WO2013099650A1 - 無灰炭の製造方法 - Google Patents
無灰炭の製造方法 Download PDFInfo
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- WO2013099650A1 WO2013099650A1 PCT/JP2012/082452 JP2012082452W WO2013099650A1 WO 2013099650 A1 WO2013099650 A1 WO 2013099650A1 JP 2012082452 W JP2012082452 W JP 2012082452W WO 2013099650 A1 WO2013099650 A1 WO 2013099650A1
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- ashless coal
- coal
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- separating
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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
- C10L5/00—Solid fuels
- C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
- C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
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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
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/08—Drying or removing water
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/24—Mixing, stirring of fuel components
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/48—Expanders, e.g. throttles or flash tanks
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/544—Extraction for separating fractions, components or impurities during preparation or upgrading of a fuel
Definitions
- the present invention relates to a method for producing ashless coal for obtaining ashless coal from which ash has been removed from coal.
- Patent Document 1 As a method for producing ashless coal, for example, there is one described in Patent Document 1.
- coal and a solvent are mixed to prepare a slurry, and the resulting slurry is heated to extract a coal component soluble in the solvent (hereinafter, solvent-soluble component)
- solvent-soluble component a coal component soluble in the solvent
- the slurry from which soluble components have been extracted is separated into a solution portion containing solvent-soluble components and a solid concentrate containing a coal component insoluble in the solvent (hereinafter, solvent-insoluble components), and the solvent portion is separated from the separated solution portion.
- Ashless coal is obtained by separating and recovering The solvent separated and recovered from the solution part is stored in the solvent tank and reused.
- a spray drying method is used as a method for obtaining ashless coal by separating and recovering the solvent from the solution portion.
- organic substances and inorganic substances in ashless coal are separated and deposited, and fine inorganic substances mixed in a small amount in a solution containing solvent-soluble components and removal of metal components dissolved in the solvent are removed. Becomes easy.
- the amount of solvent to be evaporated increases when the weight ratio of the solvent contained in the solution part is large, and the solvent is sufficiently separated from the solution part. ⁇ There is a possibility that it cannot be collected. In that case, it is necessary to add a new solvent to the ashless coal production apparatus by the amount of the solvent remaining in the ashless coal that cannot be separated and recovered, which increases the production cost of the ashless coal.
- a method in which a plurality of steps for separating and recovering the solvent are provided and the solvent is recovered in a plurality of times For example, a method of simply separating and collecting the solvent remaining in the ashless coal from the ashless coal obtained by separating and collecting the solvent by the spray drying method may be considered.
- the ashless coal obtained by using the spray drying method is granular (solid), there is a problem that handling properties when transferring the ashless coal to the next separation tank are poor.
- the handling property refers to the ease of handling of ashless coal, and if it can be handled by liquid (if ashless coal can be handled in a liquid state), it can be easily handled.
- Ashless charcoal is usually solid at room temperature, fluidity increases with increasing temperature and liquid handling becomes possible.
- the conventional method for producing ashless coal for example, the spray drying method of Patent Document 1
- the residual ratio of the solvent remaining in the ashless coal is, for example, 0 to 2 wt%. Has a high softening start temperature. Therefore, the liquid cannot be handled unless the temperature is raised to a considerable temperature (for example, 380 ° C.), and the handling property is poor. Therefore, when transferring the ashless coal obtained by the spray drying method to the next separation tank, the ashless coal must be transferred in a solid state with poor handling properties.
- This invention is made
- the objective provides the manufacturing method of ashless coal which can improve a solvent recovery rate and can manufacture ashless coal efficiently. That is.
- the method for producing ashless coal of the present invention includes an extraction step of heating a slurry obtained by mixing coal and a solvent to extract a coal component soluble in the solvent, and the extraction step A separation step of separating the solution portion containing the coal component from the slurry from which the coal component is extracted, and an ashless coal that separates and recovers the solvent from the solution portion separated in the separation step to obtain ashless coal
- An ashless coal obtaining step wherein the ashless coal obtaining step reduces the pressure to a pressure lower than the vapor pressure of the solvent, thereby evaporating and separating the solvent from the solution portion to obtain solid ashless coal; and And heating the solid ashless coal obtained in the decompression step to evaporate and separate the solvent remaining in the ashless coal.
- the manufacturing method of the ashless coal of this invention is the extraction process which extracts the coal component soluble in a solvent by heating the slurry obtained by mixing coal and a solvent, A separation step of separating the solution portion containing the coal component from the slurry from which the coal component has been extracted in the extraction step; and a step of separating and recovering the solvent from the solution portion separated in the separation step to obtain ashless coal
- An ash charcoal acquisition step wherein the ashless charcoal acquisition step includes a first evaporation step for evaporating and separating the solvent from the solution portion, and an ashless coal obtained by evaporating and separating the solvent in the first evaporation step.
- the liquid ashless charcoal is in a liquid state and the second And wherein the transferring to the calling process.
- the solvent recovery rate can be improved and ashless coal can be produced efficiently.
- FIG. 1 It is the schematic which shows the manufacturing apparatus of the ashless coal which concerns on 1st Embodiment of this invention. It is the schematic of the steam tube dryer used for the manufacturing apparatus of ashless coal shown in FIG. 1, (a) is a front view, (b) is AA sectional drawing of (a). It is a graph which shows the measurement result of a solvent residual rate. It is the schematic which shows the ashless coal manufacturing apparatus which concerns on 2nd Embodiment of this invention.
- FIG. 1 is a schematic view showing an ashless coal production apparatus 1 according to the first embodiment of the present invention.
- the ashless coal manufacturing apparatus 1 of the present embodiment mixes a coal hopper 2 for storing and cutting coal, a solvent tank 3 for storing a solvent, and coal and a solvent to mix slurry.
- a solvent capable Gravity sedimentation tank 8 that separates the slurry from which the soluble component has been extracted into a solution portion (supernatant liquid) containing a solvent-soluble
- the manufacturing method of ashless coal of this embodiment has an extraction process, a separation process, and an ashless coal acquisition process.
- Bituminous coal with a high extraction rate ashless coal recovery rate
- cheaper inferior quality coal subbituminous coal, lignite
- the extraction step is a step of extracting a solvent-soluble component by heating a slurry obtained by mixing coal and a solvent.
- this extraction step includes a slurry preparation step of preparing a slurry by mixing coal and a solvent, and a solvent soluble component of extracting the solvent soluble component by heating the slurry obtained in the slurry preparation step. It is divided into the component extraction process.
- the solvent-soluble component is a coal component that can be dissolved in the solvent by extracting the coal with the solvent, and is derived from an organic component in the coal that has a relatively small molecular weight and has not developed a crosslinked structure. To do.
