WO2017219923A1 - 一种难浮煤泥的分选方法 - Google Patents

一种难浮煤泥的分选方法 Download PDF

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WO2017219923A1
WO2017219923A1 PCT/CN2017/088699 CN2017088699W WO2017219923A1 WO 2017219923 A1 WO2017219923 A1 WO 2017219923A1 CN 2017088699 W CN2017088699 W CN 2017088699W WO 2017219923 A1 WO2017219923 A1 WO 2017219923A1
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parts
flotation
coal
solution
nanobubbles
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French (fr)
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桂夏辉
邢耀文
李臣威
曹亦俊
杨自立
王东岳
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China University of Mining and Technology CUMT
China University of Mining and Technology Beijing CUMTB
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China University of Mining and Technology CUMT
China University of Mining and Technology Beijing CUMTB
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Priority to CA3025832A priority Critical patent/CA3025832C/en
Priority to AU2017282850A priority patent/AU2017282850B2/en
Priority to RU2018146151A priority patent/RU2709877C1/ru
Publication of WO2017219923A1 publication Critical patent/WO2017219923A1/zh
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/008—Organic compounds containing oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/016—Macromolecular compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/02—Collectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/04—Frothers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2203/00—Specified materials treated by the flotation agents; Specified applications
    • B03D2203/02—Ores
    • B03D2203/04—Non-sulfide ores
    • B03D2203/08—Coal ores, fly ash or soot

Definitions

  • the present application relates to a slime sorting technology, and in particular provides a sorting method for difficult to float coal slime.
  • the clean coal is selected; while the less hydrophobic meteorite particles are more difficult to adhere or can be trapped by the bubbles in the slurry but are again returned to the slurry due to foam collapse or foam seepage in the foam phase.
  • high-ash refractory coal slurry is difficult to achieve high-efficiency sorting in the conventional flotation process.
  • due to its poor hydrophobicity it is difficult to be trapped by bubbles in the bubble mineralization process, resulting in loss of clean coal. Due to its high ash content and large fine mud content, it is easy to cause serious pollution to the flotation clean coal on the surface of low-ash coal particles during the pulping process.
  • Performance, etc. such as adding a dispersant to reduce the size of the fine mud on the surface of the coal particles, thereby achieving the purpose of reducing the ash of the clean coal; emulsification of the original agent into the slurry, and further absorption through the further dispersion of the oil droplets
  • the specific surface area of the agent improves the flotation effect; based on the characteristics of the coal slurry itself, the flotation is carried out by means of low-concentration feeding, which has achieved certain effects in improving the sorting efficiency of the non-floating coal slurry, but has not been fundamentally solved.
  • the problem of low efficiency of flotation of difficult-to-float coal slurry Therefore, it is urgent to develop a new sorting technology to make up for the shortcomings of the existing slime sorting technology in the sorting of difficult-to-float coal slime, and to achieve efficient sorting and recovery of difficult-to-float coal slime.
  • the key to the flotation of difficult-to-float coal slurry is the collision and adhesion of particles and bubbles, while the nano-bubbles have the property of preferentially accumulating on the surface of coal particles with better hydrophobicity, which can increase the probability of collision and adhesion of particles with bubbles and reduce shedding. Probability, which significantly increases the recovery rate of difficult coals.
  • the cover function of the fine mud is greatly reduced, and the pollution of the fine coal to the flotation clean coal is effectively alleviated.
  • the present application proposes to introduce bubbles having a diameter of about several tens of nanometers during the flotation process of the difficult-to-float coal slurry, and strengthens the flotation process of the difficult-to-float coal slurry, thereby greatly improving the recovery rate.
  • the purpose of the present application is to provide a method for sorting difficult-to-float coal slurry.
  • nano-bubbles into flotation, the problem of low flotation recovery rate caused by poor hydrophobicity of the difficult-to-float coal slurry is fundamentally solved.
  • a method for sorting difficult-to-float coal slurry comprising the steps of: feeding a nanobubble solution (5) into a slurry mixing tank (F) via a pump (E), and simultaneously adding an appropriate amount of slime (7) and a flotation agent ( 8) In the slurry mixing tank (F), the nanobubbles accumulate on the surface of the particles, greatly improving the hydrophobicity of the coal particles.
