US20160160141A1 - Production method of reformed coal - Google Patents
Production method of reformed coal Download PDFInfo
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- US20160160141A1 US20160160141A1 US14/908,296 US201414908296A US2016160141A1 US 20160160141 A1 US20160160141 A1 US 20160160141A1 US 201414908296 A US201414908296 A US 201414908296A US 2016160141 A1 US2016160141 A1 US 2016160141A1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
- C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L5/00—Solid fuels
- C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
- C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2250/00—Structural features of fuel components or fuel compositions, either in solid, liquid or gaseous state
- C10L2250/06—Particle, bubble or droplet size
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/02—Combustion or pyrolysis
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/08—Drying or removing water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/24—Mixing, stirring of fuel components
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/28—Cutting, disintegrating, shredding or grinding
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/40—Applying a magnetic field or inclusion of magnets in the apparatus
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
Definitions
- the present invention relates to a production method of reformed coal.
- Low-grade coal with high moisture content, such as lignite and sub-bituminous coal
- has a low calorific value per unit of weight thus, such coal is heated so as to be dried and pyrolyzed and is also modified in a low-oxygen atmosphere so as to reduce surface activity.
- the coal is converted to reformed coal having a high calorific value per unit of weight while preventing spontaneous combustion (see, for example, Patent Document 1).
- Patent Document 1 Japanese Unexamined Patent Application Publication No. 2011-37937A
- Patent Document 2 U.S. Pat. No. 5,403,365B
- Patent Document 3 U.S. Pat. No. 8,394,240B
- Patent Document 4 U.S. Pat. No. 7,540,384B
- the present invention has been conceived in order to solve the problem described above, and an object of the present invention is to provide a production method of reformed coal in which coal having a higher calorific value and lower mercury content can be obtained.
- a production method of reformed coal according to a first invention for solving the problem described above includes: a drying step of drying coal to obtain dried coal; a dry deashing step of removing ash from the dried coal obtained in the drying step to obtain deashed dried coal: and a pyrolyzing step of pyrolyzing the deashed dried coal obtained in the dry deashing step to obtain deashed pyrolyzed coal.
- a production method of reformed coal according to a second invention for solving the problem described above is based on the production method of reformed coal according to the first invention of the present invention and further includes: a dividing step of dividing out a portion of the deashed dried coal obtained in the dry deashing step; and a mixing step of mixing the deashed dried coal divided out in the dividing step with the deashed pyrolyzed coal obtained in the pyrolyzing step to obtain mixed coal.
- a production method of reformed coal according to a third invention for solving the problem described above is based on the production method of reformed coal according to the first invention or the second invention.
- the dry deashing step is performed using a pulverizer that pulverizes the dried coal and a magnetic separation apparatus that magnetically separates and removes the ash from the dried coal pulverized by the pulverizer.
- a production method of reformed coal according to a fourth invention for solving the problem described above is based on the production method of reformed coal according to the first invention or the second invention.
- the dry deashing step is performed using an air stream separation apparatus that, with an air stream, separates and removes the ash from the dried coal.
- a production method of reformed coal according to a fifth invention for solving the problem described above is based on the production method of reformed coal according to any one of the first to fourth inventions, in which the coal is low-grade coal.
- FIG. 1 is a process flow chart of a first embodiment of a production method of reformed coal according to the present invention.
- FIG. 2 is a process flow chart of a second embodiment of the production method of reformed coal according to the present invention.
- FIG. 1 A first embodiment of the production method of reformed coal according to the present invention will now be described with reference to FIG. 1 .
- the production method of reformed coal includes, as illustrated in FIG. 1 , a drying step S 1 of drying low-grade coal (low-rank coal) 1 to obtain dried coal 2 , a dry deashing step S 2 of dry-deashing the dried coal 2 obtained in the drying step S 1 using a dry deashing apparatus to obtain deashed dried coal 3 , and a pyrolyzing step S 3 of pyrolyzing the deashed dried coal 3 obtained in the dry deashing step S 2 to obtain deashed pyrolyzed coal 4 .
- the low-rank coal 1 is coal having a high (60 to 70%) moisture content, such as lignite or sub-bituminous coal, which, although vast deposits thereof exist, the coal has a low calorific value per unit of weight and is inefficient to transport.
- the drying step S 1 is a step of removing water 5 from the low-rank coal 1 .
- feeding the low-rank coal 1 to a hot-air dryer of belt conveyor type or the like and drying the low-rank coal 1 with hot air (100 to 280° C., preferably 150 to 200° C.) produces dried coal 2 having a moisture content of substantially 0%.
- the dry deashing step S 2 is a step of separating and removing, from the dried coal 2 , ash 6 contained in the dried coal 2 .
