WO2018216373A1 - Procédé de production de charbon sans cendres et dispositif de production de charbon sans cendres - Google Patents

Procédé de production de charbon sans cendres et dispositif de production de charbon sans cendres Download PDF

Info

Publication number
WO2018216373A1
WO2018216373A1 PCT/JP2018/014885 JP2018014885W WO2018216373A1 WO 2018216373 A1 WO2018216373 A1 WO 2018216373A1 JP 2018014885 W JP2018014885 W JP 2018014885W WO 2018216373 A1 WO2018216373 A1 WO 2018216373A1
Authority
WO
WIPO (PCT)
Prior art keywords
solvent
coal
heating
slurry
radical stabilizer
Prior art date
Application number
PCT/JP2018/014885
Other languages
English (en)
Japanese (ja)
Inventor
康爾 堺
憲幸 奥山
吉田　拓也
繁 木下
Original Assignee
株式会社神戸製鋼所
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 株式会社神戸製鋼所 filed Critical 株式会社神戸製鋼所
Priority to KR1020197036297A priority Critical patent/KR102291836B1/ko
Priority to CN201880033426.3A priority patent/CN110651027B/zh
Publication of WO2018216373A1 publication Critical patent/WO2018216373A1/fr

Links

Images

Classifications

    • 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
    • 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
    • C10L10/00—Use of additives to fuels or fires for particular purposes
    • 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

