JP4939466B2 - Solid-liquid separation device, solid-liquid separation method, and method for producing ashless coal - Google Patents

Description

  The present invention relates to a gravity precipitation-filtration combined solid-liquid separation apparatus and solid-liquid separation method that employ a combination of gravity sedimentation method and filtration method, and ashless coal for obtaining ashless coal from which ash is removed from coal. It relates to a manufacturing method.

  Coal is widely used as a fuel for thermal power generation and boilers, or as a raw material for chemical products, and development of a technique for efficiently removing ash in coal is strongly desired as one of environmental measures. For example, in a high-efficiency combined power generation system using gas turbine combustion, an attempt has been made to use ashless coal from which ash has been removed as a fuel to replace liquid fuel such as LNG. Attempts have also been made to use ashless coal as coking coal for ironmaking coke such as blast furnace coke.

The following method is proposed as a manufacturing method of ashless coal (for example, patent document 1). This will be briefly described with reference to FIG.
For example, a coal raw material and a solvent are mixed in the slurry preparation tank 101 to prepare a slurry, the slurry is heated by the preheater 103, and the coal component soluble in the solvent is extracted in the extraction tank 104. From the obtained slurry, a gravity sedimentation tank (solid-liquid separator) 105 separates a supernatant liquid containing a coal component soluble in a solvent and a solid concentrate containing a coal component insoluble in a solvent. Next, in order to sufficiently reduce the ash content in the ashless coal, the supernatant liquid is passed through the filter unit 106, and then the solvent is separated by the solvent separator 107 to obtain ashless coal (HPC). On the other hand, when the separated solid concentrate is solvent-separated by the solvent separator 108, by-product coal (RC) is obtained. In particular, as shown schematically in FIG. 6, the supernatant liquid in the gravity sedimentation tank 105 is discharged as it is from the opening of the discharge pipe 110, and is filtered by the filter unit 106 in which the filter 111 is installed upright in the vertical direction. The

However, in the above method, since the operation is performed under high temperature and high pressure conditions, it is necessary to raise and lower the temperature and pressure when replacing the filter, and there are many restrictions on the structure of the apparatus, so the replacement work is complicated.
JP 2007-735 A Japanese Patent Laid-Open No. 2005-120185

  On the other hand, in a solid-liquid separation device that employs the gravity sedimentation method, it is conceivable that a filter is installed at the opening of the supernatant liquid discharge pipe, and solid-liquid separation by filtration is also performed. Happened early. This is presumed that part of the solute was deposited as a sticky substance (hereinafter referred to as a sticky substance) due to a temperature difference from the extraction tank, and adhered to and clogged the filter.

  The present invention has been made in view of the above circumstances, and in a gravity sedimentation-filtration combined solid-liquid separation apparatus that employs a combination of a gravity sedimentation method and a filtration method, it is possible to achieve a longer filter life. Objective. That is, an object of the present invention is to provide a gravity-precipitation combined filtration type solid-liquid separation device and a solid-liquid separation method that achieve a longer filter life.

  Another object of the present invention is to provide a method for producing ashless coal that can produce ashless coal from which ash is sufficiently removed at high efficiency and at low cost.

The present invention is a solid-liquid separation device that separates a supernatant liquid and a solid concentration liquid by precipitating a solid content in a slurry,
A settling tank containing the slurry and settling solids;
A supernatant discharge pipe having an opening for allowing the supernatant in the settling tank to flow in, and for discharging the introduced supernatant to the outside of the settling tank;
A filter that is installed at the opening of the supernatant liquid discharge pipe and captures the solid content in the supernatant liquid, and is disposed so that the solid content capture surface faces the slurry liquid surface and is inclined with respect to the horizontal plane. A filter; and a solid content receiving member disposed at the lower end of the filter;
It is related with the solid-liquid separator characterized by having provided.

The present invention is also a solid-liquid separation method in which the solid content in the slurry is settled and the supernatant liquid and the solid content concentrate are separated using the solid-liquid separation apparatus,
A solid deposit layer is formed on a filter installed at an inclination with respect to a horizontal plane by a solid content receiving member, and a supernatant liquid is passed through the solid deposit layer and the filter to be discharged. The present invention relates to a solid-liquid separation method.

The present invention also provides
A slurry preparation step of preparing a slurry by mixing a coal raw material and a solvent;
An extraction step of heating the slurry obtained in the slurry preparation step to extract a coal component soluble in a solvent;
A separation step of separating the supernatant and solids concentrate from the slurry obtained in the extraction step by the solid-liquid separator; and a ashless coal by separating the solvent from the supernatant separated in the separation step Ashless charcoal acquisition process to obtain
It is related with the manufacturing method of ashless charcoal characterized by including.