- a dry deashing apparatus provided with a pulverizer that pulverizes the dried coal 2 and a magnetic separation apparatus that magnetically separates and removes the ash 6 from the dried coal 2 pulverized by the pulverizer, and pulverizing the dried coal 2 to, for example, a particle diameter of 200 mesh or less and magnetically separating and removing the ash 6 (especially pyrite and the like having a high mercury content) produces deashed dried coal 3 having, for example, an ash content of about 35% or less.
- the dry deashing step S 2 for example, feeding the dried coal 2 to the dry deashing apparatus, such as an air stream separation apparatus, allowing the dried coal 2 to flow on a fluidized bed and supplying air thereto to separate and remove the ash 6 (especially substances including high-mercury-content pyrite, which are heavier than the coal) produces the deashed dried coal 3 having an ash content of, for example, about 35% or less.
- the dry deashing step S 2 produces deashed dried coal 3 obtained by removing, from the dried coal 2 , ash 6 along with the better part of the mercury in the dried coal 2 .
- Non Patent Document 1 can be used as the dry deashing apparatus provided with the pulverizer and the magnetic separation apparatus.
- the apparatus disclosed, for example, in Patent Document 4 or Non Patent Document 2 can be used as the dry deashing apparatus such as the air stream separation apparatus.
- the pyrolyzing step S 3 is a step of removing volatile components 7 such as tar from the deashed dried coal 3 .
- the pyrolyzing step S 3 for example, feeding the deashed dried coal 3 to a continuous pyrolyzer and pyrolyzing the deashed dried coal 3 at an elevated temperature (300 to 500° C., preferably 400 to 450° C.) to separate and collect mercury contained in the deashed dried coal 3 along with the volatile components 7 such as tar produces deashed pyrolyzed coal 4 .
- mercury in the low-rank coal 1 can be removed in both the dry deashing step S 2 and the pyrolyzing step S 3 , with the mercury being physically removed along with the ash 6 in the dry deashing step S 2 before being removed along with the volatile components 7 , thereby allowing the deashed pyrolyzed coal 4 to have a lower mercury content than that of pyrolyzed coal obtained by drying and pyrolyzing the low-rank coal 1 .
- deashed pyrolyzed coal 4 having a higher calorific value and a lower mercury content can be obtained.
- the present embodiment is constituted by the steps of the production method of reformed coal illustrated in FIG. 1 to which a dividing step and a mixing step are added.
- the rest of the steps is substantially identical to that illustrated in FIG. 1 as described above, so the identical steps and substances will be given the same reference numerals and duplicated description thereof will be omitted as appropriate.
- the production method of reformed coal includes, as illustrated in FIG. 2 , a drying step S 1 of drying low-grade coal (low-rank coal) 1 to obtain dried coal 2 , a dry deashing step S 2 of dry deashing the dried coal 2 obtained in the drying step S 1 using a dry deashing apparatus to obtain deashed dried coal 3 , a dividing step S 11 of dividing out a portion of the deashed dried coal 3 obtained in the dry deashing step S 2 , a pyrolyzing step S 12 of pyrolyzing deashed dried coal 3 a that has not been divided out in the dividing step S 11 to obtain deashed pyrolyzed coal 11 , and a mixing step S 13 of mixing the deashed pyrolyzed coal 11 obtained in the pyrolyzing step S 12 with deashed dried coal 3 b that has been divided out in the dividing step S 11 to obtain mixed coal 12 .
- the dividing step S 11 is a step of dividing out a portion of the deashed dried coal 3 .
- feeding the deashed dried coal 3 to a dividing apparatus such as a conveyer belt or a screw feeder divides the deashed dried coal 3 into the deashed dried coal 3 a to be sent to the pyrolyzing step S 12 and the deashed dried coal 3 b to be sent to the mixing step S 13 .
- the proportion of how the deashed dried coal 3 is divided can be adjusted according to the target oxygen content or mercury content of the mixed coal 12 . This is because the oxygen content or mercury content of the deashed dried coal 3 and the deashed pyrolyzed coal 11 can be adjusted in accordance with respective processing conditions, and can also be determined through analysis.
- the pyrolyzing step S 12 is a step, identical to the pyrolyzing step S 3 described above, of removing volatile components 13 such as tar from the deashed dried coal 3 a.
- the pyrolyzing step S 12 for example, feeding the deashed dry coal 3 a to a continuous pyrolyzer, pyrolyzing the deashed dry coal 3 a at an elevated temperature (300 to 500° C. preferably 400 to 450° C.), and separating and collecting mercury contained in the deashed dried coal 3 a along with the volatile components 13 such as tar, produces deashed pyrolyzed coal 11 .