- 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 in a heated state and has an excellent affinity for coal. Therefore, the ratio of the soluble component (herein, the coal component) extracted into the solvent is high (hereinafter also referred to as the extraction rate), and the solvent can be easily recovered by a method such as distillation.
- the main component of the non-hydrogen donating solvent include naphthalene, methylnaphthalene, dimethylnaphthalene, and trimethylnaphthalene, which are bicyclic aromatics.
- non-hydrogen donating solvent examples include naphthalenes having an aliphatic side chain, anthracenes, fluorenes, and biphenyl and alkylbenzene having a long chain aliphatic side chain.
- a non-hydrogen donating compound is used as a solvent.
- a hydrogen donating compound including coal liquefied oil
- tetralin may be used as a solvent.
- boiling point of the solvent is not particularly limited, from the viewpoint of pressure reduction in the extraction step and separation step, extraction rate in the extraction step, solvent recovery rate in the ashless coal acquisition step, etc., for example, A solvent having a boiling point of 180 to 300 ° C., particularly 240 to 280 ° C. is preferably used.
- the slurry preparation step is a step of preparing a slurry by mixing coal and a solvent, and is performed in the slurry preparation tank 4 in FIG.
- Coal is charged into the slurry preparation tank 4 from the coal hopper 2, and a solvent is charged into the slurry preparation tank 4 from the solvent tank 3.
- the coal and solvent charged in the slurry preparation tank 4 are mixed by a stirrer (not shown) to become a slurry.
- the mixing ratio of coal with respect to the solvent is not particularly limited, but for example, it is preferably in the range of 10 to 50 wt%, more preferably in the range of 15 to 35 wt% on the basis of dry coal.
- solvent soluble component extraction process The solvent-soluble component extraction step is performed in the preheater 6 and the extraction tank 7 in FIG.
- the slurry prepared in the slurry preparation tank 4 is once supplied to the preheater 6 by the pump 5 and heated to a predetermined temperature, then supplied to the extraction tank 7, and held at the predetermined temperature while being stirred by the stirrer 7a. Then, extraction is performed.
- the preheater 6 does not need to be installed.
- the temperature of the slurry in the solvent-soluble component extraction step is not particularly limited as long as the solvent-soluble component can be dissolved, but from the viewpoint of sufficient extraction of the solvent-soluble component, for example, in the range of 300 to 420 ° C., more preferably The range is 350 to 400 ° C.
- the heating time is not particularly limited, but is preferably in the range of 5 to 60 minutes, more preferably in the range of 20 to 40 minutes from the viewpoint of sufficient dissolution and extraction rate.
- the heating time when heated once by the preheater 6 is the total of the heating time in the preheater 6 and the heating time in the extraction tank 7.
- the pressure in the extraction step is preferably in the range of 1.0 to 2.0 MPa, although it depends on the temperature at the time of extraction and the vapor pressure of the solvent used.
- the pressure in the extraction tank 7 is lower than the vapor pressure of the solvent, the solvent volatilizes and is not confined in the liquid phase, so that extraction cannot be performed.
- a pressure higher than the vapor pressure of the solvent is required.
- the pressure is too high, the cost of the equipment and the operating cost increase, which is not economical.
- coal may be supplied into a solvent at a high temperature (for example, 380 ° C.) (supplied in a dry state), the coal may be mixed and heated, and solvent-soluble components in the coal may be extracted with the solvent.
- a high temperature for example, 380 ° C.
- the coal hopper 2 (in order to be able to supply the coal directly into the pipe 13 connecting the preheater 6 and the extraction tank 7 or into the extraction tank 7 without arranging the coal hopper 2 upstream of the pump 5.
- a lock hopper is disposed.
- the connecting portion between the pipe 13 or the extraction tank 7 and the coal hopper 2 is pressurized with an inert gas such as nitrogen so that the solvent does not flow back into the coal hopper 2.
- the slurry preparation tank 4 can be omitted.
- the extraction tank 7 is not arranged.
- a pipe that directly connects the preheater 6 and the gravity settling tank 8 is provided, and the coal hopper 2 (for example, a lock hopper) is disposed so that coal can be directly supplied into the pipe.
- the connecting portion between the pipe and the coal hopper 2 is pressurized with an inert gas such as nitrogen so that the solvent or the like does not flow back into the coal hopper 2.
- an inert gas such as nitrogen
- the separation step is a step of separating the slurry from which the solvent-soluble component has been extracted in the extraction step into a solution portion (supernatant liquid) containing the solvent-soluble component and a solid content concentrate containing the solvent-insoluble component by gravity sedimentation.
- the gravity sedimentation method is a separation method in which solid content is settled by using gravity to separate the solid and liquid. While the slurry is continuously fed into the tank, the solution part containing solvent-soluble components can be discharged from the upper part, and the solid content concentrate containing solvent-insoluble components can be discharged from the lower part, enabling continuous separation processing. It becomes.
- the solution part containing the solvent-soluble component accumulates in the upper part of the gravity settling tank 8, and is filtered by the filter unit 9 as necessary, and then discharged to the flasher.
- the solid concentrate containing the solvent-insoluble component is collected in the lower part of the gravity settling tank 8 and discharged to the solvent separator 12.
- the separation method is not limited to the gravity sedimentation method, and may be separated by, for example, a filtration method or a centrifugal separation method. In that case, a filter, a centrifuge, etc. are used as a solid-liquid separation device which replaces a gravity sedimentation tank.
- the solvent-insoluble component is a coal component (solid content) such as ash remaining without being dissolved in the solvent or coal containing the ash (that is, by-product coal) even when the coal component is extracted with the solvent.
- a coal component solid content
- the solvent-insoluble component is derived from an organic component having a relatively large molecular weight and a developed cross-linked structure.
- the gravity settling tank 8 is preferably kept warm, heated or / and pressurized in order to prevent reprecipitation of solvent-soluble components.
- the heating temperature is preferably in the range of 300 to 420 ° C.
- the pressure is preferably in the range of 1.0 to 3.0 MPa, more preferably in the range of 1.7 to 2.3 MPa.
- the time for maintaining the slurry in the gravity sedimentation tank 8 is not particularly limited, but the sedimentation can be performed in about 30 to 120 minutes.
- the ashless coal acquisition step is a step of obtaining ashless coal by separating and recovering the solvent from the solution part (supernatant liquid) separated in the separation step.
- the ashless coal acquisition step is a decompression step of obtaining a solid (powdered) ashless coal by evaporating and separating the solvent from the solution portion by reducing the pressure to a pressure lower than the vapor pressure of the solvent.
- the ashless coal obtained in the depressurization step is heated and the solvent remaining in the ashless coal is again evaporated and separated.
- the decompression step is a step of evaporating and separating the solvent from the solution portion separated in the separation step by flash distillation, and is performed by the flasher 10 in FIG.
