JP2012172076A - Coal upgrading system, dewatering system of carbon-containing substance, and solvent circulation system for upgrading of carbon-containing substance - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a coal upgrading system that can upgrade low grade coal by a method which excels in thermal efficiency and prevents coal dust occurrence, and that reduces spontaneously combustible property of the resultant upgraded coal; and to provide a dewatering system for the carbon-containing substance and a solvent circulation system suitable for the coal upgrading system.SOLUTION: This coal upgrading system includes: a dewatering means 20 which dewaters low grade coal; an upgrading tower 40 which upgrades the dewatered low grade coal by heating at a temperature of ≥300°C in the presence of a solvent; a solid-liquid separator 50 which separates the upgraded low grade coal and solvent into a solid phase and a liquid phase; and molding means 60, 62 and 66 which heat and mold the solid phase to obtain a molded product containing the upgraded coal. The dewatering means 20 includes: a slurrying tank 10 which blends the low grade coal with the solvent to conduct slurrying; and a dewatering tower 20 which dewaters the slurry raw material to be moisture-free by heating to a temperature of ≥100°C. Moreover, the coal upgrading system includes a solvent generating means 70 which generates the solvent by decomposing at least partially the liquid phase separated from the solid phase.

Description

  The present invention relates to a coal reforming system, and more particularly to a coal reforming system for reforming low-grade coal having a high water content such as lignite and subbituminous coal.

  Low-grade coal with high water content such as lignite and sub-bituminous coal has a large reserve, but has a low calorific value per unit weight and poor transport efficiency. In addition to increasing the amount of heat generated, the handleability is improved by compression molding. A coal reforming apparatus for reforming such low-grade coal is disclosed in US Pat. No. 5,401,364.

  The coal reformer described in this document includes a dryer that evaporates and removes moisture from low-grade coal by hot air drying, and a carbonizer that heats and dries the dried coal at 350 to 550 ° C. However, such hot air drying requires a great amount of energy and power, and has a problem of high equipment construction costs. In addition, coal whose water has been evaporated by such drying becomes porous coal, has high pyrophoric properties, and inactivation treatment is indispensable, but the inactivation technology itself has not yet been established. There is also a problem. Furthermore, when briquetting pulverized coal or product charcoal generated in the process of drying and dry distillation for the purpose of preventing the generation of charcoal dust and preventing spontaneous ignition by reducing the surface area, there is a limit to the scale up of briquetters. There is a problem that a large number is required and a large amount of power is consumed.

  On the other hand, in JP-A-2005-120185 and Japanese Patent No. 3920899, coal is mixed with an extraction solvent and heated to 300 ° C. or higher to extract the extracted coal from the coal in the extraction solvent. Describes a method for reforming slag into ashless coal. These publications do not particularly describe an effective utilization method for the remaining coal after extracting the extracted coal.

US Pat. No. 5,401,364 Japanese Patent Laid-Open No. 2005-120185 Japanese Patent No. 3920899

  In view of the above-mentioned problems, the present invention can improve low-grade coal with a method that prevents the generation of coal dust with excellent thermal efficiency, and can reduce the pyrophoricity of the obtained modified coal. It aims to provide a coal reforming system.

  In addition, the present invention is used not only for low-grade coal, but also for removing moisture from a carbon-containing material such as wood by a method that has excellent thermal efficiency and prevents generation of coal dust. Another object of the present invention is to provide a dehydration system for carbon-containing materials that can be used.

  Furthermore, the present invention provides a solvent circulation system that can be used in this coal reforming system as well as the solvent used for reforming carbon-containing substances such as wood, not limited to low-grade coal. That is another purpose.

  In order to achieve the above object, a coal reforming system according to the present invention comprises a means for dehydrating low-grade coal and a means for reforming the dehydrated low-grade coal by heating to 300 ° C. or higher in the presence of a solvent. And means for solid-liquid separation of the modified low-grade coal and solvent, and means for heating and molding the solid-liquid separated solid phase to obtain a molded product containing the modified coal.

  The dehydrating means is preferably a means for dehydrating without evaporating in the presence of the solvent, and the raw slurry obtained by mixing the low-grade coal and the solvent into a slurry is heated to 100 to 200 ° C. or higher. Thus, it is more preferable that the water contained in the low-grade coal is released in a liquid state. The reforming means is heated under pressure conditions where the solvent does not evaporate.