- the mixing step S 13 is a step of mixing the deashed pyrolyzed coal 11 obtained in the pyrolyzing step S 12 with the deashed dried coal 3 b divided out in the dividing step S 11 .
- feeding the deashed dried coal 3 b divided out in the dividing step S 11 into a mixer along with the deashed pyrolyzed coal 11 and stirring until the two are uniformly mixed produces mixed coal 12 .
- the mixing ratio of the deashed pyrolyzed coal 11 to the deashed dried coal 3 b in the mixture are adjusted, as appropriate, according to the respective oxygen content of the deashed pyrolyzed coal 11 and the deashed dried coal 3 b, the respective mercury contents of the deashed pyrolyzed coal 11 and the deashed dried coal 3 b, and the like. This is because the oxygen content and mercury content of the deashed dried coal 3 can be obtained through the processing condition of the dry deashing step S 2 or analysis, and the oxygen content and mercury content of the deashed pyrolyzed coal 11 can be obtained through the processing condition of the pyrolyzing step S 12 or analysis.
- the mixed coal 12 is a mixture of the deashed pyrolyzed coal 11 obtained by removing mercury from the low-rank coal 1 through dry deashing and pyrolysis and the deashed dried coal 3 b obtained by removing mercury from the low-grade coal 1 through dry deashing, with the dry deashing physically removing mercury and the pyrolysis uniformly chemically removing mercury from the entirety of the coal, the mercury content of the deashed pyrolyzed coal 11 can be reduced to less than that of pyrolyzed coal obtained by drying and pyrolyzing the low-rank coal 1 . As a result, the deashed pyrolyzed coal 11 having a higher calorific value and a lower mercury content can be obtained.
- the volume of the deashed dried coal 3 b to be mixed can be increased according to the respective oxygen content and mercury content of the deashed pyrolyzed coal 11 and the deashed dry coal 3 b and the target oxygen content and mercury content of the mixed coal 12 , the yield can be increased over the production method of reformed coal according to the first embodiment, which does not include the dividing step S 11 and the mixing step S 13 , resulting in higher productivity of the mixed coal 12 .
- low-rank coal having a mercury content of 69 ppm is used.
- the low-rank coal is dried with hot air at a temperature of, for example, 100 to 280° C. in the drying step to remove water from the low-rank coal and obtain dried coal.
- the mercury content of the dried coal is 69 ppm, which is the same as the low-rank coal.
- the dried coal is pulverized to 200 mesh or less and the ash is magnetically removed therefrom, for example, by a dry deashing apparatus provided with a pulverizer and a magnetic separation apparatus, and deashed dried coal is obtained.
- the ash is a substance such as pyrite having magnetic properties, which contains more mercury than the other substances in the coal.
- the mercury content of the deashed dried coal 3 is 24.2 ppm.
- the size of the finely powdered ash-containing dried coal was set so as to allow 98% of the calorific value of the coal to be retained while reducing mercury content by 65%. In other words, the dry deashing step physically removes the mercury contained in the dried coal.
- the dividing step a portion of the deashed dried coal is divided out.
- the remainder of the deashed dried coal is pyrolyzed in the pyrolyzing step at an elevated temperature (300 to 500° C., preferably 400 to 450° C.) to obtain deashed pyrolyzed coal.
- an elevated temperature 300 to 500° C., preferably 400 to 450° C.
- the mercury contained in the deashed dried coal is volatilized along with the volatile components, and removed by 80%.
- the mercury content of the deashed pyrolyzed coal is 4.83 ppm.
- the pyrolyzing step chemically removes the mercury contained in the deashed dried coal.
- the deashed dried coal divided out in the dividing step and the deashed pyrolyzed coal obtained in the pyrolyzing step are mixed to obtain mixed coal.
- the divided out deashed dried coal and the deashed pyrolyzed coal obtained in the pyrolyzing step are mixed at the ratio of, for example, 54% by weight to 46% by weight to obtain the mixed coal.
- the mercury content of the obtained mixed coal is 13.8 ppm.
- oxygen content and mercury content can he adjusted by adjusting the particle size of the dried coal and the amount of ash to be removed in the dry deashing step and the mixing ratio of deashed pyrolyzed coal and deashed dried coal in the mixing step, thereby obtaining mixed coal having a higher calorific value and a lower mercury content.
- the production method of reformed coal in which the low-rank coal 1 is dried, dry deashed, and pyrolyzed to obtain the deashed pyrolyzed coal 4 has been described, but a production method of reformed coal in which coal is obtained from the deashed pyrolyzed coal 4 having its surface deactivated through a deactivating process in which the deashed pyrolyzed coal 4 is brought into contact with a specific treatment gas (oxygen-containing gas) is also possible.