- the flash distillation method refers to the boiling point from the distillation target by spraying (flashing) the distillation target (the solution portion separated in the separation step in the present embodiment) into the flasher (for example, the inner wall surface of the flasher) in a mist form. This is a distillation method for evaporating and separating a low substance (in this embodiment, a solvent).
- the pressure inside the flasher 10 is reduced to a pressure (for example, 0.1 MPa) lower than the vapor pressure of the solvent (for example, 1.0 MPa when the temperature of the solvent is 380 ° C.).
- the solvent contained in the solution portion supplied into the solvent 10 is separated by evaporation.
- the separated solvent is recovered, circulated to the slurry preparation tank 4 and repeatedly used.
- a pressure reduction process is performed in inert gas presence, such as nitrogen, from a viewpoint of solvent collection
- the solution portion before being supplied into the flasher 10 is pressurized to a pressure higher than the vapor pressure of the solvent (for example, 2.0 MPa at 380 ° C.) and is in a liquid state. Further, the temperature of the solution part before being supplied into the flasher 10 is set to 300 ° C., for example.
- solid (powdered) ashless coal is obtained.
- the pressure in the flasher 10 is lower than the vapor pressure of the solvent, and the ashless coal loses sensible heat due to the evaporation of the solvent, so that the temperature of the ashless coal becomes fluid.
- the temperature decreases to a temperature lower than the temperature indicating the temperature (for example, about 150 to 230 ° C.).
- the pressure in the flasher 10 is reduced to the same level as or lower than the atmospheric pressure. Therefore, the ashless coal becomes solid, and the ratio (residual rate) of the solvent remaining in the ashless coal is also reduced.
- the ashless coal is fused or deposited on a heating source (in this embodiment, the tube 23 of the steam tube dryer 11), heat exchange efficiency is reduced, and solvent recovery rate is reduced. Is suppressed.
- the pressure in the flasher 10 may be a pressure higher than the atmospheric pressure (limited to a pressure lower than the vapor pressure of the solvent) as long as the ashless coal is obtained as a solid.
- the inside of the flasher 10 can be set to about 10 to 230 ° C. from the viewpoint of preventing the ashless coal from being fused or precipitated in the flasher 10.
- the solid ashless coal obtained in the depressurization step is specifically a powder having a particle size (maximum length) of about several mm or less, and is about several ⁇ m to several hundred ⁇ m. .
- the residual ratio of the solvent remaining in the ashless coal obtained in the depressurization step is not particularly limited as long as the ashless coal is solid, but in the heating step, the ashless coal is fused or deposited on the heating source. From the viewpoint of prevention, it is preferably 10 wt% or less.
- the “remaining ratio of the solvent remaining in the ashless coal” here means the ratio of the solvent remaining in the ashless coal to the mixture of the ashless coal and the solvent remaining in the ashless coal.
- the pressure in the flasher 10 As a method of setting the residual ratio of the solvent remaining in the ashless coal to 10 wt% or less, there is a method of reducing the pressure in the flasher 10 to the same level as or lower than the atmospheric pressure. For example, it is preferable to perform the evaporative separation in about the same time as when the solvent is separated by about 100 wt% (99 wt% or more) at a time as in the prior art.
- the flash distillation method is used for evaporative separation of the solvent in the depressurization step, but it is not particularly limited as long as it is a method for evaporating and separating the solvent by depressurization.
- a vacuum distillation method or the like is used. Also good.
- the heating step is a step of evaporating and separating the solvent contained in the ashless coal from the solid ashless coal (solvent-free ashless coal) obtained in the decompression step by a distillation method using a steam tube dryer.
- the distillation method using a steam tube dryer is a substance having a low boiling point from the subject of distillation by indirectly heating the subject of solid distillation (in this embodiment, solid ashless coal obtained in the decompression step) in the dryer. This is a method of evaporating and separating (a solvent in this embodiment).
- FIG. 2A and 2B are schematic views of the steam tube dryer 11.
- FIG. 2A is a front view
- FIG. 2B is a cross-sectional view taken along line AA in FIG.
- the solid ashless coal obtained in the decompression step is charged into the dryer body 21 by the screw conveyor 22 (may be charged by a method other than the screw conveyor 22).
- the ashless coal charged into the dryer main body 21 is indirectly heated by coming into contact with a plurality of tubes 23 through which high-temperature steam (for example, 215 ° C. or 225 ° C.) flows while the dryer main body 21 rotates and is agitated.
- high-temperature steam for example, 215 ° C. or 225 ° C.
- a plurality of tubes 23 are provided on the outer peripheral side inside the dryer body 21.
- the solvent remaining in the ashless coal is evaporated and separated by contact with the tube 23. As a result, ashless coal from which the solvent is separated by about 100 wt% is obtained.
- the separated solvent is recovered by an inert gas (for example, nitrogen) flowing in the dryer main body 21 and is circulated to the slurry preparation tank 4 to be repeatedly used.
- an inert gas for example, nitrogen
- the dryer main body 21 is inclined and installed so that the discharge port 24b is downward so that the ashless coal supplied from the supply port 24a is discharged from the discharge port 24b side.
- the solid ashless coal obtained in the decompression step can be put into the dryer main body 21 in a solid state. Further, since the solvent is evaporated and separated by heating, the time for performing the evaporation and separation can be shortened.
- the distillation method using the steam tube dryer 11 is used in the heating step.
- any other distillation method can be used as long as it can add solid ashless coal and evaporate and separate the solvent by heating. The method may be used.
- the ashless charcoal substantially free of ash from the solution part and separated from the solvent by about 100% can be obtained by the above-described decompression step and heating step.
- the residual ratio of the solvent in the ashless coal finally obtained is 2 wt% or less, preferably 1 wt% or less.
- the ashless coal (the ashless coal finally obtained) means one having an ash content of 5 wt% or less, preferably 3 wt% or less, and the moisture content of the ashless coal is 1.0% or less. Yes, usually 0.5% or less.
- ashless coal contains almost no ash and has no moisture.
- the calorific value is higher than that of raw coal.
- the softening and melting property which is a particularly important quality as a raw material for coke for iron making, is greatly improved, and exhibits far superior performance (fluidity) compared to, for example, raw coal. Therefore, ashless coal can be used as a blended coal for coke raw materials.
- the ashless coal acquisition process has a two-stage solvent separation process, so that a solvent that cannot be recovered in the decompression process can be recovered in the heating process.
- the two-stage solvent separation step is originally intended to remove the solvent as much as possible in the decompression step, but in some cases the solvent remains in the ashless coal only in the decompression step. Because there is. Therefore, the removal rate of the solvent is increased by heating in the heating step. As a result, the solvent can be sufficiently recovered, and the solvent recovery rate can be improved as compared with the prior art (for example, Patent Document 1).