Definitions

  • the present invention relates to a method for producing ashless coal and an apparatus for producing ashless coal.
  • Coal is widely used as a raw material for thermal power generation and boiler fuel or chemicals.
  • HPC ash-free charcoal
  • Attempts have been made to use ash-free charcoal (HPC) 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.
  • a method for producing ashless coal As a method for producing ashless coal, a method of separating a solution containing a coal component soluble in a solvent (hereinafter also referred to as a solvent-soluble component) from a slurry using a gravity sedimentation method has been proposed (for example, JP, A 2005-120185).
  • This method includes a slurry preparation step in which coal and a solvent are mixed to prepare a slurry, and an extraction step in which the slurry obtained in the slurry preparation step is heated to extract a solvent-soluble component.
  • This method further includes a separation step of separating the solution in which the solvent-soluble component is dissolved from the slurry from which the solvent-soluble component has been extracted in the extraction step, and separating the solvent from the solution separated in the separation step to obtain ashless coal.
  • ashless coal is obtained by separating the solvent from a solution containing a coal component that is soluble in the solvent. Therefore, the yield of ashless coal depends on the proportion of coal components soluble in the solvent, that is, the extraction rate. For this reason, in order to raise the manufacture efficiency of ashless coal, the further improvement of this extraction rate is desired.
  • the present invention has been made based on the above circumstances, and an object thereof is to provide a method for producing ashless coal and an apparatus for producing ashless coal with an increased extraction rate.
  • the inventors of the present invention have found that the extraction rate of ashless coal can be increased by adding a radical stabilizer to the slurry before heating to extract the solvent-soluble component, and completed the present invention. This is presumably because the radical stabilizer can suppress polymerization due to polycondensation of coal radicals caused by heating the slurry.
  • the invention made in order to solve the above problems includes a step of heating a mixture of coal, a radical stabilizer and a solvent, and a component soluble in the solvent from the coal in the slurry obtained in the heating step.
  • An elution step a step of separating the slurry eluted in the elution step into a liquid component containing a solvent-soluble component and a solvent insoluble component, and a step of evaporating the solvent from the liquid component separated in the separation step.
  • a method for producing ashless coal is a method for producing ashless coal.
  • a radical stabilizer is added to the slurry before heating to extract solvent-soluble components. Since this radical stabilizer can suppress polymerization due to polycondensation of coal radicals caused by heating of the slurry, it is possible to increase the soluble components of coal eluted in the elution step. Therefore, the extraction rate of ashless coal can be increased by using the method for producing ashless coal.
  • the heating step may include a step of mixing coal, a radical stabilizer and a solvent, and a step of raising the temperature of the slurry obtained in the mixing step.
  • a step of mixing coal a radical stabilizer and a solvent
  • a step of raising the temperature of the slurry obtained in the mixing step by heating the slurry after mixing the radical stabilizer, the polymerization of coal radicals can be effectively suppressed, so that the extraction rate of ashless coal can be further increased.
  • the heating step includes a step of heating a solvent, a step of transporting the solvent heated in the solvent heating step to the elution step, and a step of supplying coal and a radical stabilizer to the solvent in the solvent transport step. It is good to have.
  • coal can be heated up rapidly and coal and a solvent can be stirred with the flow of a solvent.
  • coal can be melt
  • a radical stabilizer together with coal it is possible to effectively inhibit the polymerization of coal radicals, thereby further increasing the extraction rate of ashless coal.
  • the amount of the radical stabilizer added to coal on an anhydrous coal basis is preferably 0.045 mmol / g or more and 0.4 mmol / g or less.
  • the radical stabilizer is preferably an amine or an ammonium salt.
  • the extraction rate of ashless charcoal can further be raised by using the radical stabilizer as an amine or an ammonium salt.
  • the amine is preferably a monoamine, diamine or triamine.
  • the amine is preferably a monoamine, diamine or triamine.
  • Another invention made to solve the above-mentioned problems is a heating part for heating a mixture of coal, a radical stabilizer and a solvent, and a component soluble in the solvent from the coal in the slurry obtained in the heating part.
  • An elution part for elution, a solid-liquid separation part for separating the slurry after elution in the elution part into a liquid component containing a solvent-soluble component and a solvent-insoluble component, and the liquid component separated in the solid-liquid separation unit An ashless coal manufacturing apparatus including an evaporation separation unit that evaporates a solvent.
  • the said ashless coal manufacturing apparatus extracts the solvent-soluble component by heating the slurry to which the radical stabilizer is added in the heating section. Since this radical stabilizer can suppress polymerization due to the polycondensation of coal radicals caused by heating the slurry, it is possible to increase the soluble components of coal eluted in the elution part. Therefore, the extraction rate of ashless coal can be increased by using the ashless coal manufacturing apparatus.
  • ashless coal is a type of modified coal obtained by reforming coal, and a modified coal that removes ash and insoluble components from coal as much as possible using a solvent. It is.
  • the ashless coal may contain ash as long as the fluidity and expansibility of the ashless coal are not significantly impaired.
  • coal contains ash content of 7% by mass or more and 20% by mass or less, but ashless coal may contain ash content of about 2% by mass, and in some cases about 5% by mass.
  • “Ash” means a value measured in accordance with JIS-M8812: 2004.
  • the extraction rate of ashless coal can be increased by using the method and apparatus for producing ashless coal of the present invention.
  • the apparatus for producing ashless coal shown in FIG. 1 mainly includes a heating unit 1, an elution unit 2, a solid-liquid separation unit 3, a first solvent separation unit 4, and a second solvent separation unit 5.
  • the heating unit 1 includes a solvent tank 11, a pump 12, a preheater 13, and a feeder 14 that supplies coal and a radical stabilizer.
  • the heating unit 1 also includes a transport pipe 15 that transports the solvent in the solvent tank 11 to the elution unit 2.
  • the solvent tank 11 stores a solvent to be mixed with coal.
  • the solvent is not particularly limited as long as it dissolves coal.
