CN113426568B - High-sodium low-rank coal flotation sodium removal method and system - Google Patents
High-sodium low-rank coal flotation sodium removal method and system Download PDFInfo
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- CN113426568B CN113426568B CN202110747176.3A CN202110747176A CN113426568B CN 113426568 B CN113426568 B CN 113426568B CN 202110747176 A CN202110747176 A CN 202110747176A CN 113426568 B CN113426568 B CN 113426568B
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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
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B7/00—Combinations of wet processes or apparatus with other processes or apparatus, e.g. for dressing ores or garbage
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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
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
- B03B9/005—General arrangement of separating plant, e.g. flow sheets specially adapted for coal
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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
- B03D1/018—Mixtures of inorganic and organic compounds
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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
- B03D1/14—Flotation machines
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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
- B03D1/08—Subsequent treatment of concentrated product
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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
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/02—Collectors
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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
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/04—Frothers
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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
- 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
Abstract
The invention discloses a high-sodium low-rank coal flotation sodium removal method and a system, wherein primary flotation is carried out through a primary flotation machine, primary flotation foam products are medium-sodium concentrates, primary flotation residual ore pulp is medium-sodium tailings, and medium-sodium clean coal is obtained after washing and suction filtration are carried out on the primary flotation foam products; and performing secondary flotation on the medium-sodium clean coal through a separation flotation machine, wherein a separation foam product is low-sodium vitrinite concentrate, and the separation residual ore pulp is low-sodium inert-vitrinite tailings. The acetic acid solution is added on the basis of the two-stage flotation process, so that the sodium content of the coal sample can be effectively reduced while the coal rock micro-components are separated by flotation, no harmful waste gas is generated, the acetic acid has little corrosion to production equipment, the service cycle of the equipment is not influenced basically, and the method is safe and green. The method can ensure good flotation enrichment effect and effectively reduce the sodium content in the high-sodium coal, improves the quality of the coal, and has considerable economic benefit.
Description
Technical Field
The invention relates to the technical field of coal sodium removal, in particular to a high-sodium low-rank coal flotation sodium removal method and system.
Background
The high-sodium coal refers to a special coal with high content of alkali metal compounds in the coal, and sodium-based compounds are generally abundant in various alkali metal compounds, so the high-sodium coal is called as the high-sodium coal and has a certain reserve in China, australia, america, germany and the like. The part of the alkali metals such as sodium in the high-sodium coal after combustion exists in the smoke in the form of steam, which easily causes a plurality of problems when the boiler burns the high-sodium coal. Therefore, in order to solve the utilization problem of the high-sodium coal, sodium removal pretreatment is often carried out, acid cleaning pretreatment is an effective method for sodium removal, hydrochloric acid is often used as an acid cleaning solution, the hydrochloric acid can corrode equipment, and the added chloride ions are harmful elements. In addition, the low-rank coal has long and much smoke flame during combustion, high content of inert components, high ignition point and burnout temperature, poor burnout characteristics of the coal and is not beneficial to combustion utilization.
Disclosure of Invention
In order to solve the technical problems, the invention provides a high-sodium low-rank coal flotation sodium removal method and system.
In order to achieve the technical purpose, the invention adopts the following technical scheme:
a high-sodium low-rank coal flotation sodium removal method comprises the following steps:
s1: crushing and grinding the high-sodium low-rank coal into fine-grain raw coal with the particle size of 5-500 mu m;
s2: adding fine raw coal and a sodium-removed solution into a primary separation size mixing barrel to prepare coal slurry, sequentially adding a polar collecting agent and an alcohol foaming agent into the coal slurry, feeding the prepared coal slurry into a primary separation flotation machine for flotation, and respectively collecting primary separation foam products and primary separation residual ore pulp; the primary selection foam product is medium sodium concentrate, and the primary selection residual ore pulp is medium sodium tailings; washing and filtering the primary selected foam product to obtain medium-sodium clean coal;
s3: adding the medium-sodium clean coal and the sodium-removed solution into a separation and size mixing barrel to prepare coal slurry, sequentially adding a non-polar hydrocarbon oil collecting agent and an alcohol foaming agent into the separation and size mixing barrel, feeding the prepared coal slurry into a separation flotation machine for flotation, and respectively collecting separation foam products and separation residual ore pulp; the separated foam product is low-sodium vitrinite concentrate, and the separated residual ore pulp is low-sodium inertinite tailing;
s4: and washing, filtering, drying and cooling the low-sodium vitrinite-rich concentrate and the low-sodium inertinite-rich tailing to obtain the low-sodium vitrinite-rich coal and the low-sodium inertinite-rich coal.