  • the slurry (9) is fed into the countercurrent static microbubble flotation column via the feed pump (G). Flotation is carried out in (H), and finally two products of clean coal (10) and tailings (11) are produced.
  • the flotation agent is composed of the following parts by weight: kerosene: 20-80 parts, ethionamide: 5-13 parts, Tween 40: 1-10 parts, fatty alcohol polyoxyethylene ether sodium sulfate: 0.01-0.05 parts, p-toluenesulfonic acid: 0.01-0.07 parts, Span 60: 1-3 parts, phthalic anhydride: 1-3 parts, sodium dodecylbenzenesulfonate: 0.03-0.1 parts , phthalic anhydride: 0.01-0.06 parts.
  • the slime is -325 mesh.
  • the foaming agent is octanol.
  • the nanobubble-containing gas is easily obtained by mixing water (2) and a foaming agent (1) into a mixing tank (A), stirring uniformly, and then passing the mixture (3) through a mixture feeding pump ( B) feeding into the venturi (C), the mixture dissolves the air under the negative pressure generated by the jet and generates a large number of bubbles at the end of the venturi (C), and the bubble-containing solution (4) is fed into the defoaming bucket (D)
  • a baffle is installed in the middle of the bubble tank (D), and the baffle is divided into two parts.
  • the two parts which are divided into the barrel are only connected to the lower part, and the nanobubbles are injected with the solution from the upper part of the side of the defoaming barrel, and the lower communication channel is connected.
  • the large bubbles in the mixture rise to the top of the defoaming bucket under buoyancy and gradually rupture, so that the bubbles generated by the venturi (C) pass through the defoaming bucket (D) After the large bubbles are removed, leaving the nanobubbles in solution.
  • the defoaming bucket (D) is installed with a baffle in the middle of the conventional drum, and is divided into two parts, the two parts of the barrel are divided into only the lower part, and the nanobubbles are separated from the solution by the defoaming barrel.
  • the upper part of the side is injected, and the lower communication passage enters the other side of the defoaming bucket (D).
  • the ratio of the water and the foaming agent is 0.01-0.1 g of foaming agent per liter of water;
  • the ratio of liquid, slime and flotation agent is 60-90 g dry coal slurry and 0.01-0.04 g flotation agent per liter of nanobubble solution.
  • the flotation agent is composed of the following parts by weight: kerosene: 76 parts, ethionyl ester: 9 parts, Tween 40: 7 parts, fatty alcohol polyoxyethylene ether sodium sulfate: 0.03 parts, Methylbenzenesulfonic acid: 0.02 parts, Span 60: 2.1 parts, phthalic anhydride: 1.6 parts, sodium dodecylbenzenesulfonate: 0.07 parts, phthalic anhydride: 0.03 parts.
  • the flotation reagent is composed of the following parts by weight: kerosene: 48 parts, ethionyl ester: 9 parts, Tween 40: 3 parts, fatty alcohol polyoxyethylene ether sulfate: 0.045 parts, Methylbenzenesulfonic acid: 0.046 parts, Span 60: 2.6 parts, phthalic anhydride: 1.7 parts, sodium dodecylbenzenesulfonate: 0.067 parts, phthalic anhydride: 0.022 parts.
  • the ratio of the water and the foaming agent is 0.016 g of foaming agent per liter of water; the ratio of the nanobubble solution, the slime, and the flotation agent is 80 g of dry coal slurry per liter of the nanobubble solution, and 0.024 g of floatation is added.
  • the present application overcomes the deficiencies of the traditional difficult-to-float coal slurry sorting technology, and proposes a sorting method based on nanobubbles for difficult-to-floating coal slime, which utilizes the characteristics of nanobubbles preferentially on the hydrophobic surface area to expand the low-ash ash.
  • the difference in hydrophobicity between the granules and the high ash vermiculite solves the problem that the poorly floating coal slime has poor selectivity, high drug consumption, low recovery rate, and easy to exceed the standard of clean coal ash.