  In another aspect, the present invention is a dehydration system for a carbon-containing material, wherein the carbon-containing raw material and a solvent are mixed to form a slurry, and the raw material slurry is heated to 100 ° C. or higher. And a means for releasing and dehydrating moisture contained in the low-grade coal.

  The carbon-containing substance dehydration system of the present invention preferably further comprises means for separating the light phase of water released by the dehydration means from the heavy phase containing the raw slurry.

  Further, the present invention provides a solvent circulation system comprising a means for reforming a carbon-containing raw material by heating to 300 ° C. or higher in the presence of a solvent, a means for solid-liquid separation of the modified carbon-containing raw material and the solvent, And means for decomposing at least a part of the separated liquid phase to produce the solvent.

  As described above, according to the present invention, the low-grade coal is heated to 100 to 200 ° C. in the presence of the solvent, so that the water contained in the low-grade coal is released in a liquid state in the solvent, so that it is not evaporated. Can be easily dehydrated with excellent thermal efficiency, and if heated to 300 ° C or higher, low-grade coal is reformed and part of the hydrocarbons in the coal dissolves in the solvent. By forming the modified coal with the charcoal and the dissolved component, the pores of the porous modified coal are closed with the dissolved component, so that the modified coal with low spontaneous ignition can be obtained. In addition, carbon-containing materials such as low-grade coal as a raw material are dehydrated and modified in a solvent, so that generation of coal dust can be prevented.

It is a mimetic diagram showing one embodiment of a coal reforming system concerning the present invention. It is a schematic diagram which shows one Embodiment of the solvent production | generation equipment of FIG. It is the schematic diagram from which the water | moisture content contained in coal is removed, (a) shows the method of this invention, (b) shows a conventional method. It is a schematic diagram of the autoclave apparatus used for the test. It is the figure which plotted the composition of each product on the coal band. It is a graph which shows the yield of each product. It is a graph which shows the change of the emitted-heat amount of each coal before and behind a process. It is a graph which shows the breakdown of the emitted-heat amount after a process. It is a H-NMR spectrum of a normal temperature solid dissolution component and a normal temperature liquid dissolution component. It is a graph which shows the aromatic index of a normal temperature solid melt | dissolution component and a normal temperature liquid melt component. It is a graph which shows the change of the form of carbon before and behind processing. It is a graph which shows the thermogravimetric analysis curve of each product. It is a graph which shows the thermomechanical analysis curve of each product.

  Hereinafter, an embodiment of a coal reforming system according to the present invention will be described with reference to the accompanying drawings. The coal reforming system according to the present embodiment includes each embodiment of the dehydration system and the solvent circulation system according to the present invention, and the dehydration system and the solvent circulation system according to the present invention include the coal reforming system. It is not limited to the use of.

  As shown in FIG. 1, the coal reforming system of the present embodiment is a slurrying tank 10 that mixes slurry as a raw material coal and a solvent, and releases moisture from the coal in the raw slurry. A dehydration tower 20 for performing dehydration, an oil / water separation tank 30 for oil-water separation of a water phase and a raw material slurry (oil content) phase, a reforming tower 40 for reforming the separated raw material slurry by heating, and reforming A solid-liquid separator 50 that solid-liquid separates the raw slurry and a pelletizer 60 that shapes the separated solid phase into pellets to form modified coal pellets are mainly provided.

  The slurrying tank 10 is not particularly limited as long as it can uniformly disperse coal as a raw material in a solvent to form a slurry, but a slurry tank 10 provided with a stirrer 12 as shown in FIG. 1 is preferable. The slurrying tank 10 includes a raw material slurry supply pipe 16 that sends the slurryed raw material slurry to the dehydrating tower 20 at the bottom thereof. The raw slurry supply pipe 16 is provided with a pump 18 for pumping the raw slurry and a preheater 22 for heating the raw slurry. The preheater 22 is a device that can heat the raw slurry to a range of 100 to 200 ° C. The pump 18 is a device that can pressurize the raw material slurry in the range of 0.5 to 10 MPaG.