- a specific treatment gas oxygen-containing gas
- a production method of reformed coal is also possible in which, after the coal obtained by the deashed pyrolyzed coal 4 having its surface deactivated through the deactivation process in which the deashed pyrolyzed coal 4 is brought into contact with a specific treatment gas (oxygen-containing gas), the coal is mixed with a binder such as corn starch or asphalt and compressed (at a pressure of 1,200 kg/cm 2 and a temperature of 300 to 450° C., preferably 350 to 450° C.) into a solid briquette such as a cylinder or a charcoal briquette to produce formed coal.
- a binder such as corn starch or asphalt
- compressed at a pressure of 1,200 kg/cm 2 and a temperature of 300 to 450° C., preferably 350 to 450° C.
- the production method of reformed coal has been described in which the deashed dried coal 3 a obtained by drying and dry deashing the low-rank coal 1 is pyrolyzed to obtain the deashed pyrolyzed coal 11 , a portion of the deashed dried coal 3 is divided out and the deashed pyrolyzed coal 11 and the divided out deashed dried coal 3 b are mixed to obtain the mixed coal 12 , but a production method of reformed coal in which coal is obtained by the mixed coal 12 having its surface deactivated through a deactivation process in which the mixed coal 12 is brought into contact with a specific treatment gas (oxygen-containing gas) is also possible.
- a specific treatment gas oxygen-containing gas
- a production method of reformed coal is also possible in which, after the coal is obtained by the mixed coal 12 having its surface deactivated through the deactivation process in which the mixed coal 12 is brought into contact with a specific treatment gas (oxygen-containing gas), the coal is mixed with a binder such as corn starch or asphalt and compressed (at a pressure of 1,200 kg/cm 2 and a temperature of 300 to 450° C., preferably 350 to 450° C.) into a solid briquette such as a cylinder or a charcoal briquette to produce formed coal.
- a binder such as corn starch or asphalt
- compressed at a pressure of 1,200 kg/cm 2 and a temperature of 300 to 450° C., preferably 350 to 450° C.
- the production method of reformed coal according to the present invention can obtain coal having a high calorific value and a lower mercury content, and thus can be used to great advantage in industrial applications.
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Abstract
The purpose of the present invention is to increase the calorific value, and to obtain coal having further reduced mercury content. A drying step (S1) of drying low-rank coal (1) constituting coal to obtain dried coal (2), a dry deashing step of removing ash (6) from the dried coal (2) obtained in the drying step (S1) by a dry deashing apparatus, and a pyrolyzing step (S3) of pyrolyzing the deashed dried coal (3) obtained in the dry deashing step (S2) to obtain deashed pyrolyzed coal (4) are performed.
Description
- The present invention relates to a production method of reformed coal.
- Low-grade coal (low-rank coal) with high moisture content, such as lignite and sub-bituminous coal, has a low calorific value per unit of weight; thus, such coal is heated so as to be dried and pyrolyzed and is also modified in a low-oxygen atmosphere so as to reduce surface activity. As a result, the coal is converted to reformed coal having a high calorific value per unit of weight while preventing spontaneous combustion (see, for example, Patent Document 1).
- It is also known that mercury can be removed in coal reformation processes involving such pyrolysis described above through heating operation during pyrolysis (see, for example, Patent Document 2).
- Patent Document 1: Japanese Unexamined Patent Application Publication No. 2011-37937A
- Patent Document 2: U.S. Pat. No. 5,403,365B
- Patent Document 3: U.S. Pat. No. 8,394,240B
- Patent Document 4: U.S. Pat. No. 7,540,384B
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- Non Patent Document 1: R. Weinstein and R. Snoby, “Advances in dry jigging improves coal quality”, p. 29 to p. 34, Mining Engineering, January 2007
- Non Patent Document 2: William H. Pollock et al., “Lowering Costs with Dry Coal Cleaning Technology to Meet New Environmental Requirements”, p. 1 to p. 13, presented at the 10th Anniversary CoalGen Conference, Pittsburgh, Pa., Aug. 10, 2010
- However, although the coal reformation process described above is capable of obtaining reformed coal by removing mercury from the raw coal through pyrolysis, there is a demand for coal having a lower mercury content.
- The present invention has been conceived in order to solve the problem described above, and an object of the present invention is to provide a production method of reformed coal in which coal having a higher calorific value and lower mercury content can be obtained.
- A production method of reformed coal according to a first invention for solving the problem described above includes: a drying step of drying coal to obtain dried coal; a dry deashing step of removing ash from the dried coal obtained in the drying step to obtain deashed dried coal: and a pyrolyzing step of pyrolyzing the deashed dried coal obtained in the dry deashing step to obtain deashed pyrolyzed coal.