  • a bicyclic aromatic compound derived from coal is preferably used. Since this bicyclic aromatic compound has a basic structure similar to the structural molecule of coal, it has a high affinity with coal and can obtain a relatively high extraction rate.
  • the bicyclic aromatic compound derived from coal include methyl naphthalene oil and naphthalene oil, which are distilled oils of by-products when carbon is produced by carbonization to produce coke.
  • the boiling point of the solvent is not particularly limited.
  • the lower limit of the boiling point of the solvent is preferably 180 ° C., more preferably 230 ° C.
  • the upper limit of the boiling point of the solvent is preferably 300 ° C and more preferably 280 ° C. If the boiling point of the solvent is less than the above lower limit, the solvent is likely to volatilize, and it may be difficult to adjust and maintain the mixing ratio of coal and solvent in the slurry. Conversely, if the boiling point of the solvent exceeds the upper limit, separation of the solvent-soluble component from the solvent becomes difficult, and the solvent recovery rate may be reduced.
  • the pump 12 is disposed in the transport pipe 15 and transports the solvent in the solvent tank 11 to the elution unit 2.
  • the type of the pump 12 is not particularly limited as long as the solvent can be pumped to the elution part 2 through the transport pipe 15, and for example, a positive displacement pump or a non-positive displacement pump can be used. More specifically, a diaphragm pump, a tube diaphragm pump, or the like can be used as the positive displacement pump, and a spiral pump or the like can be used as the non-positive displacement pump.
  • the lower limit of the pressure (the internal pressure of the conveying pipe 15) when the solvent is pumped to the elution part 2 by the pump 12 is preferably 1.1 MPa, and more preferably 1.5 MPa.
  • the upper limit of the internal pressure of the transport pipe 15 is preferably 5 MPa, and more preferably 4 MPa. If the internal pressure of the transport pipe 15 is less than the lower limit, the power of stirring the coal when the coal is supplied to the solvent being transported, which will be described later, becomes weak, so that the coal may not be sufficiently dissolved. Conversely, if the internal pressure of the transport pipe 15 exceeds the above upper limit, the effect of improving coal dissolution obtained with respect to an increase in the cost of manufacturing equipment for ensuring the pressure resistance required for the heating unit 1 may be insufficient. There is.
  • the said solvent conveyed by the pump 12 may be conveyed in a laminar flow state, it is good to be conveyed in a turbulent flow state.
  • a turbulent flow state By transporting the solvent in a turbulent state in this way, the force with which the solvent stirs the coal at the time of supplying the coal to the solvent being transported is increased, so that the coal is easily mixed with the solvent and the dissolution of the coal is promoted.
  • laminar flow state means a state where the Reynolds number Re is less than 2100
  • the “turbulent state” means a state where the Reynolds number Re is 2100 or more, more preferably, the Reynolds number Re is 4000 or more.
  • the lower limit of the flow rate of the solvent conveyed by the pump 12 is preferably 0.5 m / sec, and more preferably 1 m / sec.
  • the upper limit of the flow rate of the solvent is preferably 10 m / sec, and more preferably 5 m / sec.
  • the preheater 13 will not be specifically limited if the solvent which passes the inside of the preheater 13 can be heated, For example, a resistance heating type heater and an induction heating coil are mentioned. Moreover, you may heat using a heat medium.
  • a heating pipe is arranged around the solvent flow path that passes through the preheater 13, and the solvent passing through the preheater 13 can be heated by supplying a heating medium such as steam or oil to the heating pipe. .
  • the lower limit of the temperature of the solvent after heating by the preheater 13 is preferably 300 ° C, more preferably 350 ° C.
  • the upper limit of the temperature of the solvent is not particularly limited as long as it is a temperature at which elution is possible, but is preferably 480 ° C and more preferably 450 ° C. If the temperature of the solvent is lower than the lower limit, the binding between the molecules constituting the coal in the elution part 2 cannot be sufficiently weakened, and the elution rate may decrease. On the contrary, when the temperature of the solvent exceeds the upper limit, the amount of heat for maintaining the temperature of the solvent becomes unnecessarily large, which may increase the manufacturing cost.
  • the lower limit of the heating rate by the preheater 13 is preferably 10 ° C / min, and more preferably 20 ° C / min.
  • the upper limit of the heating rate is preferably 100 ° C./min, more preferably 50 ° C./min. If the heating rate is less than the lower limit, it takes time to heat the solvent to a predetermined temperature, which may reduce the production efficiency of ashless coal. On the other hand, when the heating rate exceeds the upper limit, energy for heating, costs for manufacturing equipment, and the like may increase unnecessarily.
  • the heating time by the preheater 13 is not particularly limited, but can be set to, for example, 10 minutes or more and 30 minutes or less because of the relationship between the temperature and the heating rate described above.
  • the supplier 14 supplies coal and a radical stabilizer to the transport pipe 15.
  • a known hopper such as a normal pressure hopper used in a normal pressure state or a pressure hopper used in a normal pressure state or a pressurized state can be used.
  • the coal and radical stabilizer are mixed and charged into the hopper.
  • coal As the coal supplied from the supply device 14, various quality coals can be used. As the coal, for example, bituminous coal having a high extraction rate of ashless coal or cheaper inferior quality coal (subbituminous coal or lignite) is preferably used. Further, when coal is classified by particle size, finely pulverized coal is preferably used.
  • finely pulverized coal means, for example, coal in which the mass ratio of coal having a particle size of less than 1 mm to the mass of the entire coal is 80% or more.
  • lump coal can also be used as coal supplied from the supply device 14.
  • particle size refers to a value measured in accordance with the JIS-Z8815 (1994) general screening test rules. For sorting according to the particle size of coal, for example, a metal mesh screen defined in JIS-Z8801-1 (2006) can be used.
  • the lower limit of the proportion of inferior coal in the whole coal to be supplied is preferably 80% by mass, and more preferably 90% by mass.
  • the lower limit of the carbon content of the inferior coal is preferably 70% by mass.
  • the upper limit of the carbon content of the inferior coal is preferably 85% by mass, and more preferably 82% by mass.
  • the radical stabilizer is mixed with the coal and charged into the feeder 14.
  • radical stabilizers examples include amine stabilizers and phenol stabilizers, among which amine stabilizers such as amines and ammonium salts are preferred, and amines are particularly preferred.