  The dehydration tower 20 is an apparatus that performs dehydration by maintaining the raw slurry at a predetermined temperature and releasing the water contained in the coal dispersed in the raw slurry into a liquid state. The dehydration tower 20 includes a dehydrated product supply pipe 28 for sending the dehydrated product to the oil / water separation tank 30 at the top of the tower, and a raw slurry supply pipe 16 for supplying the raw slurry into the tower at the bottom of the tower. The dehydration tower 20 preferably has a capacity such that the raw slurry supplied from the bottom stays in the tower for a sufficient amount of time until the slurry is discharged from the top. Of course, the dehydration tower 20 is not limited to such a continuous structure, and may be a batch system. Moreover, it is preferable that the dehydration tower 20 has a pressure | voltage resistant structure so that a high voltage | pressure raw material slurry can be accommodated.

  The oil / water separation tank 30 is an apparatus for removing the aqueous phase by separating the dehydrated product into an aqueous phase and an oil phase because the dehydrated product contains moisture released from coal and the oil content of the raw slurry. The water phase has a lighter specific gravity than the oil phase of the raw material slurry, and an aqueous phase (light layer) is formed on the oil phase (heavy layer). Therefore, the aqueous phase can be easily removed by decantation. The oil / water separation tank 30 is provided with a weir 31 that bisects the inside of the tank, and in one section, a dehydrated product supply pipe 28 that supplies the dehydrated product into the tank, and the separated oil phase is reformed by the reforming tower 40. An oil phase supply pipe 32 is provided for feeding the water phase to the waste water treatment facility (not shown) in the other section. The section to which the dehydrated product is fed preferably has a capacity such that the dehydrated product stays for a time sufficient to separate into an aqueous phase and an oil phase. Of course, the oil / water separation tank 30 is not limited to such a continuous structure, and may be a batch type.

  The oil phase supply pipe 32 is provided with a heat exchanger 34 for exchanging heat between the reformed slurry and the oil phase, which will be described later, and a heating furnace 44 for further heating the oil phase in order from the oil / water separation tank 30 side. The heating furnace 44 is an apparatus capable of heating the oil phase to a range of 250 to 450 ° C. The oil phase supply pipe 32 is provided with a pump 33 for pumping the oil phase. The pump 33 is a device that can pressurize the oil phase in a range of 0.5 to 10 MPaG. The water phase discharge pipe 36 is provided with a cooler 37 for cooling the water phase.

  The reforming tower 40 maintains the oil phase (raw material slurry from which water has been removed) at a predetermined temperature, and converts oxygen-containing functional groups (—OH, —COOH, etc.) present in the coal dispersed in the raw material slurry to carbon dioxide. It is an apparatus that reforms low-grade coal by decomposing into carbon and water and releasing it. By this reforming treatment, part of the hydrocarbons contained in the coal is dissolved in the solvent.

  The reforming tower 40 includes an oil phase supply pipe 32 for supplying an oil phase into the tower at the top of the tower and an exhaust pipe 49 for discharging carbon dioxide and water vapor from the inside of the tower. A reforming slurry supply pipe 46 for feeding the reforming slurry to the solid-liquid separator 50 is provided. The modified slurry supply pipe 46 is provided with a heat exchanger 34 for the oil phase described above and a cooler 47 for cooling the modified slurry to, for example, room temperature.

  The solid-liquid separator 50 is an apparatus that separates the solid phase and the liquid phase of the modified slurry. The solid-liquid separator 50 is not particularly limited, and for example, a filtration device such as a belt filter or a drum filter, a centrifugal separator, or the like can be used. The solid-liquid separator 50 includes a solvent circulation pipe 52 that sends the separated liquid phase to the slurrying tank 10, a solid phase supply line 54 that sends the separated solid phase (including sludge) to the pelletizer 60, and solid-liquid separation. An exhaust pipe 56 for discharging the gas phase generated at the time is provided. The solvent circulation pipe 52 is provided with a pump 53 for pumping the liquid phase.

  In addition, the liquid phase contains a solvent and a component dissolved from coal and liquid at room temperature (room temperature liquid dissolved component). If necessary, the room temperature liquid dissolved component is thermally decomposed. For example, a solvent generating facility 70 that decomposes into low molecular weight hydrocarbons and has the same components as the solvent can be installed. The solvent generation facility 70 is disposed in an extraction pipe 72 that extracts a part of the liquid phase from the solvent circulation pipe 52.