According to the gravity-precipitation combined filtration type solid-liquid separation apparatus and solid-liquid separation method according to the present invention, it is possible to obtain a supernatant liquid from which solid content has been sufficiently removed while achieving a longer filter life. .
According to the method for producing ashless coal according to the present invention, it is possible to obtain a supernatant liquid from which solid content (solvent insoluble component) has been sufficiently removed while achieving a longer filter life in the separation step. As a result, ashless coal from which ash has been sufficiently removed can be produced with high efficiency and at low cost.

[Solid-liquid separation device and solid-liquid separation method]
The solid-liquid separator according to the present invention is a gravity sedimentation-filtration combined type apparatus that separates a supernatant liquid and a solid concentrate from a slurry by using a gravity sedimentation method and a filtration method in combination. The solid-liquid separator according to the present invention will be described in detail with reference to FIG. FIG. 1A is a schematic configuration diagram showing a cross-sectional configuration of an example of a solid-liquid separation device according to the present invention, and FIG. 1B is a schematic perspective view when the device of FIG. 1A is viewed from above. It is a figure, Comprising: It is for showing the positional relationship of each structural member.

  The solid-liquid separation device 50 according to the present invention has a sedimentation tank 1; a supernatant liquid discharge pipe 2; a filter 10; and a solid content receiving member 3. Usually, a lid 4, a slurry supply pipe 5, A liquid concentrate outlet 6 is provided.

  The sedimentation tank 1 is a gravity sedimentation tank, which contains slurry and settles the solid content, and separates the supernatant liquid and the solid content concentrate. As shown in FIG. 1, the sedimentation tank 1 generally has a generally cylindrical shape as a whole and an inverted conical shape at the bottom.

  The supernatant liquid discharge pipe 2 has an opening 20 through which the supernatant liquid in the sedimentation tank 1 flows, and discharges the supernatant liquid that has flowed out of the sedimentation tank. The filter 10 is installed so as to close the opening 20. And traps solids in the supernatant. In particular, as shown in FIG. 1, the filter 10 is disposed so that the solid content capturing surface (filtering surface) faces the slurry liquid surface (upward direction) and is inclined with respect to the horizontal plane. That is, the filter 10 is disposed so that the solid content capturing surface (filtering surface) is inclined with respect to the horizontal plane while facing upward in the drawing. The solid content receiving member 3 is installed at the lower end of the filter 10, and the solid content receiving member 3 supports the solid content captured on the solid content capturing surface of the filter 10. Therefore, in the process of filtering and discharging the supernatant liquid, the solid content deposition layer 22 is effectively formed on the solid content capture surface of the filter 10, and the solid content deposition layer 22 and the filter 10 can be passed through the supernatant liquid. it can. As a result, the supernatant liquid from which the solid content has been sufficiently removed can be discharged and the filter can be prevented from being clogged for a relatively long period of time. The details of the mechanism of such a phenomenon are not clear, but are thought to be based on the following mechanism. If the filter is tilted as described above and a solid content receiving member is used, the solid content will flow down after the solid content (undissolved by-product charcoal) reaches a certain level or more. A layer is formed. Such a deposited layer also includes a solid component having a relatively large particle size, and a gap between the particles is appropriately secured, so that the deposited layer exhibits a filter effect. By-product coal has become more porous due to the extraction of ashless coal, so it absorbs sticky substances and prevents clogging of the filter surface. Therefore, it is considered that a supernatant liquid from which solid content has been sufficiently removed can be obtained while achieving a long life of the filter. For example, when the filter is used in a vertical position, the adhesive material selectively causes clogging of the filter, thereby shortening the life of the filter. Further, for example, when the filter is used in parallel to the horizontal plane, the solid content can be removed, but the deposited layer becomes too thick, so that the throughput is reduced relatively early, and as a result, the filter life is shortened. Also, for example, if the filter is installed so that the solid content capture surface of the filter does not face the slurry liquid surface (upward) but the bottom of the sedimentation tank (downward), the adhesive substance selectively clogs the filter. Filter life is shortened.

  In FIG. 1, the supernatant discharge pipe 2 extends through the lid 5 and extends to the upper part of the slurry accommodated in the settling tank 1. As shown in FIG. 2, the supernatant discharge pipe 2 is formed on the side wall of the settling tank. It may be penetrated.