  • the application has the following advantages:
  • the sorting method proposed in the present application has novel and unique ideas for improving the flotation of difficult-to-float coal slime, and solves the problem of low efficiency of the traditional froth flotation, and is of great significance for the realization of the efficient sorting process of difficult-to-float coal slime.
  • the application optimizes the sorting reagents, especially the design of the flotation reagent, the content ratio, the flotation of the difficult-to-float coal slurry, the improvement of the efficiency, and the effect is better than the traditional flotation reagent.
  • the application adopts a specially designed defoaming bucket, which is easy to generate a large amount of nano bubbles.
  • the device seems simple, but the efficiency of removing large bubbles is high, and the production efficiency is improved.
  • the sorting method and apparatus proposed in the present application are simple, have low investment, low operating cost, and significant economic benefits.
  • Figure 1 is a schematic representation of the application.
  • water (2) and octanol foaming agent (1) are mixed into a mixing tank (A), and the ratio of water and foaming agent is 0.07 g of foaming agent per liter of water, and the mixture is evenly stirred.
  • the mixture (3) is fed into the venturi tube (C) through the mixture feed pump (B), the mixture dissolves the air under the negative pressure generated by the jet and generates a large number of bubbles at the end of the venturi tube (C), containing the bubble solution ( 4)
  • the slurry mixing tank (F) On the right side of the bubble tank (D), the large bubbles in the mixture rise to the top of the bubble removal tank under buoyancy and gradually rupture, so that the bubbles generated by the venturi tube (C) pass through the bubble removal tank (D) and the large bubbles It is removed, leaving the nanobubbles in solution, and the nanobubble containing solution (5) is fed into the slurry mixing tank (F) via the pump (E) while the appropriate amount of -325 mesh slime (7) and flotation reagent ( 8)
  • the ratio of nanobubble solution, slime and flotation agent is 77g dry coal slurry per liter of nanobubble solution, 0.018g flotation agent,
  • the rice bubbles accumulate on the surface of the particles, greatly improving the hydrophobicity of the coal particles.
  • the slurry (9) is fed into the countercurrent static microbubble flotation column (H) via the feed pump (G) for flotation, and finally the clean coal is produced. (10) and tailings (1
  • the flotation reagent is composed of the following parts by weight: kerosene: 55 parts, ethionyl ester: 8.6 parts, Tween 40: 5.6 parts, fatty alcohol polyoxyethylene ether sulfate: 0.027 parts, p-toluene Sulfonic acid: 0.033 parts, Span 60: 2.68 parts, phthalic anhydride: 2.6 parts, sodium dodecylbenzenesulfonate: 0.055 parts, phthalic anhydride: 0.04 parts.
  • water (2) and octanol (1) are mixed into a mixing tank (A), and the ratio of water and foaming agent is 0.033 g of foaming agent per liter of water, and the mixture is stirred uniformly (3).
  • the mixture pump (B) into the venturi tube (C) the mixture dissolves the air under the negative pressure generated by the jet and generates a large number of bubbles at the end of the venturi tube (C), containing the bubble solution (4)
  • the nanobubbles enter the right side of the defoaming barrel (D) with the solution from the lower communication channel, and the large bubbles in the mixture rise under buoyancy. Floats to the top of the defoaming bucket and gradually ruptures, so that the bubbles generated by the venturi (C) are removed by the defoaming bucket (D), leaving the nanobubbles in solution, containing the nanobubble solution (5)
  • the pump (E) is fed into the slurry mixing tank (F), and the -325 mesh slime (7) and flotation agent (8) are fed into the slurry mixing tank (F), nanobubble solution, slime, flotation
  • the ratio of the medicament is 80g dry coal slurry and 0.027g flotation agent per liter of nanobubble solution, and the nanobubbles accumulate on the surface of the particles, which greatly improves the hydrophobicity of the coal particles.
  • the slurry (9) is fed through the feed pump (G). Feeding into the countercurrent static microbubble flotation
  • the flotation reagent is composed of the following parts by weight: kerosene: 65 parts, ethionamide: 5.65 parts, Tween 40: 2.2 parts, fatty alcohol polyoxyethylene ether sulfate: 0.026 parts, p-toluene Sulfonic acid: 0.044 parts, Span 60: 1.26 parts, phthalic anhydride: 2.1 parts, sodium dodecylbenzenesulfonate: 0.034 parts, phthalic anhydride: 0.026 parts.