  As shown in FIG. 2, the solvent generation facility 70 includes, as shown in FIG. 2, a distillation column 73 that separates the extracted liquid phase into a solvent and a room temperature liquid dissolved component, and the separated room temperature liquid dissolved component as a solvent. And a pyrolysis furnace 76 that pyrolyzes them. Between the distillation column 73 and the pyrolysis furnace 76, a circulation path 74 for thermally decomposing the normal temperature liquid dissolved component separated by distillation and returning it to the distillation tower 73 is provided, and a pump 77 is provided in the circulation path 74. The distillation column 75 is provided with a gas discharge path 75 for discharging a gas containing the separated solvent, and a heat exchanger 81 and a condenser 78 are disposed in the gas discharge path 75. The condenser 78 is provided with a solvent supply path 80 for supplying the condensed solvent to the slurrying tank 10, and the solvent supply path 80 is provided with a pump 79. The solvent supply path 80 can also return a part of the solvent to the distillation column 73.

  The solid phase supply line 54 is provided with a heater 62 for heating the solid phase and a kneader 66 for kneading the heated solid phase in this order from the solid-liquid separator 50 side. The heater 62 is a device that can heat the solid phase in the range of 150 to 250 ° C. The kneader 66 is not particularly limited as long as it can knead a part of the solid phase melted by heating at a predetermined temperature.

  The pelletizer 60 is an apparatus for extruding the kneaded material into pellets of a predetermined size, and for example, an under water cutter method or a strand cutter method can be adopted. In the case of a strand cutter system, it has equipment such as a die pump, a die, and a water circulation type strand cooling tank.

  In addition, in the slurrying tank 10, the dehydration tower 20, the reforming tower 40, and each pipe, the thermometers 14, 24, 41, 48, and 64 for measuring the temperature of the object to be processed and the pressure of the object to be processed are measured. Pressure gauges 26 and 42 are provided.

  According to the above configuration, first, coal and a solvent as raw materials are supplied to the slurrying tank 10. As the coal, for example, low-grade coal having a moisture content of 15 to 70%, preferably 40 to 70%, such as lignite, lignite, subbituminous coal, and peat is used. Moreover, it is preferable to grind | pulverize the raw material to supply in a modification | reformation process. For pulverization, for example, the particle size is preferably 4 mm or less, more preferably 2 mm or less.

  The solvent is not particularly limited as long as it is a stable substance even when heated to the temperature of the reforming treatment. In addition to the native solvent, for example, 1-methylnaphthalene, dimethylnaphthalene, naphthalene, anthracene, C12 to C19 dodecanes An organic solvent such as can be used. If it is not an indigenous solvent, it is necessary to regenerate and manufacture the solvent that flows out of the system as a loss. The mixing ratio of coal and solvent is preferably such that the solid content concentration of the resulting slurry is 20 to 65%, more preferably 50 to 65%.

  In the slurrying tank 10, the mixture is agitated with a stirrer 12 so that the pulverized coal is uniformly dispersed in the supplied solvent. The temperature of the slurrying tank 10 may be from room temperature (25 ° C.) to 40 ° C. The raw material slurry in which the coal is dispersed in the solvent is sent to the dehydration tower 20 through the raw material slurry supply pipe 16. At this time, the raw material slurry is heated by the pump 18 and the preheater 22 to a pressure of 0.5 to 10 MPaG, preferably 0.8 to 5 MPaG, and at a temperature of 100 to 200 ° C., preferably 130 to 170 ° C. To do.

  In the dehydrating tower 20, the raw slurry slowly flows from the tower bottom to the tower top at a predetermined temperature, during which moisture in the coal is liberated in the solvent. FIG. 3 (a) shows a schematic diagram in which moisture contained in coal is liberated in the solvent by this method. Moreover, the schematic diagram of the behavior of coal at the time of drying by conventional hot air evaporation is shown in FIG.3 (b). As shown in FIG. 3 (b), in the conventional method, among the oxygen-containing functional groups present on the coal surface, the carboxyl group is thermally decomposed and polymerized, and the coal is linked by an ether bond (—O—). In contrast, in the present invention, as shown in FIG. 3 (a), the water in the coal can be released into the solvent in a liquid state without polymerizing the coal by thermal condensation.

  The residence time of the raw material slurry in the dehydration tower 20 is preferably 30 minutes to 2 hours. The dehydrated product obtained by dehydrating the raw slurry is sent from the bottom of the tower to the oil / water separation tank 30 through the dehydrated product supply pipe 28.