  The opening direction of the opening 20 is not particularly limited as long as the filter 10 can be arranged as described above. For example, the opening may be formed so as to open in the slurry liquid surface direction (upward direction) as shown in FIG. 1, or may be formed so as to open in the horizontal direction. Although not shown, even if the opening is formed so as to open in the horizontal direction, the solid content capturing surface (filtering surface) of the filter is opposed to the slurry liquid surface (upward direction) and is in a horizontal plane. The filter can be arranged so as to be inclined.

  The inclination angle of the filter 10 is not particularly limited as long as the object of the present invention is achieved. For example, the smaller angle formed by the filter and the horizontal plane is preferably 10 to 60 °. In particular, when the present apparatus is used in a method for producing ashless coal, the angle is preferably 20 to 45 °.

  The type of the filter 10 may be appropriately selected according to the type and temperature of the slurry, the pressure, the target solid content removal rate, and the like. For example, as a filter material, a metal filter, a ceramic filter, or the like can be used. For example, the hole diameter of the filter is not particularly limited, and may be, for example, 0.1 μm to 20 mm. In particular, when this apparatus is used in a method for producing ashless coal, it is preferable to use a metal filter having an opening of 0.5 μm.

  The form, size, and material of the solid content receiving member 3 are not particularly limited as long as a deposited layer having a desired thickness is formed on the solid content capturing surface of the filter 10. For example, the form of the solid content receiving member can be used from a relatively thin sheet shape to a relatively thick board shape, and may be a net shape. Further, for example, the width of the solid content receiving member may be a circumferential length of the lower half of the filter 10 arranged in an inclined manner or a longer length as shown in FIG. 1, or FIG. 2 and FIG. As shown in FIG. 3, the length may be less than the circumferential length of the lower half of the filter 10. For example, the length by which the solid content receiving member protrudes from the filter may be 10 to 50 mm as long as a deposited layer having a desired thickness is formed. Further, for example, the material of the solid content receiving member may be carbon steel, stainless steel, or the like.

  The thickness of the deposited layer formed by blocking the solid content by the solid content receiving member 3 is not particularly limited as long as the object of the present invention is achieved. For example, the deposited layer is based on the solid content capturing surface of the filter 10. The thickness may be 5 to 100 mm. In particular, when the present apparatus is used in a method for producing ashless coal, the thickness of the deposited layer is preferably 10 to 50 mm.

  The lid 4 seals the upper end of the settling tank 1 and is installed when desired, and is useful when it is necessary to heat or pressurize the slurry.

  The slurry supply pipe 5 is usually installed and supplies slurry into the sedimentation tank 1. In FIG. 1, the slurry supply pipe 5 extends through the lid portion 4 and extends to the lower or central portion of the slurry accommodated in the sedimentation tank 1, but in the same manner as the supernatant liquid discharge pipe 2, You may penetrate in the side wall of the tank 1. FIG.

  The solid content concentrate discharge port 6 is for discharging the solid content concentrate separated in the settling tank, and is usually installed.

  Another example of the solid-liquid separator according to the present invention is schematically shown in FIGS. The same reference numerals as those in FIG. 1 attached in FIGS. 2 and 3 are common and indicate members having the same functions, and thus description thereof is omitted.

  2 (A) and 2 (B) is the same as the apparatus of FIGS. 1 (A) and 1 (B) except that the supernatant liquid discharge pipe 2 is provided through the side wall of the sedimentation tank 1. 2A is a schematic configuration diagram showing a cross-sectional configuration of an example of the solid-liquid separation device according to the present invention, and FIG. 2B is a schematic perspective view when the device of FIG. 2A is viewed from above. It is a figure, Comprising: It is for showing the positional relationship of each structural member.

  3 (A) and 3 (B), the sedimentation tank 1 is provided with an opening 20 of the supernatant liquid discharge pipe 2, and the sedimentation tank 1 and the opening 20 are integrated. The apparatus is the same as the apparatus shown in FIGS. 1A and 1B except that the liquid discharge pipe 2 is penetrated in the side wall of the settling tank 1 as a result and the width of the solid content receiving member 3 is reduced. 3A is a schematic configuration diagram showing a cross-sectional configuration of an example of the solid-liquid separation device according to the present invention, and FIG. 3B is a schematic perspective view of the device of FIG. 3A viewed from above. It is a figure, Comprising: It is for showing the positional relationship of each structural member.