- A production method of reformed coal according to a second invention for solving the problem described above is based on the production method of reformed coal according to the first invention of the present invention and further includes: a dividing step of dividing out a portion of the deashed dried coal obtained in the dry deashing step; and a mixing step of mixing the deashed dried coal divided out in the dividing step with the deashed pyrolyzed coal obtained in the pyrolyzing step to obtain mixed coal.
- A production method of reformed coal according to a third invention for solving the problem described above is based on the production method of reformed coal according to the first invention or the second invention. In such a production method of reformed coal, the dry deashing step is performed using a pulverizer that pulverizes the dried coal and a magnetic separation apparatus that magnetically separates and removes the ash from the dried coal pulverized by the pulverizer.
- A production method of reformed coal according to a fourth invention for solving the problem described above is based on the production method of reformed coal according to the first invention or the second invention. In such a production method of reformed coal, the dry deashing step is performed using an air stream separation apparatus that, with an air stream, separates and removes the ash from the dried coal.
- A production method of reformed coal according to a fifth invention for solving the problem described above is based on the production method of reformed coal according to any one of the first to fourth inventions, in which the coal is low-grade coal.
- In accordance with the production method of reformed coal according to the present invention, it is possible to increase a calorific value of coal by drying and dry deashing the coal, before pyrolyzing the coal. In addition, removing ash from the dried coal through dry deashing before pyrolyzing the dried coal allows for the removal of both the ash and mercury contained within the dried coal, resulting in deashed pyrolyzed coal having a mercury content lower than that of pyrolyzed coal obtained by pyrolyzing dried coal. As a. result, coal having a higher calorific value and a lower mercury content can be obtained.
-
FIG. 1 is a process flow chart of a first embodiment of a production method of reformed coal according to the present invention. -
FIG. 2 is a process flow chart of a second embodiment of the production method of reformed coal according to the present invention. - Embodiments of a production method of reformed coal according to the present invention will now be described with reference to the drawings. However, the present invention is not limited to the embodiments described hereafter with reference to the drawings.
- A first embodiment of the production method of reformed coal according to the present invention will now be described with reference to
FIG. 1 . - The production method of reformed coal according to the present embodiment includes, as illustrated in
FIG. 1 , a drying step S1 of drying low-grade coal (low-rank coal) 1 to obtain driedcoal 2, a dry deashing step S2 of dry-deashing the driedcoal 2 obtained in the drying step S1 using a dry deashing apparatus to obtain deashed driedcoal 3, and a pyrolyzing step S3 of pyrolyzing the deashed driedcoal 3 obtained in the dry deashing step S2 to obtain deashed pyrolyzedcoal 4. - The low-
rank coal 1 is coal having a high (60 to 70%) moisture content, such as lignite or sub-bituminous coal, which, although vast deposits thereof exist, the coal has a low calorific value per unit of weight and is inefficient to transport. - The drying step S1 is a step of removing
water 5 from the low-rank coal 1. In the drying step S1, for example, feeding the low-rank coal 1 to a hot-air dryer of belt conveyor type or the like and drying the low-rank coal 1 with hot air (100 to 280° C., preferably 150 to 200° C.) produces driedcoal 2 having a moisture content of substantially 0%. - The dry deashing step S2 is a step of separating and removing, from the dried
coal 2,ash 6 contained in the driedcoal 2. In the dry deashing step S2, for example, feeding the driedcoal 2 to a dry deashing apparatus provided with a pulverizer that pulverizes the driedcoal 2 and a magnetic separation apparatus that magnetically separates and removes theash 6 from the driedcoal 2 pulverized by the pulverizer, and pulverizing the driedcoal 2 to, for example, a particle diameter of 200 mesh or less and magnetically separating and removing the ash 6 (especially pyrite and the like having a high mercury content) produces deashed driedcoal 3 having, for example, an ash content of about 35% or less. Alternatively, in the dry deashing step S2, for example, feeding the driedcoal 2 to the dry deashing apparatus, such as an air stream separation apparatus, allowing the driedcoal 2 to flow on a fluidized bed and supplying air thereto to separate and remove the ash 6 (especially substances including high-mercury-content pyrite, which are heavier than the coal) produces the deashed driedcoal 3 having an ash content of, for example, about 35% or less. In other words, the dry deashing step S2 produces deashed driedcoal 3 obtained by removing, from the driedcoal 2,ash 6 along with the better part of the mercury in the driedcoal 2. - The apparatus disclosed, for example, in