  In the oil / water separation tank 30, the dehydrated product is supplied to one section with the weir 31 as a boundary. While the water contained in the dehydrated product is stored in this section, it forms a water phase on the oil phase containing the raw slurry. And since this aqueous phase flows over the weir 31 and flows out into the other section, the aqueous phase can be separated and removed from the oil phase containing the raw slurry. The aqueous phase is cooled to room temperature by a cooler 37 and then sent to a wastewater treatment facility (not shown) via an aqueous phase discharge pipe 36.

  Thus, since the water in the low-grade coal can be separated in a liquid state without being evaporated as in the prior art, it can be dehydrated with high thermal efficiency. Conventionally, hot air drying has been used to evaporate moisture, but hot air drying requires a fan that requires a large amount of power. However, according to the dehydration method of the present invention, power consumption is reduced. be able to.

  The raw material slurry from which the moisture in the coal has been dehydrated and removed is sent to the reforming tower 40 through the oil phase supply pipe 32 as an oil phase. At that time, the oil phase is pressurized to 0.5 to 10 MPaG, preferably 0.8 to 5 MPaG, and the temperature is 250 to 400 ° C., preferably 330, by the pump 33, the heat exchanger 34 and the heating furnace 44. Heat to ~ 370 ° C.

  In the reforming tower 40, the raw material slurry slowly flows from the top to the bottom of the tower at a predetermined temperature, while the carboxyl groups present in the coal are decomposed and converted to carbon dioxide. Therefore, since the oxygen content contained in the coal can be removed without polymerization between the coals, the calorific value is greatly improved, and the low-grade coal can be reformed. In addition, by the treatment in the reforming tower 40, a part of the hydrocarbons contained in the coal is dissolved in the solvent. The residence time of the raw material slurry in the reforming tower 40 is preferably 30 minutes to 2 hours. The gas containing carbon dioxide and water vapor generated by the reforming process is discharged out of the system through the exhaust pipe 49.

  The reformed slurry modified in the reforming tower 40 is extracted from the bottom of the tower through the reforming slurry supply pipe 46, cooled to room temperature to 50 ° C. by the heat exchanger 34 and the cooler 47, and then solidified. Send to liquid separator 50. The solvent in the reformed slurry contains a dissolved component from coal. This dissolved component is cooled to room temperature and a component that precipitates at about 150 ° C. or lower (room temperature solid dissolved component). There are two types of liquid components (room temperature liquid dissolved components). Therefore, in the solid-liquid separator 50, it can isolate | separate into the solid phase containing a modified coal and a normal temperature solid solution component, and the liquid phase containing a solvent and a normal temperature liquid solution component. In addition, since the gas containing carbon dioxide is generated by cooling the reforming slurry, it is discharged out of the system through the exhaust pipe 56.

  The solid phase (including sludge) separated by the solid-liquid separator 50 is first introduced into the heater 62 via the solid phase supply line 54. In the heater 62, by heating the solid phase to 150 ° C. or higher, the reformed coal in the solid phase remains solid, but the room temperature solid dissolved component melts. As a result, a melt of the solid reformed coal and the molten room temperature solid dissolved component is generated. In addition, it is preferable that the upper limit of heating shall be 250 degrees C or less from a viewpoint of volatilization of a normal temperature solid melted component, and the heat resistance of an installation. This melt is introduced into the kneader 66 and mixed uniformly, and then supplied to the pelletizer 60 to form the melt into pellets. The size of the pellet is preferably a cylindrical shape having a diameter of 20 to 30 mm and a length of 30 to 40 mm, for example. After molding, the modified charcoal pellets are naturally cooled to room temperature. If the viscosity of the melt is too high, a part of the room temperature liquid dissolved component may remain in the solid phase.

  In the modified pellets thus obtained, the pores of the porous modified coal are closed by the room temperature solid dissolved component, and the surface area of the modified coal can be reduced. Therefore, the modified pellet can greatly suppress the spontaneous ignition compared with the conventional hot air drying, and the conventional inactivation step and stabilization step can be made unnecessary. Further, in the present invention, in a series of steps, the coal is handled in a solvent, and the solid phase obtained by the solid-liquid separator 50 is immediately heated to partially melt, so that the coal dust is scattered. Can be avoided, and measures for that can be eliminated.