  The solid-liquid separation device 50 according to the present invention supplies the supernatant liquid from the supernatant liquid discharge pipe 2 while supplying the slurry continuously into the sedimentation tank 1 by the slurry supply pipe 5, and converts the solid content concentrate to the solid-liquid concentrate. By continuously discharging from the discharge port 6, a continuous separation process is possible.

  In the solid-liquid separation method according to the present invention, the above-described solid-liquid separation device 50 is used to precipitate the solid content in the slurry and separate the supernatant liquid and the solid content concentrate. Specifically, as described above, in the process of filtering and discharging the supernatant liquid, the solid content deposition layer 22 is formed on the filter 10 installed to be inclined with respect to the horizontal plane by the support by the solid content receiving member 3. The Therefore, while achieving a longer life of the filter, the supernatant liquid can be discharged through the solid content deposition layer 22 and the filter 10, and a supernatant liquid from which the solid content has been sufficiently removed can be obtained. .

  The time for maintaining the slurry in the solid-liquid separator 50 is a time required for separating the slurry into a supernatant and a solid concentrate, and is not particularly limited, but in the present invention, it is 30 to 300. Sufficient separation can be achieved in minutes. In particular, when the present apparatus is used in a method for producing ashless coal, the maintenance time is preferably 60 to 180 minutes.

  The solid-liquid separator 50 can be heated or / and pressurized as desired. In particular, when this apparatus is used in a method for producing ashless coal, the heating temperature is preferably in the range of 300 to 420 ° C., and the pressure is preferably in the pressure range of 1 to 2 MPa.

  The supernatant liquid subjected to the solid-liquid separation process by such a method can reduce the solid content concentration to 0.1% by weight or less based on the total amount.

[Production method of ashless coal]
The method for producing ashless coal according to the present invention is a method for producing ashless coal by sufficiently removing solvent-insoluble components such as ash that are inevitably contained in the coal in a relatively small amount from the coal. . The method for producing ashless coal according to the present invention will be described in detail with reference to FIG. FIG. 4 is a schematic diagram showing an example of an ashless coal production apparatus for carrying out the ashless coal production method of the present invention.

  The method for producing ashless coal according to the present invention includes a slurry preparation step, an extraction step, a separation step, and an ashless coal acquisition step, and further includes a by-product coal acquisition step as desired. Hereinafter, each step will be described.

<Slurry preparation process>
The slurry preparation step is a step of preparing a slurry by mixing a coal raw material and a solvent, and is performed in a slurry preparation tank 51 in FIG.

  The coal raw material is not particularly limited, and for example, bituminous coal, subbituminous coal, lignite, and the like are used.

  Although there are various methods for classifying coal, JIS M 1002-1978 classifies them according to the calorific value and fuel ratio. Brown coal is an anhydrous ashless based calorific value of 5800 kcal / kg or more and less than 7300 kcal / kg, subbituminous coal is 7300 kcal / kg or more and less than 8100 kcal / kg, bituminous coal is 8100 kg / cal or more, and the fuel ratio is less than 4.

The calorific value specified by the coal classification method (JIS M 1002-1978) is a value calculated based on the following equation.
Calorific value (corrected anhydrous ashless base) = calorific value / (100-1.08 x ash-moisture) x 100
The fuel ratio defined by the coal classification method (JIS M 1002-1978) is a value calculated based on the following equation.
Fuel ratio = fixed oxygen / volatile matter

  A solvent will not be restrict | limited especially if coal can be melt | dissolved, For example, the oil component derived from coal is used preferably. The oil component derived from coal is an oil component born from coal, and as such an oil component derived from coal, for example, a non-hydrogen donating solvent mainly containing a bicyclic aromatic compound is preferably used.

  The non-hydrogen donating solvent is a coal derivative which is a solvent mainly composed of a bicyclic aromatic compound purified mainly from a carbonization product of coal. Since this non-hydrogen donating solvent is stable even in a heated state and has excellent affinity with coal, 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 methods such as distillation. The recovered solvent can be recycled for improving economic efficiency.

  The main components of the non-hydrogen donating solvent include naphthalene, methylnaphthalene, dimethylnaphthalene, trimethylnaphthalene and the like, which are bicyclic aromatic compounds, and other naphthalenes having an aliphatic side chain, biphenyl, Alkylbenzenes with long aliphatic side chains are included.

  The boiling point of the solvent is not particularly limited. For example, from the viewpoint of pressure reduction from the extraction step to the separation step, extraction rate in the extraction step and solvent recovery rate in the ashless coal acquisition step, 180 to 300 ° C, In particular, those having a temperature of 230 to 280 ° C. are preferably used.