Non Patent Document 1 can be used as the dry deashing apparatus provided with the pulverizer and the magnetic separation apparatus. The apparatus disclosed, for example, inPatent Document 4 orNon Patent Document 2 can be used as the dry deashing apparatus such as the air stream separation apparatus. - The pyrolyzing step S3 is a step of removing
volatile components 7 such as tar from the deashed driedcoal 3. In the pyrolyzing step S3, for example, feeding the deashed driedcoal 3 to a continuous pyrolyzer and pyrolyzing the deashed driedcoal 3 at an elevated temperature (300 to 500° C., preferably 400 to 450° C.) to separate and collect mercury contained in the deashed driedcoal 3 along with thevolatile components 7 such as tar produces deashed pyrolyzedcoal 4. - Thus, in accordance with the production method of reformed coal according to the present embodiment, it is possible to dry, dry deash, and pyrolyze the low-
rank coal 1 to obtain deashed pyrolyzedcoal 4, thereby allowing for a higher calorific value than that of the low-rank coal 1. In addition, mercury in the low-rank coal 1 can be removed in both the dry deashing step S2 and the pyrolyzing step S3, with the mercury being physically removed along with theash 6 in the dry deashing step S2 before being removed along with thevolatile components 7, thereby allowing the deashedpyrolyzed coal 4 to have a lower mercury content than that of pyrolyzed coal obtained by drying and pyrolyzing the low-rank coal 1. As a result, deashed pyrolyzedcoal 4 having a higher calorific value and a lower mercury content can be obtained. - A second embodiment of the production method of reformed coal according to the present invention will now be described with reference to
FIG. 2 . - The present embodiment is constituted by the steps of the production method of reformed coal illustrated in
FIG. 1 to which a dividing step and a mixing step are added. The rest of the steps is substantially identical to that illustrated inFIG. 1 as described above, so the identical steps and substances will be given the same reference numerals and duplicated description thereof will be omitted as appropriate. - The production method of reformed coal according to the present embodiment includes, as illustrated in
FIG. 2 , a drying step S1 of drying low-grade coal (low-rank coal) 1 to obtain driedcoal 2, a dry deashing step S2 of dry deashing the driedcoal 2 obtained in the drying step S1 using a dry deashing apparatus to obtain deashed driedcoal 3, a dividing step S11 of dividing out a portion of the deashed driedcoal 3 obtained in the dry deashing step S2, a pyrolyzing step S12 of pyrolyzing deashed driedcoal 3 a that has not been divided out in the dividing step S11 to obtain deashed pyrolyzedcoal 11, and a mixing step S13 of mixing the deashed pyrolyzedcoal 11 obtained in the pyrolyzing step S12 with deashed driedcoal 3 b that has been divided out in the dividing step S11 to obtain mixedcoal 12. - The dividing step S11 is a step of dividing out a portion of the deashed dried
coal 3. In the dividing step S11, for example, feeding the deashed driedcoal 3 to a dividing apparatus such as a conveyer belt or a screw feeder divides the deashed driedcoal 3 into the deashed driedcoal 3 a to be sent to the pyrolyzing step S12 and the deashed driedcoal 3 b to be sent to the mixing step S13. The proportion of how the deashed driedcoal 3 is divided can be adjusted according to the target oxygen content or mercury content of themixed coal 12. This is because the oxygen content or mercury content of the deashed driedcoal 3 and the deashed pyrolyzedcoal 11 can be adjusted in accordance with respective processing conditions, and can also be determined through analysis. - The pyrolyzing step S12 is a step, identical to the pyrolyzing step S3 described above, of removing
volatile components 13 such as tar from the deashed driedcoal 3 a. In the pyrolyzing step S12, for example, feeding the deasheddry coal 3 a to a continuous pyrolyzer, pyrolyzing the deasheddry coal 3 a at an elevated temperature (300 to 500° C. preferably 400 to 450° C.), and separating and collecting mercury contained in the deashed driedcoal 3 a along with thevolatile components 13 such as tar, produces deashed pyrolyzedcoal 11. - The mixing step S13 is a step of mixing the deashed pyrolyzed
coal 11 obtained in the pyrolyzing step S12 with the deashed driedcoal 3 b divided out in the dividing step S11. In the mixing step S13, feeding the deashed driedcoal 3 b divided out in the dividing step S11 into a mixer along with the deashed pyrolyzedcoal 11 and stirring until the two are uniformly mixed producesmixed coal 12. - The mixing ratio of the deashed pyrolyzed