- you may make it an ashless coal acquisition process have a 3 or more steps of solvent separation processes.
- the by-product charcoal acquisition step is a step of obtaining by-product charcoal by evaporating and separating the solvent from the solid concentration liquid separated by the gravity sedimentation tank 8 in the separation step, and is performed by the solvent separator 12 in FIG.
- the in addition, the byproduct charcoal acquisition process is not necessary.
- a general distillation method or an evaporation method can be used as a method for separating the solvent from the solid content concentrate.
- the separated and recovered solvent can be circulated to the slurry preparation tank 4 and repeatedly used.
- by-product coal also referred to as RC or residual coal
- By-product charcoal contains ash, but has no water and has a sufficient calorific value.
- the oxygen-containing functional groups are eliminated, so that when used as a blended coal, it inhibits the softening and melting properties of other coals contained in this blended coal.
- this by-product coal can be used as a part of the blended coal of coke raw material in the same way as ordinary non-slightly caking coal, and is used for various fuels without being used as coke raw coal. It is also possible. The by-product coal may be discarded without being collected.
- the by-product coal acquisition step includes a first-stage solvent separation step of evaporating and separating the solvent from the solid concentrate, and a solvent remaining in the by-product coal from the by-product coal obtained in the solvent separation step. May be divided into a second-stage solvent separation step of evaporating and separating the solvent. That is, the byproduct charcoal acquisition process may have a two-stage solvent separation process. As a result, the solvent that cannot be recovered in the first-stage solvent separation process can be recovered in the second-stage solvent separation process. Therefore, the solvent recovery rate can be improved also in the byproduct charcoal acquisition step. In addition, you may make it a byproduct charcoal acquisition process have a solvent separation process of three steps or more.
- the by-product coal acquisition process has a two-stage solvent separation process
- the rate is preferably 10 wt% or less.
- by-product coal is fused or deposited on a heating source (for example, a tube of a steam tube dryer), heat exchange efficiency is lowered, and solvent recovery rate is lowered. Can be suppressed.
- the flash distillation method is preferably used for the first solvent separation process, and the distillation method using a steam tube dryer is used for the second solvent separation process. Is preferred.
- Example 1 As ashless coal in the middle of solvent recovery in the ashless coal acquisition process (ashless coal obtained in the decompression process), ashless coal with 5 wt%, 10 wt%, and 15 wt% of the solvent remaining in the ashless coal, respectively. Prepared. All ashless coal is solid. And about each prepared ashless coal, it heated up to about 215 degreeC corresponding to the conditions of the steam pressure of a steam tube dryer 2.05MPa, and performed the drying test. Ashless charcoal was charged into a round bottom flask, and the round bottom flask was placed in a mantle heater to raise the temperature. The inside of the round bottom flask was under a nitrogen atmosphere.
- the ashless coal in which 5 wt% and 10 wt% of the solvent remain in the ashless coal, the ashless coal does not melt even if the temperature is raised to 220 ° C. It was recovered in the same shape. On the other hand, for ashless coal in which 15 wt% of the solvent remained in the ashless coal, it was confirmed that the ashless coal was slightly fused when the temperature was raised to about 180 ° C. From this experiment, it has been found that it is preferable to suppress the residual ratio of the solvent remaining in the ashless coal to 10 wt% or less in order not to cause the fusion of the ashless coal.
- Example 2 Next, a drying test was performed using a steam tube dryer. As ashless coal in the middle of solvent recovery in the ashless coal acquisition process (ashless coal obtained in the decompression process), ashless coal in which 15 wt% of the solvent remains in the ashless coal is used, and a steam pressure of 2. It was performed under the condition of 05 MPa (215 ° C.). Ashless coal is solid. As a result, ashless coal was slightly fused around the tube. From this experiment, it was found that when ashless coal left at 15 wt% in ashless coal was used in a steam tube dryer, evaporative separation could be performed, but a slight fusion occurred in the actual machine.
- Example 3 Drying tests were performed using a steam tube dryer. This time, steam is used as the ashless coal in the middle of solvent recovery in the ashless coal acquisition process (ashless coal obtained in the decompression process) using ashless coal in which 5 wt% of the solvent remains in the ashless coal. The pressure was 2.05 MPa (215 ° C.) and 2.55 MPa (225 ° C.). Ashless coal is solid. The results are shown in FIG. As shown in FIG. 3, under either condition, a significant decrease in the solvent residual rate (synonymous with the solvent content in FIG. 3) was observed 12 minutes after the start of drying, and after 12 minutes, the solvent residual rate was 1 wt. % Or less.
- the ashless coal acquisition step is reduced to a pressure lower than the vapor pressure of the solvent, whereby the solvent is evaporated from the solution portion to obtain a solid ashless coal, and
- the solid ashless coal obtained in the decompression step is heated to have a heating step of evaporating and separating the solvent remaining in the ashless coal.
- the solvent that cannot be recovered in the decompression step is recovered in the heating step.
- the solvent can be sufficiently recovered, and the solvent recovery rate can be improved as compared with the prior art (for example, Patent Document 1).
- a distillation method for example, a distillation method using a steam tube dryer
- a heating source for example, a heating source
- the ashless coal that is put into the heating step is a solid in which the solvent is evaporated and separated to some extent in the decompression step, and it is necessary to return the ashless coal obtained in the decompression step to a liquid state once. do not do. Therefore, the rate at which ashless coal is fused or deposited on the heating source can be minimized. As a result, the heat exchange efficiency can be improved and the solvent recovery rate can be improved. Furthermore, since the solvent is evaporated and separated by heating, the evaporation and separation can be performed in a short time. As mentioned above, ashless coal can be manufactured efficiently.
- a distillation method using reduced pressure for example, flash distillation method, vacuum distillation method
- a distillation method using heating for example, distillation method using a steam tube dryer
- the pressure reduction step is performed by reducing the pressure below atmospheric pressure, so the residual rate of the solvent remaining in the ashless coal obtained in the pressure reduction step can be reduced. Therefore, the fall of the softening temperature of ashless coal by a solvent remaining in ashless coal can be suppressed. As a result, ashless coal with low meltability can be obtained at the heating temperature in the heating step (for example, about 200 to 230 ° C.), and the ashless coal is fused or deposited on the heating source in the heating step. Can be suppressed.
- the heating temperature in the heating step (for example, about 200 to 230 ° C.) Even when heated, ashless coal that exhibits almost no meltability can be obtained. As a result, ashless coal can be prevented from being fused or deposited on the heating source in the heating step.
- the flash distillation method is used for the evaporation and separation of the solvent in the depressurization step, so the liquid solution part separated in the separation step is put into the flasher in the liquid state. it can.
- the production efficiency of ashless coal can be improved.