  • the amine is preferably a monoamine such as octadecylamine, a diamine such as N-alkyl-1,3-diaminopropane, or a triamine such as beef tallow dipropylenetriamine, and more preferably a monoamine.
  • the addition amount of the above-mentioned radical stabilizer to coal on an anhydrous carbon basis 0.045 mmol / g is preferred and 0.15 mmol / g is more preferred.
  • the upper limit of the amount of radical stabilizer added is preferably 0.4 mmol / g, more preferably 0.22 mmol / g. If the added amount of the radical stabilizer is less than the lower limit, the effect of improving the extraction rate of ashless coal may be insufficient. Conversely, if the amount of the radical stabilizer added exceeds the upper limit, the cost of the radical stabilizer may be too high for the effect of improving the extraction rate of ashless coal.
  • the mixture of coal and radical stabilizer should be preheated. By preheating the mixture, it is possible to prevent the temperature of the slurry from being lowered when the mixture is supplied to the transport pipe 15 and mixed with the solvent. Although it does not specifically limit as preheating temperature of the said mixture, For example, it can be 200 degreeC or more and 300 degrees C or less.
  • a mixture obtained by mixing a solvent into a slurry may be used as the mixture supplied from the supply device 14 to the transport pipe 15.
  • the coal and the radical stabilizer are easily mixed with the solvent in the transport pipe 15, and the coal can be dissolved more quickly.
  • the lower limit of the coal concentration on the basis of anhydrous carbon in the slurry is preferably 20% by mass, more preferably 30% by mass.
  • the upper limit of the coal concentration is preferably 70% by mass, and more preferably 60% by mass. If the coal concentration is less than the above lower limit, the elution amount of solvent-soluble components eluted in the elution part 2 to be described later decreases with respect to the slurry processing amount, which may reduce the production efficiency of ashless coal. . Conversely, if the coal concentration exceeds the upper limit, the effect of facilitating the mixing of coal and solvent by slurrying may be insufficient.
  • the transport pipe 15 transports the solvent in the solvent tank 11 to the elution unit 2. Further, the mixture of coal and radical stabilizer supplied from the supply device 14 to the transport pipe 15 is mixed with the heated solvent flowing in the transport pipe 15 in the transport pipe 15 and rapidly heated.
  • “rapid temperature rise” means heating at a heating rate of about 10 ° C./second or more and 500 ° C./second or less, for example.
  • the temperature of the slurry which is a mixture of the solvent, the coal, and the radical stabilizer, becomes a relatively uniform temperature within a few seconds to a few dozen seconds after the coal and the radical stabilizer are added.
  • the temperature of the slurry is lower than the temperature of the solvent after heating by the sensible heat of coal, for example, about 350 ° C. or more and 420 ° C. or less.
  • the lower limit of the coal concentration on the basis of anhydrous carbon in the slurry is preferably 5% by mass, and more preferably 10% by mass.
  • the upper limit of the coal concentration is preferably 40% by mass, and more preferably 30% by mass. If the coal concentration is less than the above lower limit, the elution amount of solvent-soluble components eluted in the elution part 2 to be described later decreases with respect to the slurry processing amount, which may reduce the production efficiency of ashless coal. . Conversely, if the coal concentration exceeds the upper limit, the solvent-soluble component is saturated in the solvent, and the elution rate of the solvent-soluble component may be reduced.
  • the elution part 2 elutes a coal component soluble in a solvent from the coal in the slurry obtained in the heating part 1.
  • the elution part 2 has an extraction tank 21.
  • the slurry is supplied to the extraction tank 21 from the transport pipe 15.
  • coal components soluble in the solvent are eluted from the coal while maintaining the temperature of the slurry.
  • the extraction tank 21 has a stirrer 21a. The elution can be promoted by stirring the slurry with the stirrer 21a.
  • the lower limit of the internal pressure of the extraction tank 21 is preferably 1.1 MPa, and more preferably 1.5 MPa.
  • the upper limit of the internal pressure of the extraction tank 21 is preferably 5 MPa, and more preferably 4 MPa.
  • the elution time in the elution part 2 is not particularly limited, but can be 10 minutes or more and 70 minutes or less from the viewpoint of the extraction amount of solvent-soluble components and the extraction efficiency.
  • the slurry from which the soluble coal component is eluted in the elution unit 2 is sent to the solid-liquid separation unit 3 through the supply pipe.
  • the solid-liquid separation unit 3 separates the solution obtained by dissolving the coal component obtained in the elution unit 2 in the solvent and the solid concentrate containing the solvent-insoluble component from the slurry.
  • the solvent-insoluble component refers to an extraction residue that is mainly composed of ash and insoluble coal that are insoluble in the extraction solvent, and also includes the extraction solvent.
  • the separation in the solid-liquid separation unit 3 can be performed by, for example, a gravity sedimentation method.
  • the gravity sedimentation method is a separation method in which a solid content is settled by using gravity in a sedimentation tank to perform solid-liquid separation.
  • a solution containing a solvent-soluble component is accumulated at the upper part of the solid-liquid separation unit 3.
  • This solution is filtered using a filter unit as necessary, and then discharged to the first solvent separation unit 4.
  • the solid concentrate containing the solvent-insoluble component is collected at the lower part of the solid-liquid separation unit 3 and discharged to the second solvent separation unit 5.
  • the liquid containing the solvent-soluble component and the solid content containing the solvent-insoluble component are discharged from the settling tank while continuously supplying the slurry into the solid-liquid separation unit 3. be able to. Thereby, continuous solid-liquid separation processing becomes possible.
  • the time for maintaining the slurry in the solid-liquid separation unit 3 is not particularly limited, but can be, for example, 30 minutes or more and 120 minutes or less, and sedimentation separation in the solid-liquid separation unit 3 is performed within this time.
  • the time which maintains a slurry in the solid-liquid separation part 3 can be shortened.
  • the solid-liquid separation unit 3 It is preferable to heat and pressurize the solid-liquid separation unit 3. As a minimum of heating temperature in solid-liquid separation part 3, 300 ° C is preferred and 350 ° C is more preferred. On the other hand, as an upper limit of the heating temperature in the solid-liquid separation part 3, 420 degreeC is preferable and 400 degreeC is more preferable. If the heating temperature is less than the lower limit, the solvent-soluble component may reprecipitate and the separation efficiency may be reduced. Conversely, if the heating temperature exceeds the upper limit, the operating cost for heating may increase.