Preferably, the sodium removal solution is 3-5% acetic acid solution, and the temperature of the acetic acid solution is 60-90 ℃.
Preferably, the primary sizing mixing barrel and the sorting sizing mixing barrel can be used for stirring and sizing mixing, and the stirring rotating speed is 1000r/min and 1500r/min respectively.
Preferably, the mass ratio of the sodium-removed solution to the fine-grained raw coal in the coal slurry in the steps S2 and S4 is 5.
Preferably, the carbon chain length of the polar collector is between 8 and 12.
Preferably, the alcoholic foaming agent is sec-octanol or fusel.
Preferably, the drying in step S4 is performed in a forced air drying oven at a temperature of 85 to 95 ℃.
Preferably, the cooling in step S4 is performed under a natural standing condition.
Preferably, the polar collector is n-octanoic acid; the nonpolar hydrocarbon oil collector is kerosene or diesel oil.
A high-sodium low-rank coal flotation sodium removal system comprises: the ore mill, the mill lower part is connected with primary dressing bucket through fine particle raw coal conveyer, primary dressing bucket enters the flotation pulp pipeline through the primary dressing and is connected with the primary dressing flotation machine, the primary dressing flotation machine is equipped with primary dressing tailing discharge pipeline, primary dressing concentrate discharge pipeline, primary dressing flotation machine is connected with the cleaned coal washery bucket through the primary dressing concentrate discharge pipeline, the cleaned coal washery bucket is connected with the concentrate filter through the washed concentrate discharge pipeline, the concentrate filter is connected with the separation bucket through the cleaned coal conveyer, the separation bucket is connected with the separation flotation machine through passing the separation flotation pulp pipeline, the first output end of the separation flotation machine is connected with the minor constituent washery bucket through the separation concentrate discharge pipeline, the minor constituent washery bucket is connected with the minor constituent filter through the washed minor constituent discharge pipeline, the output end of the minor constituent filter is connected with the minor constituent conveyer, the second output end of the separation flotation machine is connected with the inert constituent washery bucket through the separation tailing discharge pipeline, the minor constituent washery bucket is connected with the inert constituent filter through the washed minor constituent discharge pipeline, the inert constituent filter is connected with the inert constituent filter through the inert constituent filter.
Compared with the prior art, the invention has the beneficial effects that:
according to the high-sodium low-rank coal flotation sodium removal method, the acetic acid solution is used for replacing water in the process of preparing coal slurry from a coal sample through flotation, and the acetic acid solution contains hydrogen ions, so that the acetic acid solution has a stronger sodium removal effect compared with water, the temperature during coal slurry stirring is increased, the acetic acid solution is easier to permeate into pores of coal, the contact with sodium components in the coal is more sufficient, and the sodium removal effect is greatly improved. Meanwhile, the acetic acid solution is weakly acidic, so that ash content of the coal sample can be reduced, and the temperature during flotation is increased, so that the activity of the flotation reagent is enhanced, the reagent can be better contacted with the coal sample, the flotability is enhanced, the recovery rate of combustible substances is increased, the ash content is reduced, the separation effect of coal rock micro-components is enhanced, and the enrichment rate of vitrinite and inert matter is improved. Through the flotation sodium removal processes, the low-sodium vitrinite-rich coal and the low-sodium inertinite-rich coal are obtained respectively, the quality and the utilization rate of the high-sodium low-rank coal are improved, the content of alkali metals volatilized in the raw coal combustion process is greatly reduced, the problems of contamination, slag bonding and ash deposition caused by the combustion of the high-sodium coal are well controlled, and therefore the treated high-sodium low-rank coal can be widely utilized.
Drawings
For a clearer explanation of the embodiments or technical solutions of the present invention, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for a person skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 is a flow chart of a high-sodium low-rank coal flotation sodium removal method;
FIG. 2 is a schematic structural diagram of a high-sodium low-rank coal flotation sodium removal system.