- the solution part is sprayed (flashed) in the flasher (for example, the inner wall surface of the flasher) in a mist form, the surface area of the solution part can be increased, and the solvent can be efficiently separated by evaporation.
- it is not necessary to heat the inside of the flasher 10 it is possible to suppress ashless coal from being fused or precipitated in the flasher 10.
- the ashless coal acquisition step is a step of obtaining ashless coal by separating and recovering the solvent from the solution part (supernatant liquid) separated in the separation step.
- the ashless coal acquisition step includes a first evaporation step of evaporating and separating the solvent from the solution portion, and the ashless coal from the ashless coal obtained by evaporating and separating the solvent in the first evaporation step.
- the second evaporation step in which the solvent remaining therein is again evaporated and separated.
- the first evaporation step is a step of evaporating and separating the solvent from the solution portion separated in the separation step by flash distillation, and is performed by the flasher 10 in FIG.
- the flash distillation method refers to the boiling point from the distillation target by spraying (flashing) the distillation target (the solution portion separated in the separation step in the present embodiment) into the flasher (for example, the inner wall surface of the flasher) in a mist form. This is a method of evaporating and separating a low-substance substance (in this embodiment, a solvent).
- the pressure in the flasher 10 is lower than the vapor pressure of the solvent, the solvent contained in the solution portion supplied into the flasher 10 is evaporated and separated.
- the separated solvent is recovered, circulated to the slurry preparation tank 4 and repeatedly used.
- the first evaporation step is preferably performed in the presence of an inert gas such as nitrogen from the viewpoint of solvent recovery.
- the solution portion before being supplied into the flasher 10 is pressurized to a pressure higher than the vapor pressure of the solvent and is in a liquid state. Further, the temperature of the solution part before being supplied into the flasher 10 is set to 300 ° C., for example.
- powder (solid) ashless coal is usually obtained. This is due to the fact that the inside of the flasher is usually at a pressure comparable to the atmospheric pressure, and that sensible heat is taken away by evaporation of the solvent.
- liquid ashless coal is obtained by leaving a solvent in the ashless coal at a predetermined ratio.
- the pressure in the flasher 10 is set to 0.5 MPa, for example, so that the ashless coal is easily maintained in a liquid state.
- the flasher 10 may be heated to set the temperature inside the flasher 10 to 200 to 450 ° C., for example.
- the residual ratio (ratio) of the solvent remaining in the ashless coal is not particularly limited as long as the ashless coal is in a liquid state, but is in the range of 10 to 50 wt% from the viewpoint of easily maintaining the ashless coal in a liquid state. The range of 15 to 30 wt% is more preferable.
- the “remaining ratio of the solvent remaining in the ashless coal” here means the ratio of the solvent remaining in the ashless coal to the mixture of the ashless coal and the solvent remaining in the ashless coal.
- a method of performing evaporative separation in a time shorter than the time of separation in% (99 wt% or more) and a method of simultaneously performing these two methods are a method of performing the first evaporation step at a lower temperature than the case where the solvent is separated by about 100 wt% from the solution part.
- the softening start temperature of the ashless coal is lowered.
- a phenomenon occurs in which ashless coal dissolves into the solvent. Therefore, the fluidity of ashless coal can be obtained at a lower temperature.
- ashless coal can maintain a liquid state at a lower temperature. As a result, it is excellent in handling property when transferring ashless coal, and ashless coal can be easily transferred from the first evaporation step to the second evaporation step.
- the ashless coal when transferring the ashless coal obtained in the first evaporation step to the second evaporation step, the ashless coal is easily maintained in a liquid state so as to easily maintain a liquid state. Thus, it is preferable to transfer the ashless coal to the second evaporation step while heating.
- the temperature of the ashless coal transferred is, for example, 300 ° C.
- the flash distillation method is used in the first evaporation step, but other methods such as a thin film distillation method (details will be described later) and a vacuum distillation method may be used.
- the solvent contained in the ashless coal is evaporated and separated from the ashless coal obtained in the first evaporation step (the ashless coal in which the solvent is left in a predetermined ratio) by thin film distillation.
- This process is performed in the thin film distillation tank 31 in FIG.
- the thin film distillation method is an object to be distilled from the upper part of the thin film distillation tank 31 containing the scraper 31b (also referred to as a wiper) into the thin film distillation tank 31 (in this embodiment, ashless coal obtained in the first evaporation step).
- a continuous distillation is performed by forming a thin film to be distilled with a scraper 31b on the inner wall of the thin film distillation tank 31.
- a heater 31a is attached around the thin film distillation tank 31, and the thin film distillation tank 31 is heated from the outside by the heater 31a so that the inner wall of the thin film distillation tank 31 has a desired temperature.
- the liquid ashless coal obtained in the first evaporation step is supplied into the thin film distillation tank 31 in a liquid state, and remains in the ashless coal by being heated from the outside by the heater 31a.
- the solvent is evaporated off.
- ashless coal from which the solvent is separated by about 100 wt% is obtained. Further, the separated solvent is recovered, circulated to the slurry preparation tank 4 and repeatedly used.
- the second evaporation step is preferably performed in the presence of an inert gas such as nitrogen from the viewpoint of solvent recovery.
- the pressure in the thin film distillation tank 31 is 0.1 MPa (normal pressure) or 0.1 MPa (normal pressure) or less.
- the heating temperature (the temperature in the thin film distillation tank 31) is, for example, 250 to 350 ° C. Since the temperature in the thin film distillation tank 31 is the above temperature, liquid ashless coal is obtained by the thin film distillation method. Therefore, the obtained liquid ashless coal is dropped into solidifying means (for example, water, a metal endless belt of a belt conveyor, a molding die having a hollow portion of a predetermined shape, etc.) at about 0 to 150 ° C. As a result, ashless coal solidified into a desired shape can be easily obtained. Therefore, if it is a thin-film distillation method, the process of once returning ashless coal to a liquid state and solidifying it to a desired shape can be eliminated.
- solidifying means for example, water, a metal endless belt of a belt conveyor, a molding die having a hollow portion of a predetermined shape, etc.
- the thin film distillation method is used in the second evaporation step, but other methods such as a flash distillation method and a vacuum distillation method may be used. That is, the flash distillation method can be used for both the first evaporation step and the second evaporation step, and the thin film distillation method can be used for both the first evaporation step and the second evaporation step.
- the ashless coal acquisition process includes the two-stage solvent separation process, the solvent that cannot be recovered in the first evaporation process can be recovered in the second evaporation process. As a result, the solvent can be sufficiently recovered and the solvent recovery rate can be improved. In addition, you may make it an ashless coal acquisition process have a 3 or more steps of solvent separation processes.
- the ashless coal acquisition step includes a first evaporation step for evaporating and separating the solvent from the solution portion, and an ashless coal obtained by evaporating and separating the solvent in the first evaporation step.