  • the pressure in the solid-liquid separation part 3 1 MPa is preferable and 1.4 MPa is more preferable.
  • the upper limit of the pressure is preferably 3 MPa, more preferably 2 MPa. If the pressure is less than the lower limit, the solvent-soluble component may reprecipitate and the separation efficiency may be reduced. Conversely, when the pressure exceeds the upper limit, the operating cost for pressurization may increase.
  • a method of isolate separating the said solution and solid content concentrate
  • it is not restricted to a gravity sedimentation method
  • a filtration method or a centrifugation method is used as the solid-liquid separation method
  • a filter, a centrifuge, or the like is used as the solid-liquid separation unit 3.
  • the first solvent separation unit 4 evaporates the solvent from the solution separated by the solid-liquid separation unit 3. Ashless coal HPC is obtained by evaporating and separating the solvent.
  • the first solvent separation unit 4 can be called an evaporation separation unit.
  • the ashless coal HPC obtained in this way exhibits a higher calorific value than, for example, coke raw material coal. Furthermore, ashless coal has a significantly improved softening and melting property, which is a particularly important quality as a raw material for iron-making coke, and exhibits fluidity far superior to, for example, raw material coal. Therefore, ashless coal can also be used as coal blended with coke raw materials.
  • a separation method including a general distillation method using an evaporative separator or an evaporation method (spray drying method or the like) can be used.
  • the solvent evaporated in the first solvent separation unit 4 may be liquefied by, for example, a heat exchanger, supplied to the heating unit 1, and used as a solvent to be mixed with coal and a radical stabilizer.
  • a heat exchanger supplied to the heating unit 1
  • the recycling cost of a solvent can reduce the manufacturing cost of ashless coal.
  • the second solvent separation unit 5 evaporates and separates the solvent from the solid concentrate separated by the solid-liquid separation unit 3 to obtain by-product coal RC.
  • By-product charcoal RC does not show softening and melting properties, but the oxygen-containing functional groups are eliminated. Therefore, by-product coal RC does not inhibit the softening and melting properties of other coals included in this blended coal when used as a blended coal. Therefore, this byproduct charcoal RC can be used, for example, as a part of the blended coal of the coke raw material. Moreover, you may utilize byproduct coal RC as a fuel similarly to general coal.
  • a general distillation method or evaporation method e.g., spray drying method
  • an evaporation separator is used, as in the separation method of the first solvent separation unit 4. it can.
  • the solvent evaporated in the second solvent separation unit 5 may be liquefied by, for example, a heat exchanger, supplied to the heating unit 1, and used as a solvent to be mixed with coal and a radical stabilizer.
  • a heat exchanger supplied to the heating unit 1
  • the recycling cost of a solvent can reduce the manufacturing cost of ashless coal.
  • the method for producing ashless coal includes a heating step, an elution step, a separation step, a first evaporation step, and a second evaporation step.
  • the said ashless coal manufacturing method can be performed using the manufacturing apparatus of ashless coal of FIG.
  • the heating process includes a solvent heating process, a solvent transport process, and a supply process for supplying coal and a radical stabilizer.
  • the solvent heating step the solvent is heated. Specifically, the solvent stored in the solvent tank 11 is caused to flow to the transport pipe 15 by the pump 12, and the solvent flowing in the transport pipe 15 is heated while passing through the preheater 13.
  • the solvent heated in the solvent heating step is transported to the elution step. Specifically, the solvent is supplied to the elution part 2 through the transport pipe 15.
  • coal and a radical stabilizer are supplied to the solvent in the solvent transport step.
  • coal and a radical stabilizer are supplied from the feeder 14 to the conveying pipe 15 through which the heated solvent flows, and the coal, the radical stabilizer and the solvent are mixed to form a slurry.
  • the coal and radical stabilizer supplied to the transport pipe 15 are rapidly heated by the solvent, and the solvent flowing through the transport pipe 15 stirs the coal, so that the coal is easily dissolved and the solvent and the coal are well mixed. A slurry is obtained.
  • the lower limit of the coal heating rate in the supplying step is preferably 600 ° C./min, and more preferably 700 ° C./min.
  • the upper limit of the heating rate is not particularly limited, but can be 30000 ° C./min.
  • the temperature increase rate exceeds the upper limit, the cost for temperature increase may increase unnecessarily.
  • the said temperature increase rate can be adjusted with the heating temperature of the solvent in the said solvent heating process.
  • a coal component soluble in a solvent is eluted from the coal in the slurry obtained in the heating step.
  • the slurry prepared in the heating step is supplied to the extraction tank 21, and the solvent-soluble component is extracted while being held at a predetermined temperature while being stirred by the stirrer 21a.
  • the separation step the slurry eluted in the elution step is separated into a liquid component containing a solvent-soluble component and a solid content concentrate containing a solvent-insoluble component.
  • the slurry discharged from the extraction tank 21 is supplied to the solid-liquid separation unit 3, and the slurry supplied into the solid-liquid separation unit 3 is separated into the liquid component and the solid content concentrate by, for example, gravity sedimentation. To do.
  • First evaporation step the solvent is evaporated from the solution separated in the separation step. Specifically, the solution separated by the solid-liquid separation unit 3 is supplied to the first solvent separation unit 4, and the solvent is evaporated by the first solvent separation unit 4. This separates the solution into solvent and ashless coal.
  • ⁇ Second evaporation step> the solvent is evaporated from the solid content concentrate separated in the separation step. Specifically, the solid concentrate separated by the solid-liquid separation unit 3 is supplied to the second solvent separation unit 5, and the solvent is evaporated by the second solvent separation unit 5 to separate the solvent and by-product coal. .
  • a radical stabilizer is added to the slurry before heating and extracting a solvent soluble component. Since this radical stabilizer can suppress polymerization due to polycondensation of coal radicals caused by heating the slurry, it is possible to increase the soluble components of coal to be eluted. Therefore, the extraction rate of ashless coal can be increased by using the ashless coal production apparatus and the ashless coal production method.