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  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Treatment Of Sludge (AREA)

Abstract

一种难浮煤泥的分选方法，包括以下步驟：含纳米气泡溶液(5)经泵(E)给入矿浆搅拌桶(F)，同时将适量的煤泥(7)和浮选药剂(8)给入矿浆搅拌桶(F)中，调浆后矿浆(9)经给料泵(G)给入逆流静态微泡浮选柱(H)中进行浮选，最终产生精煤(10)及尾煤(11)两种产品，所述浮选药剂由下述物质组成：煤油，乙硫氨酯，吐温40，脂肪醇聚氧乙烯醚硫酸钠，对甲基苯磺酸，司盘60，邻苯二甲酸酐，十二烷基苯磺酸钠，苯酐。该方法的有益效果是利用纳米气泡优先在疏水性表面积聚的特点，拉大精煤与矸石的疏水性差异，纳米气泡的积聚也大大减弱了细泥在煤颗粒表面的罩盖作用，显著降低了细泥的污染、提高了精煤的回收率。

Description

一种难浮煤泥的分选方法 技术领域
本申请涉及一种煤泥分选技术，特别提供了一种难浮煤泥的分选方法。
背景技术
随着我国采煤机械化程度的提高、资源地质条件的恶化、选煤厂大型化建设及重介质分选技术的广泛应用，高灰难选煤泥比例急剧增加，并呈现继续恶化趋势，煤泥分选的矛盾更加突出。目前浮选是处理煤泥最主要的手段之一，在常规的浮选过程中，疏水性较好的煤颗粒与气泡发生碰撞粘附在气泡上，并随气泡升浮至泡沫相最终成为浮选精煤；而疏水性较差的矸石颗粒由于其较难以粘附或者在矿浆中能被气泡捕获但在泡沫相中又由于泡沫的破裂或者泡沫渗流等因素再次返回到矿浆中。但高灰难选煤泥在常规的浮选过程中难以实现高效分选，一方面由于其疏水性较差，在气泡矿化过程中较难以被气泡捕获而造成精煤的损失，另一方面由于其灰分较高，细泥含量大，极易在调浆过程中罩盖在低灰的煤颗粒表面对浮选精煤造成严重的污染。
针对难浮煤泥浮选效率低下的难题，国内外的不少专家学者做了很多有益的探索，这些工作大致归结于新型药剂的开发、现有的分选工艺的改进以及提高设备的分选性能等几方面，例如添加分散剂等降低细泥在煤颗粒表面的罩盖，从而达到降低精煤灰分的目的；将原有药剂乳化后加入矿浆中，通过油滴的进一步分散增大捕收剂的比表面积从而改善浮选效果；基于煤泥自身特点，以低浓度入料的方式浮选等，这在改善难浮煤泥分选效率方面取得了一定的效果，但是未从根本上解决难浮煤泥浮选效率低下的问题。因此亟需开发一种新的分选技术以弥补现有的煤泥分选技术在难浮煤泥分选方面的不足，实现难浮煤泥的高效分选回收。
难浮煤泥浮选的关键是颗粒与气泡的碰撞与粘附，而纳米气泡具有优先在较好疏水性的煤颗粒表面积聚的特性，这可以提高颗粒与气泡碰撞与附着的概率并减少脱落概率，从而显著提高难浮煤泥的回收率。此外，由于纳米气泡在煤颗粒表面的覆盖，细泥的罩盖作用也大大减弱，有效减轻了细泥对浮选精煤的污染。 基于此，本申请提出了在难浮煤泥的浮选过程中引入直径约为几十纳米的气泡，强化了难浮煤泥的浮选过程，大大提高了其回收率。
发明内容
本申请的目的在于提供了一种难浮煤泥的分选方法，通过将纳米气泡引入浮选，从根本上解决了难浮煤泥疏水性差导致的浮选回收率低的问题。
本申请的技术方案是：