  On the other hand, the liquid phase separated by the solid-liquid separator 50 is supplied to the slurrying tank 10 through the liquid phase circulation pipe 52 in order to reuse the solvent. When making up the loss of solvent that goes out of the system accompanying modified coal and room temperature solid dissolved components, room temperature liquid dissolved components contained in the liquid phase are products with high utility value such as ashless coal. Therefore, it is possible to thermally decompose the room temperature liquid dissolved component in the solvent generation facility 70 and supply the solvent generated thereby to the slurrying tank 10. Specifically, as shown in FIG. 2, first, the liquid phase is distilled in a distillation column 73 to separate a solvent-containing gas and a room temperature liquid dissolved component. The room-temperature liquid dissolved component is sent to the pyrolysis furnace 76 via the circulation path 74, where a solvent is generated by pyrolysis. The produced solvent is sent to the distillation column 73 via the circulation path 74. The gas containing the solvent is cooled by the heat exchanger 81 via the gas discharge path 75, and the solvent is condensed by the condenser 78. The solvent is supplied to the slurrying tank 10 via the solvent supply path 80. In addition, when the composition of the solvent is the same as that of the room temperature liquid dissolved component, the solvent generating equipment 70 is unnecessary.

  Although the present invention has been described using the embodiment shown in FIG. 1, the present invention is not limited to this, and other embodiments can be adopted. For example, FIG. 1 shows a continuous coal reforming system, but a batch method may be used. For example, slurrying, dehydration, and reforming can be performed in a single tank. Three tanks are used as one set, the first is slurried, the second is dehydrated, and the third is reformed. Next, the coal can be reformed in a batch system by sequentially switching so that the first group is dehydrated, the second group is reformed, and the third group is slurried.

  Using the autoclave apparatus shown in FIG. 4, a test for dewatering and reforming coal was conducted. The autoclave apparatus was charged with 14 g of coal on a daf basis in a wet state, and 300 mL of 1-methylnaphthalene was supplied by a pump. The coal was pulverized to a particle size of 1 mm or less. Table 1 shows the types of coal used.

  The temperature of the autoclave apparatus was increased at 50 ° C./min, and when the temperature reached 350 ° C., this temperature was maintained for 1 hour. When the pressure increased too much during the temperature rising process, the gas valve of the autoclave device was opened and water was extracted with steam. The final pressure was 2.3 MPa. Then, the valve | bulb of the lower part of an autoclave apparatus was opened, and the content was extracted to the reservoir | reserver connected with the pipe through the stainless steel filter with an opening of 0.5 micrometer. The extracted liquid product was allowed to cool to room temperature, and then filtered through a stainless steel filter having an opening of 0.5 μm to separate a filtrate and a filtrate. And the physical and chemical characteristic value was investigated about the residue in an autoclave apparatus, and the filtrate and filtrate.

  First, Table 2 shows the composition of the residue (modified coal), filtrate (room temperature solid dissolved component), and filtrate (room temperature liquid dissolved component) in each coal. As shown in Table 2, even when any coal was used, the room temperature liquid dissolved component had almost the same composition, and the room temperature solid dissolved component had almost the same composition. Moreover, the figure which plotted the composition of each product on the coal band is shown in FIG. As shown in FIG. 5, even when any coal is used, the room temperature solid dissolved component and the room temperature liquid dissolved component are substantially in the same position, which is not limited to coal, even in a carbon-containing material such as wood, It was found that dehydration, carbon dioxide release, and hydrocarbon release were similarly performed by the above treatment.

  Moreover, the yield of the residue, filtrate, filtrate, carbon dioxide, and water in each coal is shown in FIG. And the change of the calorific value of each coal before and behind the said process is shown in FIG. 7, and the breakdown of the calorific value after a process is shown in FIG. As shown in FIG. 6, a good mass balance was obtained with any coal. As shown in FIG. 7, the calorific value hardly changed by the above treatment, but rather showed a tendency to slightly increase.

  FIG. 9 and FIG. 10 show the results of the H-NMR spectrum and the aromatic index of the filtrate (room temperature solid dissolved component) and the filtrate (room temperature liquid dissolved component). As shown in FIG. 9 and FIG. 10, regardless of which coal is used, the room-temperature solid dissolved component has almost the same structure and aromatic index, and the room-temperature liquid dissolved component also has almost the same structure and fragrance. It was a tribe index.