  • coal in the said ashless coal manufacturing apparatus and the said ashless coal manufacturing method, while supplying coal to the heated solvent in conveyance, coal can be heated up rapidly and coal and a solvent by the flow of a solvent. And can be stirred. Thereby, coal can be melt
  • the heating unit 10 in FIG. 2 is used in place of the heating unit 1 of the ashless coal manufacturing apparatus in FIG. 1.
  • the heating unit 10 in FIG. 2 includes a solvent tank 11, a feeder 14, a mixing unit 16, a pump 17, and a temperature raising unit 18.
  • the solvent tank 11 and the supply device 14 are the same as those in the ashless coal production apparatus of FIG.
  • the mixing unit 16 mixes the solvent supplied from the solvent tank 11 with the coal and radical stabilizer supplied from the supplier 14.
  • a preparation tank 19 can be used as the mixing unit 16.
  • the preparation tank 19 is supplied with the coal, radical stabilizer and solvent through a supply pipe.
  • the supplied coal, radical stabilizer and solvent are mixed to prepare a slurry.
  • the said preparation tank 19 has the stirrer 19a, and maintains the mixing state of a slurry by hold
  • the slurry prepared in the preparation tank 19 of the mixing unit 16 is sent to the temperature raising unit 18 through the supply pipe.
  • the pump 17 is disposed in a supply pipe that supplies the slurry from the mixing unit 16 to the temperature raising unit 18, and pumps the slurry stored in the preparation tank 19 to the temperature raising unit 18.
  • the type of the pump 17 is not particularly limited as long as it can pump the slurry to the temperature raising unit 18 through the supply pipe, and for example, a positive displacement pump or a non-positive displacement pump can be used.
  • a positive displacement pump or a non-positive displacement pump can be used.
  • the positive displacement pump include a diaphragm pump and a tube diaphragm pump
  • examples of the non-positive displacement pump include a spiral pump.
  • the temperature raising unit 18 raises the temperature of the slurry obtained in the mixing unit 16.
  • the temperature raising unit 18 is not particularly limited as long as it can raise the temperature of the slurry passing through the inside, and examples thereof include a resistance heating heater and an induction heating coil. Further, the temperature raising unit 18 may be configured to raise the temperature using a heat medium.
  • the temperature raising unit 18 includes a heating pipe disposed around the flow path of the slurry passing through the inside, and the heating pipe The slurry may be configured to be heated by supplying a heating medium such as steam or oil.
  • the upper limit of the temperature of the slurry is preferably 420 ° C., more preferably 400 ° C. If the temperature of the slurry is less than the lower limit, the bonds between the molecules constituting the coal cannot be sufficiently weakened, and the elution rate may decrease. On the contrary, when the temperature of the slurry exceeds the upper limit, the amount of heat for maintaining the temperature of the slurry becomes unnecessarily large, which may increase the production cost of the porous carbon particles.
  • the method for producing ashless coal includes a heating step, an elution step, a separation step, a first evaporation step, and a second evaporation step.
  • the ashless coal production method can be performed using an ashless coal production apparatus having the heating unit 10 of FIG.
  • an elution process, a separation process, a 1st evaporation process, and a 2nd evaporation process can be performed similarly to the manufacturing method of ashless coal of 1st Embodiment, only a heating process is demonstrated here.
  • the heating step the mixture of coal, radical stabilizer and solvent is heated.
  • the heating step includes a mixing step and a temperature raising step.
  • coal, radical stabilizer and solvent are mixed. Specifically, coal and radical stabilizer supplied from the supply device 14 and the solvent supplied from the solvent tank 11 are mixed in the preparation tank 19 of the mixing unit 16 to form a slurry.
  • the temperature raising step the temperature of the slurry obtained in the mixing step is raised. Specifically, the slurry is supplied to the temperature raising unit 18 by the pump 17 to raise the temperature of the slurry.
  • the manufacturing apparatus of ashless coal and the manufacturing method of ashless coal of this invention are not limited to the said embodiment.
  • the configuration in which a mixture in which coal and a radical stabilizer are mixed in advance is supplied from a feeder, but the coal and the radical stabilizer may be supplied separately.
  • the preheater is disposed on the downstream side of the pump as the heating unit, but the arrangement order of the pump and the preheater may be reversed.
  • the mixing part of the manufacturing apparatus of ashless coal demonstrated the structure which has a preparation tank, if not only this structure but mixing of a solvent, coal, and a radical stabilizer can be performed, a preparation tank will be abbreviate
  • the preparation tank may be omitted and a line mixer may be provided between the supply pipe and the temperature raising unit.
  • bituminous coal 40g was prepared as coal.
  • the said coal was grind
  • 240 g of 1-methylnaphthalene was prepared as an ashless coal extraction solvent. This coal and solvent were mixed to prepare a slurry.
  • octadecylamine which is a monoamine
  • the slurry was put into an autoclave having a capacity of 500 cc having a stainless steel filter, and the temperature was raised to 380 ° C. under a pressure condition of 2 MPa. And it stirred for 40 minutes, keeping temperature at 380 degreeC, and the coal component soluble in a solvent was eluted from coal.
  • the filtration was carried out with the above extraction temperature, the mass of the filter residue (solvent insoluble component) was measured, and the proportion of coal component soluble in the solvent, that is, the extraction rate was calculated.
  • the addition amount of monoamine being 0 g, 0.5 g, 1 g, and 4 g. Note that “the amount of monoamine added is 0 g” means that no monoamine is added.
  • the “increase rate” is an amount calculated by (Y ⁇ X) / X ⁇ 100, where X is the extraction rate when the addition amount is 0 g, and Y is the extraction rate under the condition for calculating the increase rate. It is.
  • the horizontal axis is converted to the amount of the radical stabilizer added to coal (mmol / g) based on anhydrous carbon.
  • the types of radical stabilizers are primary monoamine octadecylamine (amine A), secondary monoamine dioctadecylamine (amine B), and quaternary ammonium.
  • the same treatment was carried out as the salt dialkyldimethylammonium chloride (amine C), primary diamine N-alkyl-1,3-diaminopropane (amine D), and primary triamine tallow dipropylene triamine (amine E).
  • the extraction rate increase rate (mass%) was calculated.
  • FIG. FIG. 5 is a graph showing the above results based on the amount (mol amount) of the radical stabilizer added to the coal based on anhydrous carbon.
  • the extraction rate of ashless coal can be increased by using the method and apparatus for producing ashless coal of the present invention.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