一种难浮煤泥的分选方法，包括以下步骤：含纳米气泡溶液(5)经泵(E)给入矿浆搅拌桶(F)，同时将适量的煤泥(7)和浮选药剂(8)给入矿浆搅拌桶(F)中，纳米气泡积聚在颗粒表面，大大提高煤颗粒的疏水性，调浆后矿浆(9)经给料泵(G)给入逆流静态微泡浮选柱(H)中进行浮选，最终产生精煤(10)及尾煤(11)两种产品。，所述浮选药剂由下述重量份的物质组成：煤油：20～80份，乙硫氨酯：5-13份，吐温40：1-10份，脂肪醇聚氧乙烯醚硫酸钠：0.01-0.05份，对甲基苯磺酸：0.01-0.07份，司盘60：1-3份，邻苯二甲酸酐：1-3份，十二烷基苯磺酸钠：0.03-0.1份，苯酐：0.01-0.06份。
进一步地，所述煤泥为-325网目。
进一步地，所述起泡剂为仲辛醇。
进一步地，所述含纳米气泡容易由以下步骤制得：将水(2)与起泡剂(1)给入搅拌桶(A)中混合，搅拌均匀后混合物(3)通过混合物给料泵(B)给入文丘里管(C)，混合物在射流产生的负压作用下溶解空气并在文丘里管(C)尾端产生大量气泡，含气泡溶液(4)给入除泡桶(D)的上部，除泡桶(D)中间安装有一挡板，将其分成两部分，桶被分成的两部分只有下部连通，纳米气泡随溶液由除泡桶的一侧的上部注入，由下部连通通道进入除泡桶(D)的另一侧，混合物中的大气泡在浮力作用下升浮至除泡桶上部并逐渐破裂，这样经过文丘里管(C)产生的气泡经除泡桶(D)后大气泡被除去，留下纳米气泡在溶液中。
进一步地，所述的除泡桶(D)是在常规的圆桶中间安装有一挡板，将其分成两部分，桶被分成的两部分只有下部连通，纳米气泡随溶液由除泡桶的一侧的上部注入，由下部连通通道进入除泡桶(D)另一侧。
进一步地，所述水和起泡剂的配比为每升水0.01-0.1g起泡剂；纳米气泡溶 液、煤泥、浮选药剂的配比为每升纳米气泡溶液添加60-90g干煤泥、0.01-0.04g浮选药剂。
进一步地，所述浮选药剂由下述重量份的物质组成：煤油：76份，乙硫氨酯：9份，吐温40：7份，脂肪醇聚氧乙烯醚硫酸钠：0.03份，对甲基苯磺酸：0.02份，司盘60：2.1份，邻苯二甲酸酐：1.6份，十二烷基苯磺酸钠：0.07份，苯酐：0.03份。
进一步地，所述浮选药剂由下述重量份的物质组成：煤油：48份，乙硫氨酯：9份，吐温40：3份，脂肪醇聚氧乙烯醚硫酸钠：0.045份，对甲基苯磺酸：0.046份，司盘60：2.6份，邻苯二甲酸酐：1.7份，十二烷基苯磺酸钠：0.067份，苯酐：0.022份。
进一步地，所述水和起泡剂的配比为每升水0.016g起泡剂；纳米气泡溶液、煤泥、浮选药剂的配比为每升纳米气泡溶液添加80g干煤泥、0.024g浮选药剂。
本申请克服了传统的难浮煤泥的分选技术的不足，提出了一种基于纳米气泡的难浮煤泥的分选方法，利用纳米气泡优先在疏水性表面积聚的特点，拉大低灰颗粒与高灰矸石的疏水性差异，解决了难浮煤泥在浮选中选择性差、药耗大、回收率较低、精煤灰分容易超标的问题。除此之外，本申请还有以下优点：
本申请提出的分选方法提高难浮煤泥浮选选择性思路新颖独特，解决了传统的泡沫浮选中效率低的难题，对难浮煤泥高效分选过程的实现意义重大。
本申请对分选的试剂进行了优化，尤其是浮选药剂的设计，含量配比，对难浮煤泥易于浮选，提高效率，明显比传统浮选试剂效果好。
本申请采用了特殊设计的除泡桶，产生大量纳米气泡容易，该设备看似简单，但对于去除大气泡的效率高，提高了生产效率。
总之，本申请提出的分选方法以及装置，简单、投资少、运行费用低，经济效益显著。
附图说明