- a second evaporation step in which the solvent remaining in the ashless coal is again evaporated and separated from the charcoal.
- the ashless coal is removed by leaving the solvent in the ashless coal at a predetermined ratio.
- the liquid ashless coal is transferred to the second evaporation step in a liquid state. Therefore, the solvent that cannot be recovered in the first evaporation step can be recovered in the second evaporation step.
- the solvent can be sufficiently recovered, and the solvent recovery rate can be improved. Furthermore, since the softening temperature of ashless coal falls by leaving a predetermined ratio solvent in the ashless coal obtained in the first evaporation step, the fluidity of ashless coal can be obtained at a lower temperature. Can do. Therefore, ashless coal can maintain a liquid state at a lower temperature. As a result, the handling property (liquid handling) when transferring the ashless coal is excellent, and the ashless coal can be easily transferred from the first evaporation step to the second evaporation step.
- the solvent is omitted in the first evaporation process as in the prior art (for example, Patent Document 1). There is no need to separate 100%. That is, even if the solvent remains in the ashless coal in the first evaporation step, the solvent remaining in the ashless coal can be recovered in the second evaporation step. Therefore, it is possible to leave the solvent in the ashless coal in the first evaporation step.
- the residual ratio of the solvent remaining in the ashless coal obtained in the first evaporation step is 10 wt% or more and 50 wt% or less. If the residual ratio of the solvent remaining in the ashless coal is 10% wt or more, the meltability of the ashless coal is improved, it becomes easy to maintain the ashless coal in a liquid state, and the fluidity in the liquid state is also improved. Better. Further, if the residual ratio of the solvent remaining in the ashless coal is 50% wt or less, the load for evaporating and separating the solvent in the second evaporation step can be reduced, and the solvent can be easily separated and recovered by about 100%.
- the flash distillation method since the flash distillation method is used for the evaporation and separation of the solvent in the first evaporation step, the liquid solution portion separated in the separation step is kept in a liquid state in the flasher. Can be thrown into. As a result, the production efficiency of ashless coal can be improved and the equipment cost can be suppressed. Moreover, since the solution part is sprayed (flashed) in the flasher (for example, the inner wall surface of the flasher) in a mist form, the surface area of the solution part can be increased, and the solvent can be efficiently separated by evaporation.
- the liquid ashless coal can be supplied in the liquid state into the thin film distillation tank by using the thin film distillation method for the evaporation and separation of the solvent in the second evaporation step, The production efficiency of ash coal can be improved, and the equipment cost can be suppressed.
- the ashless coal obtained in the second evaporation step ashless coal from which the solvent is separated by about 100%
- the obtained liquid ashless coal becomes liquid
- Ashless charcoal solidified into the shape can be easily obtained. Therefore, it is possible to eliminate the step of once returning the powder (solid) ashless coal to a liquid state and solidifying it into a desired shape.
- the thin film tank formed on the inner wall of the thin film distillation tank can be surely scraped off by a scraper (wiper), for example, even if ashless coal with low fluidity (high clay) is discharged. Can do.
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Abstract
Description
(無灰炭の製造装置1の構成)
図1は、本発明の第1実施形態に係る無灰炭の製造装置1を示す概略図である。本実施形態の無灰炭の製造装置1は、図1に示すように、石炭を貯蔵および切出しする石炭ホッパ2と、溶剤を貯留する溶剤タンク3と、石炭と溶剤とを混合してスラリーを調製するスラリー調製槽4と、調製されたスラリーを移送するポンプ5と、移送されたスラリーを加熱する予熱器6と、加熱されたスラリーから溶剤可溶成分を抽出する抽出槽7と、溶剤可溶成分が抽出されたスラリーを重力沈降法により溶剤可溶成分を含む溶液部(上澄み液)と溶剤不溶成分を含む固形分濃縮液とに分離する重力沈降槽8と、分離された溶液部を濾過するフィルターユニット9と、濾過された溶液部から溶剤を分離回収して無灰炭(HPC:Hyper coal)を得るフラッシャー10及びスチームチューブドライヤ11と、重力沈降槽8にて分離された固形分濃縮液から溶剤を分離回収して副生炭(RC:Residue coal)を得る溶剤分離器12とを有する。
