WO2008044728A1 - Procédé de fabrication de charbon sans cendre - Google Patents

Procédé de fabrication de charbon sans cendre Download PDF

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Publication number
WO2008044728A1
WO2008044728A1 PCT/JP2007/069833 JP2007069833W WO2008044728A1 WO 2008044728 A1 WO2008044728 A1 WO 2008044728A1 JP 2007069833 W JP2007069833 W JP 2007069833W WO 2008044728 A1 WO2008044728 A1 WO 2008044728A1
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Prior art keywords
coal
extraction
solvent
temperature
ashless
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PCT/JP2007/069833
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English (en)
Japanese (ja)
Inventor
Noriyuki Okuyama
Naoji Tada
Atsushi Furuya
Nobuyuki Komatsu
Original Assignee
Kabushiki Kaisha Kobe Seiko Sho
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Application filed by Kabushiki Kaisha Kobe Seiko Sho filed Critical Kabushiki Kaisha Kobe Seiko Sho
Priority to US12/442,966 priority Critical patent/US20100006477A1/en
Priority to KR1020097007353A priority patent/KR101151556B1/ko
Priority to AU2007307596A priority patent/AU2007307596B2/en
Priority to CN2007800321763A priority patent/CN101511977B/zh
Publication of WO2008044728A1 publication Critical patent/WO2008044728A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/06—Methods of shaping, e.g. pelletizing or briquetting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/10—Treating solid fuels to improve their combustion by using additives

Definitions

  • the present invention relates to a method for producing ashless coal, which produces ashless coal used as raw material coal for iron making coatas from coal.
  • bituminous coal, subbituminous coal, lignite, lignite, etc. are used as raw coal, mixed with liquefied oil as a solvent to form a slurry, and this slurry is hydrogenated and liquefied using a catalyst at high temperature and pressure,
  • SRC solvent refined coal
  • caking coal has a tight resource and is expensive, so in particular, non-caking coal, coal such as low-grade lignite and sub-bituminous coal, in other words, poor quality coal.
  • non-caking coal coal such as low-grade lignite and sub-bituminous coal
  • Development and proposals have been made to produce extracted coal with the same characteristics as caking coal using these inferior coals as raw coal and to use it as raw coal for coatas.
  • low-grade coal such as lignite and subbituminous coal is heat treated in a solvent (medium liquid) at a pressure of 1 to 20 MPa and a temperature of 400 ° C or lower, and then the solvent and the heat treated coal are separated to obtain a heat treated coal.
  • a solvent medium liquid
  • a method of using this as a part of the raw coal for coatus is disclosed (for example, see Patent Document 2).
  • the raw coal is N-methyl-2-pyrrolidinone (NMP) solvent alone, or carbon disulfide and N-methyl 2-.
  • NMP N-methyl-2-pyrrolidinone
  • a method for extracting ashless coal from raw coal by contacting with a mixed solvent of pyrrolidinone in the presence of chlorine or a fluorine compound is disclosed (for example, see Patent Document 3).
  • Patent Document 1 JP-A-8-269459 (paragraphs 0010 to 0032)
  • Patent Document 2 Japanese Patent Laid-Open No. 2003-55668 (paragraphs 0017 to 0030)
  • Patent Document 3 Japanese Patent Laid-Open No. 2001-26791 (paragraphs 0009 to 0022)
  • Patent Document 3 The production method described in Patent Document 3 is a method in which a solvent-soluble component is extracted from coal using a strong polar solvent such as NMP without adding hydrogen. When using, the solvent forms a strong bond with the coal, so that the recovery of the solvent is not easy. As a result, the production cost of ashless coal increases.
  • a strong polar solvent such as NMP
  • the present invention has been made in view of the above problems, and an object of the present invention is to produce ashless coal with high efficiency and low cost, and as an excellent quality as raw coal used in iron-making coatas. It is providing the manufacturing method of ashless coal provided with this.
  • the method for producing ashless coal according to the present invention is a method for producing ashless coal used as raw material coal for iron-making coatas, and is a slurry preparation in which a solvent and coal are mixed to prepare a slurry. Extracting the slurry obtained in the step, the slurry preparation step at a temperature of 400 to 420 ° C. for 20 minutes or less, and then cooling to 370 ° C. or less, and the slurry obtained in the extraction step A separation step of separating into a liquid portion and a non-liquid portion, and a modified coal acquisition step of separating the solvent from the liquid portion separated in the separation step to obtain ashless coal that is a modified coal. It is characterized by this.