  The density | concentration of the coal raw material with respect to a solvent is not restrict | limited in particular, Usually, the range of 10-50 weight% is preferable on a dry coal basis, and the range of 15-35 weight% is more preferable.

  In order to prevent the extracted solute from precipitating, the temperature is preferably about the same as the extraction temperature, and is used in the range of 300 to 420 ° C. when used in an ashless coal production method.

<Extraction process>
The extraction step is a step of heating the slurry obtained in the slurry preparation step to extract a coal component soluble in a solvent (solvent soluble component). In FIG. To be implemented. Specifically, the slurry prepared in the slurry preparation tank 51 is once supplied to the preheater 53 by the pump 52 and heated to a predetermined temperature, then supplied to the extraction tank 54 and stirred at the predetermined temperature while being stirred by the stirrer 60. And extraction is performed.

The heating temperature of the slurry in the extraction step is not particularly limited as long as the solvent-soluble component can be dissolved. For example, from the viewpoint of sufficient extraction of the solvent-soluble component, it is preferably 300 to 420 ° C., particularly 350 to The range is 400 ° C.
The heating time (extraction time) is also not particularly limited, but is preferably 5 to 60 minutes from the viewpoint of sufficient dissolution and extraction rate, and particularly 20 to 40 minutes. The heating time is the sum of the heating times in the preheater 53 and the extraction tank 54 in FIG.

  The extraction step is preferably performed in the presence of an inert gas. This is because contact with oxygen in the extraction process is dangerous because it may ignite, and when hydrogen is used, the cost increases. As the inert gas used in the extraction step, inexpensive nitrogen is preferably used, but is not particularly limited.

  The pressure in the extraction step is preferably 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. When the pressure is lower than the vapor pressure of the solvent, the solvent is volatilized and is not trapped in the liquid phase and cannot be extracted. In order 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.

<Separation process>
The separation step is a step of separating the supernatant and the solid concentrate from the slurry obtained in the extraction step using the solid-liquid separation device 50 described above. In this method, the supernatant liquid is a solution portion in which a solvent-soluble component is dissolved, and the solid content concentrate is a slurry portion containing a solvent-insoluble component. In this separation step, a supernatant from which solvent-insoluble components as solid components have been sufficiently removed is obtained, and the filter is prevented from being clogged for a relatively long period of time. The mechanism is considered to be based on the mechanism described above.

  The solvent-insoluble component corresponds to the solid content described above, and even when coal is dissolved / extracted with a solvent, the ash remaining without being dissolved in the solvent or coal containing the ash (that is, by-product coal), etc. It is a coal component. On the other hand, the solvent-soluble component is a coal component that can be dissolved in a solvent, and is mainly derived from an organic component contained in the coal.

  The supernatant discharged from the solid-liquid separator 50 is discharged to the solvent separator 57 and the solid content concentrate is discharged to the solvent separator 58.

<Ashless coal acquisition process>
The ashless coal acquisition step is a step of obtaining ashless coal which is ashless coal by separating the solvent from the supernatant liquid separated in the separation step, and is performed by the solvent separator 57 in FIG.

  As a method for separating the solvent from the supernatant, a general distillation method or evaporation method (spray drying method, etc.) can be used, and the separated and recovered solvent should be circulated to the slurry preparation tank for repeated use. Can do. By separating and collecting the solvent, ashless coal (HPC) substantially free of ash can be obtained from the supernatant. Ashless coal contains little ash, has no moisture, and exhibits a higher calorific value than raw coal, such as steam coal. Furthermore, the softening and melting property, which is a particularly important quality as a raw material for coke for iron making, is greatly improved, and performance (fluidity) far superior to that of raw coal, for example, general coal. Therefore, ashless coal can be used as a blended coal for coke raw materials. Moreover, it can also be used as a combination charcoal by mixing with the byproduct charcoal mentioned later.

<By-product coal acquisition process>
The byproduct charcoal acquisition step is performed as necessary, and is a step of separating the solvent from the solid content concentrate separated in the separation step to obtain byproduct charcoal, and is performed by the solvent separator 58 in FIG. .