In the figure: 1. the system comprises a grinding mill, 2 a fine-grain raw coal conveyor, 3 a primary separation and pulp conditioning barrel, 4 a sodium removal solution, 5 a polar collector, 6 an alcohol foaming agent, 7 a primary separation into a flotation pulp pipeline, 8 a primary separation flotation machine, 9 a primary separation tailing discharge pipeline, 10 a primary separation concentrate discharge pipeline, 11 a clean coal washing barrel, 12 a washing concentrate discharge pipeline, 13 a concentrate filter, 14 a clean coal conveyor, 15 a separation and pulp conditioning barrel, 16 a sodium removal solution, 17 a nonpolar hydrocarbon oil collector, 18 an alcohol collector, 19 a separation into a flotation pulp pipeline, 20 a separation flotation machine, 21 a separation concentrate discharge pipeline, 22 a microscopic group water washing barrel, 23 a water washing microscopic group discharge pipeline, 24 a microscopic group filter, 25 a microscopic group conveyor, 26 a separation tailing discharge pipeline, 27 a microscopic group water washing barrel, 28 a water washing pipeline, 29 an inert group filter, 30 a microscopic group flotation machine and a residual foam product representing a foam product in the flotation machine.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
S1: crushing and grinding the high-sodium low-rank coal into fine-grain raw coal with the particle size of 5-500 mu m;
s2: adding fine-grain raw coal and acetic acid solution with the temperature of 70 ℃ and the concentration of 3% into a primary pulp mixing barrel to prepare coal slurry, wherein the mass ratio of the acetic acid solution to the fine-grain raw coal is 10; the primary selection foam product is medium sodium concentrate, and the primary selection residual ore pulp is medium sodium tailings; washing and filtering the primarily selected foam product to obtain medium-sodium clean coal;
s3: adding medium-sodium clean coal and acetic acid solution with the temperature of 70 ℃ and the concentration of 3% into a separation size mixing barrel to prepare coal slurry, wherein the mass ratio of the acetic acid solution to fine-grain raw coal is 10; the separated foam product is low-sodium vitrinite concentrate, and the separated residual ore pulp is low-sodium inertinite tailing;
s4: washing, filtering, drying and cooling the low-sodium vitrinite-rich concentrate and the low-sodium inertinite-rich tailings to obtain low-sodium vitrinite-rich coal and low-sodium inertinite coal;
s5: steps S1 to S4 were repeated as control experiments using 3% hydrochloric acid solution and deionized water instead of 3% acetic acid solution, respectively.
Through detection, the removal rate of sodium ions by using a 3% acetic acid solution is 63.11%, the yield of flotation clean coal is 70.15%, the ash content is 12.57%, the enrichment rate of vitrinite is 80.67%, and the enrichment rate of inertinite is 55.38%; the sodium ion removal rate of a 3% hydrochloric acid solution is 78.86%, the flotation clean coal yield is 73.25%, the ash content is 11.36%, the vitrinite enrichment rate is 78.35%, and the inertinite enrichment rate is 53.37%; the removal rate of sodium ions by using deionized water is 52.38%, the yield of flotation clean coal is 67.93%, ash content is 14.52%, the enrichment rate of vitrinite is 81.77%, and the enrichment rate of inertinite is 54.27%.
Example 2
S1: crushing and grinding the high-sodium low-rank coal into fine-grain raw coal with the particle size of 5-500 mu m;
s2: adding fine-grain raw coal and 5% acetic acid solution at 90 ℃ into a primary selection size mixing barrel to prepare coal slurry, wherein the mass ratio of the acetic acid solution to the fine-grain raw coal is 10; the primary selection foam product is medium sodium concentrate, and the primary selection residual ore pulp is medium sodium tailings; washing and filtering the primarily selected foam product to obtain medium-sodium clean coal;
s3: adding medium-sodium clean coal and 5% acetic acid solution at 90 ℃ into a separation size mixing barrel to prepare coal slurry, wherein the mass ratio of the acetic acid solution to fine-grain raw coal is 10; the separated foam product is low-sodium vitrinite concentrate, and the separated residual ore pulp is low-sodium inert-vitrinite tailing;
s4: washing, filtering, drying and cooling the low-sodium vitrinite-rich concentrate and the low-sodium inertinite-rich tailing to obtain low-sodium vitrinite-rich coal and low-sodium inertinite-rich coal;
s5: steps S1 to S4 were repeated as control experiments using 5% hydrochloric acid solution and deionized water instead of 5% acetic acid solution, respectively.
Through detection, the sodium ion removal rate of a 5% acetic acid solution is 68.89%, the yield of flotation clean coal is 77.62%, the ash content is 9.38%, the vitrinite enrichment rate is 87.29%, and the inertinite enrichment rate is 60.12%; the sodium ion removal rate of a 5% hydrochloric acid solution is 77.64%, the yield of flotation clean coal is 75.38%, the ash content is 7.78%, the vitrinite enrichment rate is 85.34%, and the inertinite enrichment rate is 58.43%; the removal rate of sodium ions by using deionized water is 63.69%, the yield of flotation clean coal is 74.81%, ash content is 10.59%, the enrichment rate of vitrinite is 88.18%, and the enrichment rate of inertinite is 6.73%.