抽出工程は、石炭と溶剤とを混合して得られるスラリーを加熱して溶剤可溶成分を抽出する工程である。本実施形態において、この抽出工程は、石炭と溶剤とを混合してスラリーを調製するスラリー調製工程と、スラリー調製工程にて得られたスラリーを加熱して溶剤可溶成分を抽出する溶剤可溶成分抽出工程とに分かれている。
なお、上記の説明では非水素供与性化合物を溶剤として用いる場合について述べたが、テトラリンを代表とする水素供与性の化合物(石炭液化油を含む)を溶剤として用いても良い。水素供与性溶剤を用いた場合、無灰炭の収率が向上する。
スラリー調製工程は、石炭と溶剤とを混合してスラリーを調製する工程であり、図1中、スラリー調製槽4で行われる。石炭ホッパ2から石炭がスラリー調製槽4に投入されると共に、溶剤タンク3から溶剤がスラリー調製槽4に投入される。スラリー調製槽4に投入された石炭および溶剤は、攪拌機(不図示)で混合され、スラリーとなる。
溶剤可溶成分抽出工程は、図1中、予熱器6および抽出槽7で行われる。スラリー調製槽4にて調製されたスラリーは、ポンプ5によって、一旦、予熱器6に供給されて所定温度まで加熱された後、抽出槽7に供給され、攪拌機7aで攪拌されながら所定温度で保持されて抽出が行われる。なお、予熱器6は設置されていなくてもよい。
分離工程は、抽出工程にて溶剤可溶成分が抽出されたスラリーを重力沈降法により溶剤可溶成分を含む溶液部(上澄み液)と溶剤不溶成分を含む固形分濃縮液とに分離する工程であり、図1中、重力沈降槽8で行われる。重力沈降法とは、重力を利用して固形分を沈降させて固液分離する分離方法である。スラリーを槽内に連続的に供給しながら、溶剤可溶成分を含む溶液部を上部から、溶剤不溶成分を含む固形分濃縮液を下部から排出することができるので、連続的な分離処理が可能となる。
無灰炭取得工程は、分離工程にて分離された溶液部(上澄み液)から溶剤を分離回収して無灰炭を得る工程である。本実施形態において、この無灰炭取得工程は、溶剤の蒸気圧よりも低い圧力に減圧することにより、溶液部から溶剤を蒸発分離させて固体(粉粒状)の無灰炭を得る減圧工程と、減圧工程にて得られた無灰炭を加熱して、当該無灰炭中に残存する溶剤を再度蒸発分離させる加熱工程とに分かれている。
減圧工程は、分離工程にて分離された溶液部からフラッシュ蒸留法により溶剤を蒸発分離させる工程であり、図1中、フラッシャー10で行われる。フラッシュ蒸留法とは、蒸留対象(本実施形態では分離工程にて分離された溶液部)をフラッシャー内(例えば、フラッシャーの内壁面)に霧状に噴射(フラッシュ)させることで、蒸留対象から沸点の低い物質(本実施形態では溶剤)を蒸発分離する蒸留法である。
加熱工程は、減圧工程にて得られた固体の無灰炭(溶剤が残存した無灰炭)から当該無灰炭中に含まれる溶剤をスチームチューブドライヤを利用した蒸留法により蒸発分離させる工程であり、図1中、スチームチューブドライヤ11で行われる。スチームチューブドライヤを利用した蒸留法とは、固体の蒸留対象(本実施形態では、減圧工程にて得られた固体の無灰炭)をドライヤ内で間接加熱して、蒸留対象から沸点の低い物質(本実施形態では溶剤)を蒸発分離する方法である。
副生炭取得工程は、分離工程にて重力沈降槽8により分離された固形分濃縮液から溶剤を蒸発分離させて副生炭を得る工程であり、図1中、溶剤分離器12で実施される。なお、副生炭取得工程はなくてもよい。
(実施例1)
無灰炭取得工程における溶剤回収途中の無灰炭(減圧工程にて得られた無灰炭)として、無灰炭中に溶剤をそれぞれ5wt%、10wt%、15wt%残存させた無灰炭を調製した。無灰炭はいずれも固体である。そして、調製したそれぞれの無灰炭について、スチームチューブドライヤのスチーム圧力2.05MPaの条件に相当する215℃程度まで昇温させ、乾燥試験を行った。無灰炭は丸底フラスコに投入し、丸底フラスコをマントルヒーターに設置して昇温を行った。なお、丸底フラスコ内は窒素雰囲気下とした。
次に、スチームチューブドライヤを用いて乾燥試験を行った。無灰炭取得工程における溶剤回収途中の無灰炭(減圧工程にて得られた無灰炭)として、無灰炭中に溶剤を15wt%残存させた無灰炭を用いて、スチーム圧力2.05MPa(215℃)の条件で行った。無灰炭は固体である。その結果、チューブの周囲に無灰炭がやや融着した。この実験により、無灰炭中に15wt%残存させた無灰炭をスチームチューブドライヤに使用した場合には、蒸発分離を行うことはできるが、やや融着が生じることが実機においても判明した。
スチームチューブドライヤを用いて乾燥試験を行った。今度は、無灰炭取得工程における溶剤回収途中の無灰炭(減圧工程にて得られた無灰炭)として、無灰炭中に溶剤を5wt%残存させた無灰炭を用いて、スチーム圧力2.05MPa(215℃)、2.55MPa(225℃)の2つの条件で行った。無灰炭は固体である。結果を図3に示す。図3に示すとおり、どちらの条件においても、乾燥開始から12分後にかけて溶剤残存率(図3中、溶剤含有率と同義)の大幅な低下が認められ、12分後には溶剤残存率が1wt%以下となった。乾燥開始から30分後には溶剤残存率はさらに低下しており、0.1wt%程度となった。その後の値は略横ばいであった。この実験により、無灰炭中に溶剤を5wt%残存させた無灰炭であれば、どちらの温度条件においても、30分程度という短時間で溶剤を略100wt%回収できることが判明した。
次に、第1実施形態に係る無灰炭の製造方法の効果について説明する。
また、減圧工程においては、蒸発分離の際に溶剤を加熱する必要がないので、加熱源を配備した蒸留法(例えば、スチームチューブドライヤを利用した蒸留法)を減圧工程に用いる場合に比べて、無灰炭が融着或いは析出することを抑制できる。
さらに、加熱工程に投入される無灰炭は、減圧工程にて、ある程度溶剤が蒸発分離され、かつ、固体であり、減圧工程にて得られた無灰炭を一旦液状に戻す操作を必要としない。したがって、加熱源に無灰炭が融着又は析出する割合を最小限に抑えることができる。その結果、熱交換効率を向上でき、溶剤回収率を向上できる。さらに、加熱により溶剤を蒸発分離させているので、蒸発分離を短時間で行うことができる。
以上より、無灰炭を効率よく製造できる。
次に、第2実施形態に係る無灰炭の製造方法について図4を参照しつつ説明する。但し、上記第1実施形態と同様の構成を有するものについては、同じ符号を用いて適宜その説明を省略する。本実施形態の無灰炭の製造装置は、上記第1実施形態のスチームチューブドライヤ11を有さず、代わりに、薄膜蒸留槽31を有している。また、本実施形態の無灰炭の製造方法は、無灰炭取得工程が、上記第1実施形態と異なっており、その他の工程は、上記第1実施形態と同じである。
無灰炭取得工程は、分離工程にて分離された溶液部(上澄み液)から溶剤を分離回収して無灰炭を得る工程である。本実施形態において、この無灰炭取得工程は、溶液部から溶剤を蒸発分離させる第1蒸発工程と、第1蒸発工程にて溶剤を蒸発分離して得られた無灰炭から当該無灰炭中に残存する溶剤を再度蒸発分離させる第2蒸発工程とに分かれている。
第1蒸発工程は、分離工程にて分離された溶液部からフラッシュ蒸留法により溶剤を蒸発分離させる工程であり、図4中、フラッシャー10で行われる。フラッシュ蒸留法とは、蒸留対象(本実施形態では分離工程にて分離された溶液部)をフラッシャー内(例えば、フラッシャーの内壁面)に霧状に噴射(フラッシュ)させることで、蒸留対象から沸点の低い物質(本実施形態では溶剤)を蒸発分離する方法である。
第2蒸発工程は、第1蒸発工程にて得られた無灰炭(溶剤を所定の割合で残存させた無灰炭)から当該無灰炭中に含まれる溶剤を薄膜蒸留法により蒸発分離させる工程であり、図4中、薄膜蒸留槽31で行われる。薄膜蒸留法とは、スクレーパ31b(ワイパーともいう)を収容した薄膜蒸留槽31の上部から薄膜蒸留槽31内に蒸留対象(本実施形態では、第1蒸発工程にて得られた無灰炭)を供給し、薄膜蒸留槽31の内壁にスクレーパ31bにて蒸留対象の薄膜を形成させ連続蒸留を行う蒸留法である。薄膜蒸留槽31の周囲には加熱器31aが取り付けられ、薄膜蒸留槽31の内壁が所望の温度となるように、薄膜蒸留槽31は加熱器31aにて外部から加熱される。
次に、第2実施形態に係る無灰炭の製造方法の効果について説明する。
2 石炭ホッパ
3 溶剤タンク
4 スラリー調製槽
5 ポンプ
6 予熱器
7 抽出槽
8 重力沈降槽
9 フィルターユニット
10 フラッシャー
11 スチームチューブドライヤ
12 溶剤分離器
13 管
31 薄膜蒸留槽
Claims (5)
- 石炭と溶剤とを混合して得られるスラリーを加熱して溶剤に可溶な石炭成分を抽出する抽出工程と、
前記抽出工程にて前記石炭成分が抽出されたスラリーから前記石炭成分を含む溶液部を分離する分離工程と、
前記分離工程にて分離された溶液部から溶剤を分離回収して無灰炭を得る無灰炭取得工程とを備える無灰炭の製造方法において、
前記無灰炭取得工程は、
溶剤の蒸気圧よりも低い圧力に減圧することにより、前記溶液部から溶剤を蒸発分離させて固体の無灰炭を得る減圧工程と、