coal 11 to the deashed driedcoal 3 b in the mixture are adjusted, as appropriate, according to the respective oxygen content of the deashed pyrolyzedcoal 11 and the deashed driedcoal 3 b, the respective mercury contents of the deashed pyrolyzedcoal 11 and the deashed driedcoal 3 b, and the like. This is because the oxygen content and mercury content of the deashed driedcoal 3 can be obtained through the processing condition of the dry deashing step S2 or analysis, and the oxygen content and mercury content of the deashed pyrolyzedcoal 11 can be obtained through the processing condition of the pyrolyzing step S12 or analysis. - Thus, in accordance with the production method of reformed coal according to the present embodiment, it is possible to mix the deashed pyrolyzed
coal 11 obtained by drying, dry deashing, and pyrolyzing the low-rank coal 1 with divided out deashed driedcoal 3 b to obtain themixed coal 12, thereby allowing for a higher calorific value than that of the low-rank coal 1. In addition, because themixed coal 12 is a mixture of the deashed pyrolyzedcoal 11 obtained by removing mercury from the low-rank coal 1 through dry deashing and pyrolysis and the deashed driedcoal 3 b obtained by removing mercury from the low-grade coal 1 through dry deashing, with the dry deashing physically removing mercury and the pyrolysis uniformly chemically removing mercury from the entirety of the coal, the mercury content of the deashed pyrolyzedcoal 11 can be reduced to less than that of pyrolyzed coal obtained by drying and pyrolyzing the low-rank coal 1. As a result, the deashed pyrolyzedcoal 11 having a higher calorific value and a lower mercury content can be obtained. In addition, because the volume of the deashed driedcoal 3 b to be mixed can be increased according to the respective oxygen content and mercury content of the deashed pyrolyzedcoal 11 and the deasheddry coal 3 b and the target oxygen content and mercury content of themixed coal 12, the yield can be increased over the production method of reformed coal according to the first embodiment, which does not include the dividing step S11 and the mixing step S13, resulting in higher productivity of themixed coal 12. - Examples performed in order to confirm the effects of the production method of reformed coal according to the present invention will now be described; however, the present invention is not limited to the examples described below with reference to various data.
- In the present embodiment, low-rank coal having a mercury content of 69 ppm is used. The low-rank coal is dried with hot air at a temperature of, for example, 100 to 280° C. in the drying step to remove water from the low-rank coal and obtain dried coal. As only the water has been removed from the low-rank coal, the mercury content of the dried coal is 69 ppm, which is the same as the low-rank coal.
- Next, in the dry deashing step, the dried coal is pulverized to 200 mesh or less and the ash is magnetically removed therefrom, for example, by a dry deashing apparatus provided with a pulverizer and a magnetic separation apparatus, and deashed dried coal is obtained. As a result, the ash constituting a portion of the dried coal is removed. The ash is a substance such as pyrite having magnetic properties, which contains more mercury than the other substances in the coal. The mercury content of the deashed dried
coal 3 is 24.2 ppm. The size of the finely powdered ash-containing dried coal was set so as to allow 98% of the calorific value of the coal to be retained while reducing mercury content by 65%. In other words, the dry deashing step physically removes the mercury contained in the dried coal. - Next, in the dividing step, a portion of the deashed dried coal is divided out. The remainder of the deashed dried coal is pyrolyzed in the pyrolyzing step at an elevated temperature (300 to 500° C., preferably 400 to 450° C.) to obtain deashed pyrolyzed coal. As a result, the mercury contained in the deashed dried coal is volatilized along with the volatile components, and removed by 80%. The mercury content of the deashed pyrolyzed coal is 4.83 ppm. In other words, the pyrolyzing step chemically removes the mercury contained in the deashed dried coal.
- Next, the deashed dried coal divided out in the dividing step and the deashed pyrolyzed coal obtained in the pyrolyzing step are mixed to obtain mixed coal. The divided out deashed dried coal and the deashed pyrolyzed coal obtained in the pyrolyzing step are mixed at the ratio of, for example, 54% by weight to 46% by weight to obtain the mixed coal. The mercury content of the obtained mixed coal is 13.8 ppm.
- Thus, it was apparent that oxygen content and mercury content can he adjusted by adjusting the particle size of the dried coal and the amount of ash to be removed in the dry deashing step and the mixing ratio of deashed pyrolyzed coal and deashed dried coal in the mixing step, thereby obtaining mixed coal having a higher calorific value and a lower mercury content.