  • a solvent and coal which is a raw material for ashless coal
  • the slurry obtained in the slurry preparation process is processed under the conditions of a predetermined temperature and time, so that the proportion of coal components extracted to the solvent increases, and this coal component is highly efficient in the solvent. As it is extracted, the resolidification temperature of the resulting ashless coal increases.
  • the separation step the slurry obtained in the extraction step is separated into a liquid part that is a solution containing coal components extracted in a solvent and a non-liquid part that is a slurry containing coal components insoluble in the solvent. The Then, in the modified coal acquisition process, the solvent is separated from the liquid part separated in the separation process, and ashless coal is produced.
  • the solvent in addition to obtaining ashless coal, the solvent is separated from the non-liquid portion separated in the separation step. It is characterized by obtaining by-product coal that is modified coal.
  • the solvent is separated from the non-liquid part separated in the separation step, thereby producing by-product coal. Is done.
  • the slurry obtained in the slurry preparation step is extracted by raising the temperature to a temperature of 400 to 420 ° C, and then immediately 370 It is characterized by cooling to below ° C.
  • the extraction step after the slurry obtained in the slurry preparation step is heated to a predetermined temperature and extracted, the temperature is not maintained and is immediately reduced to 370 ° C or lower. By cooling, the proportion of coal components extracted into the solvent is further increased, and this coal component is extracted into the solvent with higher efficiency.
  • the method for producing ashless coal according to the present invention is characterized in that the coal is inferior quality coal.
  • ashless coal can be produced at a lower cost by using inexpensive inferior quality coal as the raw material for ashless coal.
  • ashless coal used as raw material coal for iron-making coatas can be produced with high efficiency and at low cost.
  • this ashless coal when this ashless coal is blended with the raw coal, the softening and melting properties of this blended coal can be increased, and the amount of expensive caking coal can be suppressed.
  • the strength of iron-coated coatas can be improved by improving the adhesion of blended coal.
  • by-product coal can be produced with high efficiency and at low cost.
  • FIG. 1 is a flowchart for explaining the steps of a method for producing ashless coal.
  • FIG. 2 is a schematic diagram showing a solid-liquid separator for performing a gravity sedimentation method.
  • FIG. 3 is a graph showing a Gieseller curve by a Gieseller softening flow test in Example 1.
  • FIG. 4 is a graph showing the relationship between the extraction temperature when sub-bituminous coal C in Example 2 is used as the raw coal and the extraction process is performed for an extraction time of 1 hour and the resolidification temperature of the obtained ashless coal c.
  • FIG. 5 Sub-bituminous coal C in Example 3 was extracted with a preheater to 370 ° C, 400 ° C and 420 ° C, respectively, and held at the extractor for a predetermined time.
  • 6 is a graph showing the relationship between the extraction time and the extraction rate when extraction processing is performed after rapid cooling.
  • FIG. 1 is a flow chart for explaining the steps of the method for producing ashless coal
  • FIG. 2 is a schematic diagram showing a solid-liquid separation device for performing a gravity sedimentation method.
  • the method for producing ashless coal includes a slurry preparation step (S1), an extraction step (S2), a separation step (S3), and a modified coal acquisition step (S4). .
  • the slurry preparation step (S I) is a step of preparing a slurry by mixing a solvent and coal.
  • the solvent for dissolving coal generally used are monocyclic aromatic compounds such as benzene, toluene and xylene, polar solvents such as N-methylpyrrolidone (NMP) and pyridine, etc.
  • NMP N-methylpyrrolidone
  • non-hydrogen donating solvent mainly composed of 2-ring aromatics.
  • the non-hydrogen-donating solvent is a coal derivative, which is a solvent mainly composed of a bicyclic aromatic and purified mainly from a coal carbonization product.
  • This non-hydrogen-donating solvent is stable even when heated, and has an excellent affinity with coal. Therefore, the proportion of coal components extracted into the solvent (hereinafter also referred to as “extraction rate”) is high. It is a solvent that can be easily recovered by a method such as distillation. The recovered solvent can also be recycled for economic efficiency.