Example 3
A high-sodium low-rank coal flotation sodium removal system comprises: the ore mill 1, the lower part of the ore mill 1 is connected with a primary separation size mixing barrel 3 through a fine-grain raw coal conveyor 2, the primary separation size mixing barrel 3 is connected with a primary separation flotation machine 8 through a primary separation flotation pulp inlet pipeline 7, the primary separation flotation machine 8 is provided with a primary separation tailing discharge pipeline 9 and a primary separation concentrate discharge pipeline 10, the primary separation flotation machine 8 is connected with a refined coal washing barrel 11 through a primary separation concentrate discharge pipeline 10, the refined coal washing barrel 11 is connected with a concentrate filter 13 through a washed concentrate discharge pipeline 12, the concentrate filter 13 is connected with a separation size mixing barrel 15 through a refined coal conveyor 14, the separation size mixing barrel 15 is connected with a separation flotation machine 20 through a separation flotation pulp inlet pipeline 19, a first output end of the separation flotation machine 20 is connected with a minor constituent washing barrel 22 through a separation concentrate discharge pipeline 21, the minor constituent washing barrel 22 is connected with a minor constituent filter 24 through a washed minor constituent discharge pipeline 23, an output end of the minor constituent washing machine 24 is connected with a minor constituent washing conveyor 25, a second output end of the separation flotation machine 20 is connected with a minor constituent washing barrel 29, and an inert constituent filter 30 is connected with an inert constituent filter 30 through a minor constituent washing barrel 29.
Claims (7)
1. A high-sodium low-rank coal flotation sodium removal method is characterized by comprising the following steps:
s1: crushing and grinding high-sodium low-rank coal into fine-grain raw coal of 5-500 mu m;
s2: adding fine raw coal and a sodium-removed solution into a primary separation size mixing barrel to prepare coal slurry, sequentially adding a polar collecting agent and an alcohol foaming agent into the coal slurry, feeding the prepared coal slurry into a primary separation flotation machine for flotation, and respectively collecting primary separation foam products and primary separation residual ore pulp; the primary selection foam product is medium sodium concentrate, and the primary selection residual ore pulp is medium sodium tailings; washing and filtering the primary selected foam product to obtain medium-sodium clean coal;
s3: adding the medium-sodium clean coal and the sodium-removed solution into a separation and size mixing barrel to prepare coal slurry, sequentially adding a non-polar hydrocarbon oil collecting agent and an alcohol foaming agent into the separation and size mixing barrel, feeding the prepared coal slurry into a separation flotation machine for flotation, and respectively collecting separation foam products and separation residual ore pulp; the separated foam product is low-sodium vitrinite concentrate, and the separated residual ore pulp is low-sodium inertinite tailing;
s4: washing, filtering, drying and cooling the low-sodium vitrinite-rich concentrate and the low-sodium inertinite-rich tailing to obtain low-sodium vitrinite-rich coal and low-sodium inertinite-rich coal;
and S2, the sodium removal solution in the step S3 is an acetic acid solution with the concentration of 3-5%, the temperature of the acetic acid solution is 60-90 ℃, and the mass ratio of the sodium removal solution to the coal is 5-1.
2. The high-sodium low-rank coal flotation sodium removal method according to claim 1, characterized in that: the primary pulp mixing barrel and the sorting pulp mixing barrel can be used for stirring and mixing pulp, and the stirring speed is 1000r/min and 1500r/min respectively.
3. The high-sodium low-rank coal flotation sodium removal method according to claim 1, characterized in that: the carbon chain length of the polar collector is between 8 and 12.
4. The high-sodium low-rank coal flotation sodium removal method according to claim 1, characterized by comprising the following steps: the alcohol foaming agent is sec-octanol or fusel.
5. The high-sodium low-rank coal flotation sodium removal method according to claim 1, characterized in that: the drying in step S4 is performed in a forced air drying oven at a temperature of 85 to 95 ℃.
6. The high-sodium low-rank coal flotation sodium removal method according to claim 1, characterized in that: the cooling in step S4 is performed under a natural standing condition.
7. The high-sodium low-rank coal flotation sodium removal method according to claim 1, characterized in that: the polar collector is n-caprylic acid; the nonpolar hydrocarbon oil collector is kerosene or diesel oil.
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| CN102962122A (en) * | 2012-12-03 | 2013-03-13 | 中国矿业大学 | Deep preparation technology of coal for direct coal liquefacation |
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