化床分选装置
CN101590471A (zh) * 2009-06-21 2009-12-02 中国矿业大学 一种自流式气固磁场流化床分选装置及方法
CN102921636B (zh) * 2012-11-07 2015-04-29 中国矿业大学 一种自生介质振动流化床干法分选方法
CN105381950B (zh) * 2015-10-19 2018-06-15 中国矿业大学 一种大型干法重介质流化床分选机及分选系统
CN106622965B (zh) * 2016-12-26 2019-05-14 中国矿业大学 一种矿物梯级干法重介质分选装置及分选方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070193926A1 (en) * 2004-10-12 2007-08-23 Ness Mark A Apparatus and method of separating and concentrating organic and/or non-organic material
CN105214956A (zh) * 2015-10-28 2016-01-06 中国矿业大学 一种浓相气固流化床干法分选系统及工艺
CN107233995A (zh) * 2017-07-12 2017-10-10 六盘水师范学院 一种基于床层分板的自介质气固两相流化床干法选煤机
CN110328140A (zh) * 2019-03-29 2019-10-15 中国矿业大学 提高颗粒流化质量和分选密度稳定性的方法及配套装置

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
TAO, XIUXIANG ET AL.: "Measurement and Control of Density and Height for Gas-Solid Fluidized Bed", JOURNAL OF UNIVERSITY OF SCIENCE AND TECHNOLOGY BEIJING, vol. 24, no. 5, 31 October 2002 (2002-10-31), pages 1 - 4, XP055740427 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114700266A (zh) * 2022-04-08 2022-07-05 中国矿业大学 分选密度预测方法及预测模型构建方法和装置
CN114904778A (zh) * 2022-05-31 2022-08-16 中国矿业大学 一种流化床煤炭分选处理装置及方法
CN114904778B (zh) * 2022-05-31 2023-08-11 中国矿业大学 一种流化床煤炭分选处理装置及方法

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