  • the main components of the non-hydrogen-donating solvent include bicyclic aromatic naphthalene, methylnaphthalene, dimethylnaphthalene, trimethylnaphthalene, etc., other naphthalenes having aliphatic side chains, and biphenyls. Includes alkylbenzenes with long aliphatic side chains.
  • the non-hydrogen donating solvent preferably has a boiling point of 180 to 330 ° C. If the boiling point is less than 180 ° C, the required pressure in the extraction step (S2) and separation step (S3) will increase, and the loss due to volatilization will increase in the step of collecting the solvent, resulting in a higher solvent recovery rate. descend. Furthermore, the extraction rate in the extraction step (S2) decreases. On the other hand, when the temperature exceeds 330 ° C., it becomes difficult to separate the solvent from the liquid part and non-liquid part described later, and the solvent recovery rate decreases.
  • Coal used as the raw material for ashless coal (hereinafter also referred to as "raw coal”! /, U) is non-slightly caking coal that has almost no softening and melting property, or lignite coal that is low-grade coal. It is preferable to use poor quality coal such as subbituminous coal. By using inexpensive coal such as these, ashless coal can be produced at a lower cost, thus further improving economic efficiency. However, the coal used is not limited to these inferior coals, and caking coal may be used if necessary.
  • the inferior coal here refers to coal such as non-slightly caking coal, steam coal, low-grade coal (brown coal, subbituminous coal, etc.).
  • Low-grade coal is coal that contains 20% or more moisture and is desired to be dewatered.
  • Examples of such low-grade coal include lignite, lignite, and sub-bituminous coal.
  • brown coal includes Victoria coal, North Dakota coal, Belga coal
  • sub-bituminous coal includes West Banco coal, Binungan coal, and Samarangau coal.
  • the low-grade coal is not limited to those exemplified above, and any coal containing a large amount of water and desired to be dehydrated is included in the low-grade coal referred to in the present invention.
  • the coal concentration relative to the solvent depends on the type of raw coal, but it is 10-50 quality on a dry coal basis. A range of 20% to 35% by mass is more preferable. If the coal concentration relative to the solvent is less than 10% by mass, the proportion of coal components extracted into the solvent will be less than the amount of solvent, which is not economical. On the other hand, the higher the coal concentration, the better. However, if it exceeds 50% by mass, the viscosity of the prepared slurry becomes high, and it becomes difficult to separate the liquid part and the non-liquid part in the slurry transfer and separation step (S3). Cheap.
  • the slurry obtained in the slurry preparation step is extracted at a temperature of 400 to 420 ° C for 20 minutes or less (hereinafter also referred to as “heating”) and then cooled to 370 ° C or less.
  • the heating temperature of the slurry in the extraction step (S2) is in the range of 400 to 420 ° C. If the heating temperature is less than 00 ° C, it will not be sufficient to weaken the bonds between the molecules that make up the coal.If inferior coal is used as the raw coal, the resolidification temperature of the resulting ashless coal will It cannot be increased to the same level as the resolidification temperature of coal. On the other hand, if the temperature exceeds 420 ° C, the thermal decomposition reaction of coal becomes very active, and the generated pyrolytic radicals recombine, resulting in a decrease in the extraction rate.
  • the heating temperature is in the range of 400 to 420 ° C
  • the thermal decomposition reaction proceeds too much
  • the radical polymerization reaction proceeds, and the extraction rate decreases.
  • a relatively high extraction rate is maintained for extraction times of 20 minutes or less.
  • the extraction rate reaches its maximum at an extraction time of 30 minutes or more. After that, even if the extraction time reaches several hours, the extraction rate does not change greatly, but the obtained ash-free coal is recycled. Solidification temperature does not increase. Therefore, to increase the resolidification temperature of the resulting ashless coal and improve the extraction rate, heat it at 400-420 ° C for 20 minutes or less and then cool it to 370 ° C or less. This is the most suitable condition.
  • the lower limit of the cooling temperature is preferably 350 ° C! /. If it is lower than 350 ° C, the solvent's dissolving power will decrease, causing re-precipitation of the extracted coal components, resulting in a decrease in the yield of ashless coal.