  A visualization of changes in carbon morphology before and after the treatment is shown in FIG. It can be seen that the amount of oxygen-containing functional groups was greatly reduced by the above treatment. Further, it can be seen that the amount of aliphatic carbon is greatly reduced and the amount of aromatic carbon is greatly increased.

  FIG. 12 and FIG. 13 show the results of thermogravimetric analysis and thermomechanical analysis of raw material coal, residue, filtrate (room temperature solid dissolved component), and filtrate (room temperature liquid dissolved component). As shown in FIG. 12 and FIG. 13, the thermogravimetric analysis curve and the thermomechanical analysis curve of the room temperature solid dissolved component tend to be very similar regardless of which coal is used. The gravimetric analysis curve and the thermomechanical analysis curve showed a very similar tendency. Further, it was found that about 70% of the room temperature liquid dissolved component was volatilized by about 400 ° C., and that the room temperature liquid dissolved component was completely softened and melted before volatilizing at 100 ° C. or less.

  It was found that the liquid dissolved components at room temperature have substantially the same physical and chemical characteristic values regardless of the type of coal (C: 81.8 to 82.9%, H: 7.8 to 10. 2%, O: 7.8 to 10.2%). It did not contain any moisture. The molecular weight was as low as 100 to 500, and about 80% was a volatile component. Moreover, it completely softened and melted at 100 ° C. or lower. It was found that the liquid dissolved component at room temperature has the same characteristics as bituminous coal.

  It was found that the room temperature solid dissolved component had substantially the same physical and chemical characteristic values regardless of the type of coal (C: 75.6-77.5%, H: 5.0-5. 7%, O: 13.7 to 16.9%). It did not contain any moisture. The molecular weight was relatively low at 100 to 800, and it was completely softened and melted at about 200 to 250 ° C.

  The composition of the modified coal was different depending on the type of coal, but the oxygen content was relatively small in any coal. It contained almost no moisture.

DESCRIPTION OF SYMBOLS 10 Slurry tank 12 Stirrer 14, 24, 41, 48, 64 Thermometer 16 Raw material slurry supply pipe 18 Pump 20 Dehydration tower 22 Preheater 26, 42 Pressure gauge 28 Dehydration product supply pipe 30 Oil water separation tank 31 Weir 32 Oil Phase supply pipe 33 Pump 34 Heat exchanger 36 Water phase discharge pipe 37 Cooler 40 Reforming tower 44 Heating furnace 46 Reforming slurry supply pipe 47 Cooler 49 Exhaust pipe 50 Solid-liquid separator 52 Solvent circulation pipe 53 Pump 54 Solid phase Supply line 56 Exhaust pipe 60 Pelletizer 62 Heater 66 Kneading machine 70 Solvent generation equipment 72 Return pipe 73 Distillation tower 74 Circulation path 75 Gas discharge path 76 Pyrolysis furnace 77 Pump 78 Condenser 79 Pump 80 Solvent supply path 81 Heat exchanger

Claims (5)

  Means for dehydrating low-grade coal, means for reforming dehydrated low-grade coal by heating to 300 ° C. or higher in the presence of a solvent, means for solid-liquid separation of the reformed low-grade coal and solvent, A coal reforming system comprising: means for heating and molding a liquid-separated solid phase to obtain a molded product containing reformed coal.   The dehydration means is a means in which the water contained in the low-grade coal is released in a liquid state by heating the raw slurry obtained by mixing the low-grade coal and the solvent into a slurry to 100 to 200 ° C. or higher. The coal reforming system according to claim 1.   A means for mixing a carbon-containing raw material and a solvent to form a slurry, and a means for liberating and dehydrating water contained in the low-grade coal by heating the raw material slurry to 100 ° C. or higher. Dehydration system.   The carbon-containing material dehydration system according to claim 3, further comprising means for separating a light phase of water released by the dehydration means from a heavy phase containing the raw slurry.   A means for reforming the carbon-containing raw material by heating it to 300 ° C. or higher in the presence of a solvent, a means for solid-liquid separation of the modified carbon-containing raw material and the solvent, and decomposing at least part of the solid-liquid separated liquid phase And a means for producing the solvent.