  The method for separating the solvent from the solid concentrate can use a general distillation method or evaporation method as in the above-described ashless coal acquisition step, and the separated and recovered solvent is transferred to the slurry preparation tank. It can be used repeatedly in circulation. By separation and recovery of the solvent, by-product coal (RC) in which solvent-insoluble components including ash and the like are concentrated can be obtained from the solid concentrate. By-product charcoal contains ash, but has no water and has a sufficient calorific value. Although the by-product coal does not show softening and melting properties, 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. It is not a thing. Therefore, 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 production method of ashless coal according to the present invention is as described above. However, in carrying out the present invention, for example, a coal raw material between or before and after each step within a range that does not adversely affect each step. Other steps such as a coal pulverizing step for pulverizing the ash, a removing step for removing unnecessary materials such as dust, and a drying step for drying the obtained ashless coal may be included.

  The solid-liquid separation device and the solid-liquid separation method according to the present invention are useful for separating a supernatant liquid and a solid content concentrate from a slurry in which a solid content is dispersed in an oily or aqueous solvent. The solid-liquid separation apparatus and solid-liquid separation method according to the present invention are particularly suitable for separation of slurry for producing ashless coal. The slurry for producing ashless coal is a slurry obtained by heating and extracting coal in a solvent in order to produce ashless coal.

  The ashless coal produced by the method for producing ashless coal according to the present invention is useful as a raw material for thermal power generation and boiler fuel, a high-efficiency combined power generation system, and iron-making coke.

(A) is a schematic block diagram which shows the cross-sectional structure of an example of the solid-liquid separator which concerns on this invention, (B) is a schematic perspective view when the apparatus of (A) is seen from upper direction, Comprising: It is for showing the positional relationship of the structural members. (A) is a schematic block diagram which shows the cross-sectional structure of an example of the solid-liquid separator which concerns on this invention, (B) is a schematic perspective view when the apparatus of (A) is seen from upper direction, Comprising: It is for showing the positional relationship of the structural members. (A) is a schematic block diagram which shows the cross-sectional structure of an example of the solid-liquid separator which concerns on this invention, (B) is a schematic perspective view when the apparatus of (A) is seen from upper direction, Comprising: It is for showing the positional relationship of the structural members. It is a schematic diagram of the manufacturing apparatus for demonstrating each process in the manufacturing method of ashless coal which concerns on this invention. It is a schematic diagram of the manufacturing apparatus for demonstrating each process in the manufacturing method of the conventional ashless coal. It is a schematic block diagram for demonstrating in detail the gravity sedimentation tank and filter unit in FIG.

Explanation of symbols

  1: sedimentation tank, 2: supernatant liquid discharge pipe, 3: solid content receiving member, 4: lid, 5: slurry supply pipe, 6: solid content liquid discharge port, 10: filter, 20: opening, 22: Solid content deposition layer, 50: solid-liquid separator of the present invention, 51: slurry preparation tank, 52: pump, 53: preheater, 54: extraction tank, 57:58: solvent separator, 60: stirrer, 101: Slurry preparation tank, 103: Preheater, 104: Extraction tank, 105: Gravity settling tank, 106: Filter unit, 107: 108: Solvent separator.

Claims (3)

A solid-liquid separation device that separates a supernatant liquid and a solid concentration liquid by sedimenting a solid content in a slurry,
A settling tank containing the slurry and settling solids;
A supernatant discharge pipe having an opening for allowing the supernatant in the settling tank to flow in, and for discharging the introduced supernatant to the outside of the settling tank;
A filter that is installed at the opening of the supernatant liquid discharge pipe and captures the solid content in the supernatant liquid, and is disposed so that the solid content capture surface faces the slurry liquid surface and is inclined with respect to the horizontal plane. A solid content receiving member that is disposed at the lower end of the filter and supports the solid content captured on the solid content capturing surface of the filter to form a solid content accumulation layer ;
A solid-liquid separation device comprising: A solid-liquid separation method using the solid-liquid separation device according to claim 1 to settle a solid content in a slurry and separate a supernatant liquid and a solid content concentrate,
A solid deposit layer is formed on a filter installed at an inclination with respect to a horizontal plane by a solid content receiving member, and a supernatant liquid is passed through the solid deposit layer and the filter to be discharged. Solid-liquid separation method. A slurry preparation step of preparing a slurry by mixing a coal raw material and a solvent;
An extraction step of heating the slurry obtained in the slurry preparation step to extract a coal component soluble in a solvent;
A separation step of separating the supernatant and the solid concentrate from the slurry obtained in the extraction step by the solid-liquid separation device according to claim 1; and separating the solvent from the supernatant separated in the separation step Ashless coal acquisition process to obtain ashless coal;
The manufacturing method of the ashless coal characterized by including.

Images