  • the lower limit of the extraction time in which the extraction tank can be raised to 400-420 ° C and cooled immediately cannot be determined in general. From an operational point of view, the lower limit of extraction time should be set to 1 minute. That is, in this case, the extraction time is preferably in the range of ! to 20 minutes.
  • immediate cool means to cool by applying a cooling process as quickly as possible.
  • the slurry is cooled by the cooling process as quickly as possible until the slurry moves to the gravity settling tank described later.
  • the extraction rate is higher as the heating time (extraction time) at a temperature of 400 to 420 ° C is shorter. Therefore, in order to further improve the extraction rate, the heating time (extraction time) is 15 minutes. The following is preferable: 10 minutes or less is more preferable, and 5 minutes or less is more preferable. Furthermore, it is more preferable to cool to 370 ° C or less immediately after extracting for 0 minutes, that is, raising the temperature to 400-420 ° C!
  • a temperature close to 400 ° C. is preferably 400 ° C. This is because the closer to 400 ° C, the higher the extraction rate.
  • the pyrolysis of coal produces aromatic-rich components mainly having an average boiling point (Tb50: 50% distillation temperature) of 200-300 ° C, It can be preferably used as a part of the solvent.
  • Tb50 50% distillation temperature
  • the extraction step (S2) is preferably performed in the presence of an inert gas.
  • the inert gas used in the extraction step (S2) is preferably inexpensive nitrogen, but is not particularly limited.
  • the pressure in the extraction step (S2) is preferably 1.0 to 2. OMPa, although it depends on the temperature at the time of extraction and the vapor pressure of the solvent used. When the pressure is lower than the vapor pressure of the solvent, the solvent evaporates and is not trapped in the liquid phase and cannot be extracted. To confine the solvent in the liquid phase, a pressure higher than the vapor pressure of the solvent is required. On the other hand, if the pressure is too high, the cost of the equipment and the operating cost increase, which is not economical.
  • the separation step (S3) is a step of separating the slurry obtained in the extraction step (S2) into a liquid part and a non-liquid part.
  • the liquid part means a solution containing a coal component extracted into a solvent
  • the non-liquid part means a slurry containing a coal component insoluble in the solvent (coal containing ash, that is, ash coal).
  • the method of separating the slurry into the liquid part and the non-liquid part in the separation step (S3) is not particularly limited! /, But it is preferable to use the gravity sedimentation method! /.
  • coal in a slurry slurry preparation tank 1 is mixed with powdered coal, which is a raw material for ashless coal, and a slurry is prepared.
  • Slurry preparation step (Sl) a predetermined amount of slurry is supplied from the coal slurry preparation tank 1 to the preheater 3 by the pump 2, and the slurry is heated to 400 to 420 ° C.
  • the heated slurry is supplied to the extraction tank (extractor) 4 and heated at 400 to 420 ° C for 20 minutes or less while being stirred by the stirrer 10, and then immediately cooled to 370 ° C or less by the cooler 7.
  • Cool extraction step (S2)
  • a cooling mechanism is preferably provided in the extraction tank 4 for immediate cooling.
  • “less than 20 minutes” here is the total heating time in the preheater 3 and the extraction tank 4, and after the preheater 3 starts heating at 400 to 420 ° C. This is the time to immediately cool to below 370 ° C.
  • the slurry subjected to this extraction treatment is supplied to the gravity sedimentation tank 5, and the slurry is separated into a supernatant and a solid concentrate (separation step (S3)), and settled in the lower part of the gravity sedimentation tank 5.
  • the discharged solid content concentrate is discharged to the solid content receiver 6 and Drain a predetermined amount of the supernatant liquid to the filter unit 8.
  • the gravity settling tank 5 is preferably maintained at 350 to 370 ° C, that is, the temperature cooled after the slurry is heated. Moreover, the pressure is preferably in the pressure range of 1.0 to 2 ⁇ OMPa.
  • the time for maintaining the cooled temperature is the time required for separating the slurry into a supernatant and a solid concentrate, and is generally 60 to 120 minutes. There is no particular limitation.
  • the supernatant liquid from which the internal force of the gravity sedimentation tank 5 is also discharged is filtered by the filter unit 8 and collected in the supernatant liquid receiver 9 as necessary.