前記減圧工程にて得られた固体の無灰炭を加熱して、当該無灰炭中に残存する溶剤を蒸発分離させる加熱工程とを有することを特徴とする無灰炭の製造方法。 - 大気圧以下に減圧して前記減圧工程を行う、請求項1に記載の無灰炭の製造方法。
- 前記減圧工程にて得られた無灰炭中に残存する溶剤の残存率が10wt%以下である、請求項1又は2に記載の無灰炭の製造方法。
- 石炭と溶剤とを混合して得られるスラリーを加熱して溶剤に可溶な石炭成分を抽出する抽出工程と、
前記抽出工程にて前記石炭成分が抽出されたスラリーから前記石炭成分を含む溶液部を分離する分離工程と、
前記分離工程にて分離された溶液部から溶剤を分離回収して無灰炭を得る無灰炭取得工程とを備える無灰炭の製造方法において、
前記無灰炭取得工程は、
前記溶液部から溶剤を蒸発分離させる第1蒸発工程と、
前記第1蒸発工程にて溶剤を蒸発分離して得られた無灰炭から当該無灰炭中に残存する溶剤を蒸発分離させる第2蒸発工程とを有し、
前記第1蒸発工程において、前記無灰炭に溶剤を所定の割合で残存させることにより当該無灰炭を液状とし、当該液状の無灰炭を液状の状態で前記第2蒸発工程に移送することを特徴とする無灰炭の製造方法。 - 前記第1蒸発工程にて得られた無灰炭中に残存する溶剤の残存率が10wt%以上50wt%以下である、請求項4に記載の無灰炭の製造方法。
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KR1020147017196A KR101624816B1 (ko) | 2011-12-28 | 2012-12-14 | 무회탄의 제조 방법 |
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Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014126024A1 (ja) * | 2013-02-13 | 2014-08-21 | 株式会社神戸製鋼所 | 副生炭の製造方法 |
WO2014171460A1 (ja) * | 2013-04-16 | 2014-10-23 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
CN105612245A (zh) * | 2013-10-09 | 2016-05-25 | 株式会社神户制钢所 | 无灰煤的制造方法 |
CN106459795A (zh) * | 2014-05-27 | 2017-02-22 | 株式会社神户制钢所 | 无灰煤的制造装置以及无灰煤的制造方法 |
WO2017122459A1 (ja) * | 2016-01-13 | 2017-07-20 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
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KR20160032046A (ko) * | 2013-05-30 | 2016-03-23 | 클린 콜 테크놀로지스, 아이엔씨. | 석탄의 처리 |
JP6203698B2 (ja) * | 2014-09-30 | 2017-09-27 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
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JP6454260B2 (ja) * | 2015-11-25 | 2019-01-16 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
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Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5324301A (en) * | 1976-08-20 | 1978-03-07 | Mitsui Cokes Kogyo Kk | Process for producing coke |
JPS56145974A (en) * | 1980-04-14 | 1981-11-13 | Toyo Eng Corp | Preparation of solvent-refined coal |
JP2005120185A (ja) * | 2003-10-15 | 2005-05-12 | Kobe Steel Ltd | 無灰炭の製造方法 |
JP2007023190A (ja) * | 2005-07-19 | 2007-02-01 | Kobe Steel Ltd | コークスの製造方法、及び、銑鉄の製造方法 |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4374015A (en) * | 1981-03-09 | 1983-02-15 | Kerr-Mcgee Corporation | Process for the liquefaction of coal |
JP4295544B2 (ja) * | 2003-04-09 | 2009-07-15 | 株式会社神戸製鋼所 | 冶金用改質炭の製造方法、ならびに冶金用改質炭を用いた還元金属および酸化非鉄金属含有スラグの製造方法 |
US8226816B2 (en) * | 2006-05-24 | 2012-07-24 | West Virginia University | Method of producing synthetic pitch |
JP4061351B1 (ja) * | 2006-10-12 | 2008-03-19 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
JP5255303B2 (ja) * | 2008-03-14 | 2013-08-07 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
-
2012
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Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5324301A (en) * | 1976-08-20 | 1978-03-07 | Mitsui Cokes Kogyo Kk | Process for producing coke |
JPS56145974A (en) * | 1980-04-14 | 1981-11-13 | Toyo Eng Corp | Preparation of solvent-refined coal |
JP2005120185A (ja) * | 2003-10-15 | 2005-05-12 | Kobe Steel Ltd | 無灰炭の製造方法 |
JP2007023190A (ja) * | 2005-07-19 | 2007-02-01 | Kobe Steel Ltd | コークスの製造方法、及び、銑鉄の製造方法 |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014126024A1 (ja) * | 2013-02-13 | 2014-08-21 | 株式会社神戸製鋼所 | 副生炭の製造方法 |
JP2014152308A (ja) * | 2013-02-13 | 2014-08-25 | Kobe Steel Ltd | 副生炭の製造方法 |
WO2014171460A1 (ja) * | 2013-04-16 | 2014-10-23 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
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 |
US10035967B2 (en) | 2013-04-16 | 2018-07-31 | Kobe Steel, Ltd. | Method for producing ash-free coal |
CN105612245A (zh) * | 2013-10-09 | 2016-05-25 | 株式会社神户制钢所 | 无灰煤的制造方法 |
US9752088B2 (en) | 2013-10-09 | 2017-09-05 | Kobe Steel, Ltd. | Ashless coal production method |
CN105612245B (zh) * | 2013-10-09 | 2018-09-11 | 株式会社神户制钢所 | 无灰煤的制造方法 |
CN106459795A (zh) * | 2014-05-27 | 2017-02-22 | 株式会社神户制钢所 | 无灰煤的制造装置以及无灰煤的制造方法 |
WO2017122459A1 (ja) * | 2016-01-13 | 2017-07-20 | 株式会社神戸製鋼所 | 無灰炭の製造方法 |
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