图1是本申请示意图。
图中：1-起泡剂，2-水，3-起泡剂与水混合物，4-气泡混合物，5、6-含纳米气泡溶液，7-煤泥，8-浮选药剂，9-调浆后矿浆，10-浮选精煤，11-浮选尾煤， A-搅拌桶，B-混合物给料泵，C-文丘里管，D-自制除大泡桶，E-纳米气泡溶液给料泵，F-矿浆搅拌桶，G-矿浆给料泵，H-浮选柱。
具体实施方式
下面结合附图来具体描述本申请的优选实施例，其中，附图构成本申请一部分，并与本申请的实施例一起用于阐释本申请的原理。
实施例1
如图1，将水(2)与仲辛醇起泡剂(1)给入搅拌桶(A)中混合，水和起泡剂的配比为每升水0.07g起泡剂，搅拌均匀后的混合物(3)通过混合物给料泵(B)给入文丘里管(C)，混合物在射流产生的负压作用下溶解空气并在文丘里管(C)尾端产生大量气泡，含气泡溶液(4)给入除泡桶(D)的上部，除泡桶(D)中间安装有一挡板，将其分成两部分，桶被分成的两部分只有下部连通，纳米气泡随溶液由下部连通通道进入除泡桶(D)右侧，混合物中的大气泡在浮力作用下升浮至除泡桶上部并逐渐破裂，这样经过文丘里管(C)产生的气泡经除泡桶(D)后大气泡被除去，留下纳米气泡在溶液中，含纳米气泡溶液(5)经泵(E)给入矿浆搅拌桶(F)，同时将适量的-325网目煤泥(7)和浮选药剂(8)给入矿浆搅拌桶(F)中，纳米气泡溶液、煤泥、浮选药剂的配比为每升纳米气泡溶液添加77g干煤泥、0.018g浮选药剂，纳米气泡积聚在颗粒表面，大大提高煤颗粒的疏水性，调浆后矿浆(9)经给料泵(G)给入逆流静态微泡浮选柱(H)中进行浮选，最终产生精煤(10)及尾煤(11)两种产品；
所述浮选药剂由下述重量份的物质组成：煤油：55份，乙硫氨酯：8.6份，吐温40：5.6份，脂肪醇聚氧乙烯醚硫酸钠：0.027份，对甲基苯磺酸：0.033份，司盘60：2.68份，邻苯二甲酸酐：2.6份，十二烷基苯磺酸钠：0.055份，苯酐：0.04份。
实施例2
如图1，将水(2)与仲辛醇(1)给入搅拌桶(A)中混合，水和起泡剂的配比为每升水0.033g起泡剂，搅拌均匀后的混合物(3)通过混合物给料泵(B)给入文丘里管(C)，混合物在射流产生的负压作用下溶解空气并在文丘里管(C)尾端产生大量气泡，含气泡溶液(4)给入除泡桶(D)的上部，除泡桶(D)中 间安装有一挡板，将其分成两部分，桶被分成的两部分只有下部连通，纳米气泡随溶液由下部连通通道进入除泡桶(D)右侧，混合物中的大气泡在浮力作用下升浮至除泡桶上部并逐渐破裂，这样经过文丘里管(C)产生的气泡经除泡桶(D)后大气泡被除去，留下纳米气泡在溶液中，含纳米气泡溶液(5)经泵(E)给入矿浆搅拌桶(F)，同时将-325网目煤泥(7)和浮选药剂(8)给入矿浆搅拌桶(F)中，纳米气泡溶液、煤泥、浮选药剂的配比为每升纳米气泡溶液添加80g干煤泥、0.027g浮选药剂，纳米气泡积聚在颗粒表面，大大提高煤颗粒的疏水性，调浆后矿浆(9)经给料泵(G)给入逆流静态微泡浮选柱(H)中进行浮选，最终产生精煤(10)及尾煤(11)两种产品；
所述浮选药剂由下述重量份的物质组成：煤油：65份，乙硫氨酯：5.65份，吐温40:2.2份，脂肪醇聚氧乙烯醚硫酸钠：0.026份，对甲基苯磺酸：0.044份，司盘60：1.26份，邻苯二甲酸酐：2.1份，十二烷基苯磺酸钠：0.034份，苯酐：0.026份。