  • the solvent is separated and recovered from the liquid part and the non-liquid part using a distillation method or the like, and ash-free coal free of ash, which is a modified coal, is obtained from the liquid part.
  • Modified coal acquisition process (S4) If necessary, the power S can be used to obtain by-product coal enriched in ash, which is reformed coal, from the non-liquid part.
  • the modified coal acquisition step (S4) is a step of separating the solvent from the liquid part separated in the separation step (S3) to obtain ashless coal that is a modified coal (ashless coal acquisition step).
  • a method for separating the solvent from the supernatant liquid (liquid part) a general distillation method, an evaporation method (spray drying method, etc.) or the like can be used, and the separated and recovered solvent is a coal slurry preparation tank. Can be used repeatedly by circulating to 1 (see Figure 2). By separating and collecting the solvent, ashless coal substantially free of ash can be obtained from the supernatant.
  • This ashless coal contains almost no ash, has no moisture, and has a higher calorific value than raw coal. Furthermore, the softening and melting properties, which are particularly important qualities as raw materials for iron-making coatas, have been greatly improved, and performance (fluidity) far superior to that of raw coal. Therefore, this ashless coal can be used as a blended coal for raw materials of Kotas. In addition, it can be used as a cocoon coal by mixing with by-product coal. [0044] If necessary, in addition to obtaining ashless coal in the modified coal acquisition step (S4), the solvent is separated from the non-liquid portion separated in the separation step (S3). By-product coal, which is a modified coal, may be manufactured! /, (By-product coal acquisition process).
  • a general distillation method or evaporation method can be used in the same manner as the ashless coal acquisition step described above, and it is separated and recovered.
  • the solvent can be circulated to the coal slurry preparation tank 1 (see Fig. 2) and used repeatedly. By separating and recovering the solvent, by-product charcoal enriched in ash can be obtained from the solid concentrate.
  • this by-product coal contains ash, it has no water and has a sufficient calorific value. Although this is not shown for softening and melting properties, the oxygen-containing functional groups are eliminated, so that when used as a blended coal, the softening and melting properties of other coals contained in this blended coal are inhibited. It is not a thing. Therefore, this by-product coal can be used as part of the blended coal of Cotas raw material, as with ordinary non-coking coal, and it can be used for various fuels without being made of Cotas raw coal. It is also possible.
  • the present invention has the same force as described above.
  • Other steps such as a grinding step, a removal step to remove unnecessary materials such as dust, and a drying step to dry the obtained ashless coal may be included!
  • Example 1 when the extraction temperature in the extraction process is 370 ° C, the softening meltability (softening fluidity), resolidification temperature, etc. of the raw coal and ashless coal obtained from this raw coal The change was examined (Experiment 1).
  • the industrial analysis values and elemental analysis values shown in Table 1 are strong caking coal A, strong caking coal B, and subbituminous coal C as raw coal, and 4 times the amount (20 kg) of solvent per 5 kg of raw coal.
  • (1-me Tilnaphthalene manufactured by Nippon Steel Chemical Co., Ltd.
  • This slurry was pressurized with 1.2 MPa of nitrogen and extracted in an autoclave with an internal volume of 30 L at 370 ° C for 1 hour.
  • This slurry is separated into a supernatant and a solid concentrate in a gravity sedimentation tank maintained at the same temperature and pressure, and the solvent is separated and recovered by the supernatant liquid distillation method.
  • From coal a, strong caking coal B, ashless coal b was obtained, and from subbituminous coal C, ashless coal c was obtained.
  • These industrial analysis values and elemental analysis values are shown in Table 1.
  • ashless coal abc does not contain moisture and has a small ash content compared to raw coal. It can also be seen that the calorific value is higher than that of raw coal.
  • Sub-bituminous coal in C The oxygen concentration is as high as 15% or more, and the ash-free coal is also reduced to about 10%, but it is relatively high! /, Maintaining the oxygen concentration! /.
  • the ashless coal a and b obtained from the strong coking coals A and B are 508 ° C and 488 ° C, respectively. Although it is solidified at a higher temperature than those of strong coking coals A and B, the resolidification temperature of ashless coal c obtained from subbituminous coal C is higher than that of raw bituminous coal C! ° C and relatively low! /.