Le procédé de production de charbon sans cendres selon un mode de réalisation de la présente invention comprend : une étape de chauffage d'un mélange de charbon, d'un stabilisant radicalaire et d'un solvant ; une étape d'élution des composants solubles dans le solvant à partir du charbon dans la suspension obtenue dans l'étape de chauffage ; une étape de séparation de la suspension après élution dans l'étape d'élution pour obtenir un liquide contenant les composants solubles dans le solvant et des composants insolubles dans le solvant ; et une étape d'évaporation du solvant à partir du liquide séparé dans l'étape de séparation. Le dispositif de production de charbon sans cendres selon un mode de réalisation de la présente invention comprend : une unité de chauffage qui chauffe un mélange de charbon, d'un stabilisant radicalaire et d'un solvant ; une unité d'élution qui élue des composants solubles dans le solvant à partir du charbon dans la suspension obtenue par l'unité de chauffage ; une unité de séparation solide-liquide qui sépare la suspension après élution par l'unité d'élution pour obtenir un liquide contenant les composants solubles dans le solvant et des composants insolubles dans le solvant ; et une unité de séparation-évaporation qui évapore le solvant du liquide séparé par l'unité de séparation solide-liquide.
PCT/JP2018/014885 2017-05-24 2018-04-09 Procédé de production de charbon sans cendres et dispositif de production de charbon sans cendres WO2018216373A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
KR1020197036297A KR102291836B1 (ko) 2017-05-24 2018-04-09 무회탄의 제조 방법 및 무회탄의 제조 장치
CN201880033426.3A CN110651027B (zh) 2017-05-24 2018-04-09 无灰煤的制造方法和无灰煤的制造装置