以上所述，仅为本申请较佳的具体实施方式，但本申请的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本申请揭露的技术范围内，可轻易想到的变化或替换，都应涵盖在本申请的保护范围之内。

Claims (9)

  1. 一种难浮煤泥的分选方法，其特征在于，包括以下步骤：含纳米气泡溶液(5)经泵(E)给入矿浆搅拌桶(F)，同时将适量的煤泥(7)和浮选药剂(8)给入矿浆搅拌桶(F)中，纳米气泡积聚在颗粒表面，大大提高煤颗粒的疏水性，调浆后矿浆(9)经给料泵(G)给入逆流静态微泡浮选柱(H)中进行浮选，最终产生精煤(10)及尾煤(11)两种产品，所述浮选药剂由下述重量份的物质组成：煤油：20～80份，乙硫氨酯：5-13份，吐温40：1-10份，脂肪醇聚氧乙烯醚硫酸钠：0.01-0.05份，对甲基苯磺酸：0.01-0.07份，司盘60：1-3份，邻苯二甲酸酐：1-3份，十二烷基苯磺酸钠：0.03-0.1份，苯酐：0.01-0.06份。
  2. 如权利要求1所述的方法，其特征在于：所述煤泥为-325网目。
  3. 如权利要求2或3所述的方法，其特征在于：所述起泡剂为仲辛醇。
  4. 如权利要求2所述的方法，其特征在于：所述含纳米气泡溶液由以下步骤制得：将水(2)与起泡剂(1)给入搅拌桶(A)中混合，搅拌均匀后混合物(3)通过混合物给料泵(B)给入文丘里管(C)，混合物在射流产生的负压作用下溶解空气并在文丘里管(C)尾端产生大量气泡，含气泡溶液(4)给入除泡桶(D)的上部，除泡桶(D)中间安装有一挡板，将其分成两部分，桶被分成的两部分只有下部连通，纳米气泡随溶液由除泡桶的一侧的上部注入，由下部连通通道进入除泡桶(D)的另一侧，混合物中的大气泡在浮力作用下升浮至除泡桶上部并逐渐破裂，这样经过文丘里管(C)产生的气泡经除泡桶(D)后大气泡被除去，留下纳米气泡在溶液中。
  5. 如权利要求4所述的方法，其特征在于：所述的除泡桶(D)是在常规的圆桶中间安装有一挡板，将其分成两部分，桶被分成的两部分只有下部连通，纳米气泡随溶液由除泡桶的一侧的上部注入，由下部连通通道进入除泡桶(D)另一侧。
  6. 如权利要求4所述的方法，其特征在于：所述水和起泡剂的配比为每升水0.01-0.1g起泡剂；纳米气泡溶液、煤泥、浮选药剂的配比为每升纳米气泡溶液添加60-90g干煤泥、0.01-0.04g浮选药剂。
  7. 如权利要求1所述的方法，其特征在于：所述浮选药剂由下述重量份的物质组成：煤油：76份，乙硫氨酯：9份，吐温40：7份，脂肪醇聚氧乙烯醚硫酸 钠：0.03份，对甲基苯磺酸：0.02份，司盘60：2.1份，邻苯二甲酸酐：1.6份，十二烷基苯磺酸钠：0.07份，苯酐：0.03份。
  8. 如权利要求1所述的方法，其特征在于：所述浮选药剂由下述重量份的物质组成：煤油：48份，乙硫氨酯：9份，吐温40：3份，脂肪醇聚氧乙烯醚硫酸钠：0.045份，对甲基苯磺酸：0.046份，司盘60：2.6份，邻苯二甲酸酐：1.7份，十二烷基苯磺酸钠：0.067份，苯酐：0.022份。
  9. 如权利要求6所述的方法，其特征在于：所述水和起泡剂的配比为每升水0.016g起泡剂；纳米气泡溶液、煤泥、浮选药剂的配比为每升纳米气泡溶液添加80g干煤泥、0.024g浮选药剂。
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