  • the resulting ashless coal has softening and melting performance superior to that of the raw coal, and should be used as the raw coal for iron-making Kotas. Power of strong coking coal is expensive, so raw material costs cannot be reduced.
  • Example 2 the relationship between the extraction temperature when subbituminous coal C used in Example 1 was extracted and the resolidification temperature of ashless coal c obtained from this subbituminous coal C was examined (experimental).
  • Example 2 the relationship between the extraction temperature when subbituminous coal C used in Example 1 was extracted and the resolidification temperature of ashless coal c obtained from this subbituminous coal C was examined (experimental).
  • Example 2 the relationship between the extraction temperature when subbituminous coal C used in Example 1 was extracted and the resolidification temperature of ashless coal c obtained from this subbituminous coal C was examined (experimental).
  • Example 2 the relationship between the extraction temperature when subbituminous coal C used in Example 1 was extracted and the resolidification temperature of ashless coal c obtained from this subbituminous coal C was examined (experimental).
  • Example 2 the relationship between the extraction temperature when subbituminous coal C used in Example 1 was extracted and the resolidification temperature of ashless coal
  • Figure 4 shows the relationship between the extraction temperature when sub-bituminous coal C is used as the raw coal and the extraction time is 1 hour (60 minutes), and the resolidification temperature of the resulting ashless coal c.
  • the method for obtaining ashless coal was carried out according to Example 1 except for the extraction temperature.
  • the resolidification temperature of ashless coal c increases with an increase in extraction temperature when the extraction temperature exceeds about 360 ° C, and resolidification at an extraction temperature of 400 ° C. It was found that the temperature reached about 490 ° C, which was equivalent to the re-solidification temperature of the strong caking coal. When the temperature exceeded 400 ° C, the resolidification temperature further increased. Therefore, it can be seen that the resolidification temperature of the resulting ashless coal increases by increasing the coal extraction temperature to 400 ° C or higher.
  • Example 3 the relationship between the extraction temperature, extraction time, and extraction rate when the subbituminous coal C used in Example 1 was extracted was examined (Experimental Example 3).
  • FIG. 5 shows the relationship between extraction time and extraction rate.
  • the time and power were raised from 400 ° C to 420 ° C with the preheater. Therefore, Fig. 5 shows the extraction at 400 ° C and at 420 ° C. The time is shown as the time of 8 minutes in the preheater.
  • the method for obtaining ashless coal was carried out in accordance with Example 1 except for the extraction temperature and the extraction time.
  • the extraction rate of coal was obtained by determining the quantity of separated solid by-product coal.
  • raw coal-by-product coal / raw coal X100.
  • the raw coal and by-product coal are based on anhydrous ashless coal.
  • the extraction time is the temperature holding time from when the temperature is raised to a predetermined temperature until the temperature is maintained and cooled to 370 ° C or lower, and the extraction time 0 is the temperature raised to the predetermined temperature. After that, keep the temperature This is the case when it is cooled immediately without holding.
  • the extraction rate is about 52% or higher, it can be said that the extraction rate is relatively high.
  • the extraction temperature is 400 to 420 ° C and the cooling rate is 370 ° C or lower. It can be seen that ashless coal can be obtained with high efficiency if the time force is within 3 ⁇ 40 minutes.
  • the resolidification temperature of ashless coal obtained under the extraction conditions of 400 ° C and 0 minutes was 483 ° C, and was 490 ° C under the extraction conditions of 10 minutes.
  • the resolidification temperature of ashless coal obtained at 420 ° C at 0 minutes was 487 ° C, and at 486 ° C at 22 minutes. Because of this, the resolidification temperature of ashless coal obtained by heating undergrade coal such as subbituminous coal at a temperature of 400 to 420 ° C for 20 minutes or less and then cooling to 370 ° C or less is the above-mentioned strong caking.
  • the resolidification temperature of coal even if added to the raw coal for iron-making Kotas, it does not hinder the fluidity of the strong caking coal contained in the blended coal, but inhibits the fluidity of the entire blended coal X.