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2017-102605 2017-05-24
JP2017102605A JP6827884B2 (ja) 2017-05-24 2017-05-24 無灰炭の製造方法及び無灰炭の製造装置

Publications (1)

Publication Number Publication Date
WO2018216373A1 true WO2018216373A1 (fr) 2018-11-29

Family

ID=64396576

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2018/014885 WO2018216373A1 (fr) 2017-05-24 2018-04-09 Procédé de production de charbon sans cendres et dispositif de production de charbon sans cendres

Country Status (4)

Country Link
JP (1) JP6827884B2 (fr)
KR (1) KR102291836B1 (fr)
CN (1) CN110651027B (fr)
WO (1) WO2018216373A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114621799A (zh) * 2020-12-10 2022-06-14 株式会社神户制钢所 无灰煤的制造方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5815590A (ja) * 1981-07-22 1983-01-28 Neos Co Ltd 石炭−水スラリ−用脱水剤
JPS61285286A (ja) * 1985-06-12 1986-12-16 Nippon Steel Chem Co Ltd 石炭の乾留方法
JP2009227729A (ja) * 2008-03-19 2009-10-08 Kobe Steel Ltd 無灰炭の製造方法
JP2010083907A (ja) * 2008-09-29 2010-04-15 Kobe Steel Ltd 無灰炭の製造方法
JP2012502158A (ja) * 2008-09-12 2012-01-26 タータ スチール リミテッド 石炭のテクノ−エコノミック有機精製法の開発
JP2016056282A (ja) * 2014-09-09 2016-04-21 株式会社神戸製鋼所 無灰炭の製造方法及び無灰炭の製造装置
JP2016069570A (ja) * 2014-09-30 2016-05-09 株式会社神戸製鋼所 無灰炭の製造方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5912991A (ja) * 1982-07-13 1984-01-23 Mitsui Eng & Shipbuild Co Ltd 石炭液化油の貯蔵方法
JP4045229B2 (ja) 2003-10-15 2008-02-13 株式会社神戸製鋼所 無灰炭の製造方法
CN101177640B (zh) * 2007-11-30 2010-05-19 华南理工大学 一种稳定无灰纳米煤浆的制备方法
JP5982666B2 (ja) * 2013-12-25 2016-08-31 株式会社神戸製鋼所 無灰炭の製造方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5815590A (ja) * 1981-07-22 1983-01-28 Neos Co Ltd 石炭−水スラリ−用脱水剤
JPS61285286A (ja) * 1985-06-12 1986-12-16 Nippon Steel Chem Co Ltd 石炭の乾留方法
JP2009227729A (ja) * 2008-03-19 2009-10-08 Kobe Steel Ltd 無灰炭の製造方法
JP2012502158A (ja) * 2008-09-12 2012-01-26 タータ スチール リミテッド 石炭のテクノ−エコノミック有機精製法の開発
JP2010083907A (ja) * 2008-09-29 2010-04-15 Kobe Steel Ltd 無灰炭の製造方法
JP2016056282A (ja) * 2014-09-09 2016-04-21 株式会社神戸製鋼所 無灰炭の製造方法及び無灰炭の製造装置
JP2016069570A (ja) * 2014-09-30 2016-05-09 株式会社神戸製鋼所 無灰炭の製造方法

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114621799A (zh) * 2020-12-10 2022-06-14 株式会社神户制钢所 无灰煤的制造方法
CN114621799B (zh) * 2020-12-10 2024-02-09 株式会社神户制钢所 无灰煤的制造方法

Also Published As

Publication number Publication date
JP2018197306A (ja) 2018-12-13
CN110651027A (zh) 2020-01-03
JP6827884B2 (ja) 2021-02-10
KR20200004872A (ko) 2020-01-14
KR102291836B1 (ko) 2021-08-23
CN110651027B (zh) 2021-11-05

Similar Documents

Publication Publication Date Title
JP6035559B2 (ja) 無灰炭の製造装置および無灰炭の製造方法
JP5259216B2 (ja) 無灰炭の製造方法
WO2018216373A1 (fr) Procédé de production de charbon sans cendres et dispositif de production de charbon sans cendres
WO2018030161A1 (fr) Procédé et appareil de production de charbon sans cendres
JP6003001B2 (ja) 無灰炭の製造装置および無灰炭の製造方法
JP2020007466A (ja) 無灰炭の製造方法
JP2019077816A (ja) 無灰炭の製造方法
JP6297412B2 (ja) 無灰炭の製造装置及び無灰炭の製造方法
JP6815968B2 (ja) 無灰炭の製造方法及び無灰炭の製造装置
JP6203698B2 (ja) 無灰炭の製造方法
KR102646022B1 (ko) 무회탄의 제조 방법
JP6203692B2 (ja) 無灰炭の製造方法及び無灰炭の製造装置
JP6632486B2 (ja) 無灰炭の製造方法及び無灰炭の製造装置
JP6618866B2 (ja) コークス製造用原料炭の製造方法、コークス製造用原料炭の製造装置、及び高炉用コークスの製造方法
JP2023174409A (ja) 無灰炭の製造方法及び無灰炭の製造装置
JP2023174408A (ja) 無灰炭の製造方法及び無灰炭の製造装置
CN107406781B (zh) 无灰煤的制造方法
JP6203690B2 (ja) 無灰炭の製造装置および無灰炭の製造方法
JP2020002273A (ja) コークスの製造方法
JP2020066722A (ja) コークスの製造方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 18805792

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 20197036297

Country of ref document: KR

Kind code of ref document: A

122 Ep: pct application non-entry in european phase

Ref document number: 18805792

Country of ref document: EP

Kind code of ref document: A1