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Abstract

L'invention concerne un procédé de fabrication d'un charbon sans cendre destiné à être utilisé en tant que charbon brut pour la fabrication de coke pour la fabrication de l'acier. Le procédé comprend les étapes suivantes: la préparation de boue (S1), suivant laquelle on mélange un solvant et un charbon afin de préparer une boue ; l'extraction (S2), suivant laquelle on extrait la boue produite dans l'étape de préparation de boue (S1) de 400 à 420°C pendant 20 minutes ou moins, puis on refroidit le produit résultant à 370°C ou moins ; la séparation (S3), suivant laquelle on sépare la boue produite à l'étape d'extraction (S2) en une fraction liquide et une fraction non liquide ; et la production de charbon amélioré (S4), suivant laquelle on sépare le solvant de la fraction liquide obtenue dans l'étape de séparation (S3) afin de produire un charbon amélioré, c'est-à-dire un charbon sans cendre.
PCT/JP2007/069833 2006-10-12 2007-10-11 Procédé de fabrication de charbon sans cendre WO2008044728A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US12/442,966 US20100006477A1 (en) 2006-10-12 2007-10-11 Method of producing ashless coal
KR1020097007353A KR101151556B1 (ko) 2006-10-12 2007-10-11 무회탄의 제조 방법
AU2007307596A AU2007307596B2 (en) 2006-10-12 2007-10-11 Method for production of ashless coal
CN2007800321763A CN101511977B (zh) 2006-10-12 2007-10-11 无灰煤的制造方法

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JP2006279034 2006-10-12
JP2006-279034 2006-10-12

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WO2008044728A1 true WO2008044728A1 (fr) 2008-04-17

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WO2010035651A1 (fr) * 2008-09-29 2010-04-01 株式会社神戸製鋼所 Procédé pour la fabrication d’hyper-charbon
US20110179702A1 (en) * 2008-11-07 2011-07-28 Tata Steel Limited Method of Recovery of Organic Solvents Required in Refining of Coal
CN102803136A (zh) * 2009-06-22 2012-11-28 株式会社神户制钢所 炭材料的制造方法
WO2014171460A1 (fr) * 2013-04-16 2014-10-23 株式会社神戸製鋼所 Procédé de production de charbon sans cendre

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JP5679335B2 (ja) 2011-10-13 2015-03-04 株式会社神戸製鋼所 石炭混合燃料及びその燃焼方法
JP5739785B2 (ja) * 2011-10-31 2015-06-24 株式会社神戸製鋼所 残渣炭成形物の製造方法
JP5719283B2 (ja) * 2011-12-01 2015-05-13 株式会社神戸製鋼所 副生炭成形物の製造方法
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JP5852521B2 (ja) 2012-06-29 2016-02-03 株式会社神戸製鋼所 副生炭を主原料とするコークスの製造方法
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WO2010035651A1 (fr) * 2008-09-29 2010-04-01 株式会社神戸製鋼所 Procédé pour la fabrication d’hyper-charbon
KR101246505B1 (ko) 2008-09-29 2013-03-25 가부시키가이샤 고베 세이코쇼 무회탄의 제조 방법
CN102165049B (zh) * 2008-09-29 2013-10-30 株式会社神户制钢所 无灰炭的制造方法
US20110179702A1 (en) * 2008-11-07 2011-07-28 Tata Steel Limited Method of Recovery of Organic Solvents Required in Refining of Coal
US9815026B2 (en) * 2008-11-07 2017-11-14 Tata Steel Limited Method of recovery of organic solvents required in refining of coal
CN102803136A (zh) * 2009-06-22 2012-11-28 株式会社神户制钢所 炭材料的制造方法
WO2014171460A1 (fr) * 2013-04-16 2014-10-23 株式会社神戸製鋼所 Procédé de production de charbon sans cendre
JP2014208722A (ja) * 2013-04-16 2014-11-06 株式会社神戸製鋼所 無灰炭の製造方法
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US10035967B2 (en) 2013-04-16 2018-07-31 Kobe Steel, Ltd. Method for producing ash-free coal

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US20100006477A1 (en) 2010-01-14
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CN101511977B (zh) 2013-06-05
JP4061351B1 (ja) 2008-03-19
CN101511977A (zh) 2009-08-19
JP2008115369A (ja) 2008-05-22
KR20090060339A (ko) 2009-06-11

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