- In the first embodiment, the production method of reformed coal in which the low-
rank coal 1 is dried, dry deashed, and pyrolyzed to obtain the deashed pyrolyzedcoal 4 has been described, but a production method of reformed coal in which coal is obtained from the deashed pyrolyzedcoal 4 having its surface deactivated through a deactivating process in which the deashed pyrolyzedcoal 4 is brought into contact with a specific treatment gas (oxygen-containing gas) is also possible. In addition, a production method of reformed coal is also possible in which, after the coal obtained by the deashed pyrolyzedcoal 4 having its surface deactivated through the deactivation process in which the deashed pyrolyzedcoal 4 is brought into contact with a specific treatment gas (oxygen-containing gas), the coal is mixed with a binder such as corn starch or asphalt and compressed (at a pressure of 1,200 kg/cm2 and a temperature of 300 to 450° C., preferably 350 to 450° C.) into a solid briquette such as a cylinder or a charcoal briquette to produce formed coal. - In the second embodiment described above, the production method of reformed coal has been described in which the deashed dried
coal 3 a obtained by drying and dry deashing the low-rank coal 1 is pyrolyzed to obtain the deashed pyrolyzedcoal 11, a portion of the deashed driedcoal 3 is divided out and the deashed pyrolyzedcoal 11 and the divided out deashed driedcoal 3 b are mixed to obtain themixed coal 12, but a production method of reformed coal in which coal is obtained by themixed coal 12 having its surface deactivated through a deactivation process in which themixed coal 12 is brought into contact with a specific treatment gas (oxygen-containing gas) is also possible. In addition, a production method of reformed coal is also possible in which, after the coal is obtained by themixed coal 12 having its surface deactivated through the deactivation process in which themixed coal 12 is brought into contact with a specific treatment gas (oxygen-containing gas), the coal is mixed with a binder such as corn starch or asphalt and compressed (at a pressure of 1,200 kg/cm2 and a temperature of 300 to 450° C., preferably 350 to 450° C.) into a solid briquette such as a cylinder or a charcoal briquette to produce formed coal. - The production method of reformed coal according to the present invention can obtain coal having a high calorific value and a lower mercury content, and thus can be used to great advantage in industrial applications.
-
- 1 Low-grade coal (low-rank coal)
- 2 Dried coal
- 3 Deashed dried coal
- 3 a, 3 b Deashed dried coal
- 4 Deashed pyrolyzed coal
- 5 Water
- 6 Ash
- 7 Volatile component
- 11 Deashed pyrolyzed coal
- 12 Mixed coal
- 13 Volatile component
- S1 Drying step
- S2 Dry deashing step
- S3 Pyrolyzing step
- S1 Dividing step
- S12 Pyrolyzing step
- S13 Mixing step
Claims (13)
1. A production method of reformed coal, the method comprising:
a drying step of drying coal to obtain dried coal;
a dry deashing step of removing ash from the dried coal obtained in the drying step to obtain deashed dried coal; and
a pyrolyzing step of pyrolyzing the deashed dried coal obtained in the dry deashing step to obtain deashed pyrolyzed coal.
2. The production method of reformed coal according to claim 1 , further comprising:
a dividing step of dividing out a portion of the deashed dried coal obtained in the dry deashing step; and
a mixing step of mixing the deashed dried coal divided out in the dividing step with the deashed pyrolyzed coal obtained in the pyrolyzing step to obtain mixed coal.
3. The production method of reformed coal according to claim 1 , wherein
the dry deashing step is performed using a pulverizer that pulverizes the dried coal and a magnetic separation apparatus that magnetically separates and removes the ash from the dried coal pulverized by the pulverizer.
4-5. (canceled)
6. The production method of reformed coal according to claim 2 , wherein
the dry deashing step is performed using a pulverizer that pulverizes the dried coal and a magnetic separation apparatus that magnetically separates and removes the ash from the dried coal pulverized by the pulverizer.
7. The production method of reformed coal according to claim 1 , wherein
the dry deashing step is performed using an air stream separation apparatus that, with an air stream, separates and removes the ash from the dried coal.
8. The production method of reformed coal according to claim 2 , wherein
the dry deashing step is performed using an air stream separation apparatus that, with an air stream, separates and removes the ash from the dried coal.
9. The production method of reformed coal according to claim 1 , wherein
the coal is low-grade coal.
10. The production method of reformed coal according to claim 2 , wherein
the coal is low-grade coal.
11. The production method of reformed coal according to claim 3 , wherein
the coal is low-grade coal.
12. The production method of reformed coal according to claim 6 , wherein
the coal is low-grade coal.
13. The production method of reformed coal according to claim 7 , wherein
the coal is low-grade coal.
14. The production method of reformed coal according to claim 8 , wherein
the coal is low-grade coal.
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JP2013-158714 | 2013-07-31 | ||
JP2013158714A JP2015030737A (en) | 2013-07-31 | 2013-07-31 | Method for manufacturing modified coal |
PCT/JP2014/068852 WO2015016062A1 (en) | 2013-07-31 | 2014-07-16 | Production method for reformed coal |
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US20160160141A1 true US20160160141A1 (en) | 2016-06-09 |
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US14/908,296 Abandoned US20160160141A1 (en) | 2013-07-31 | 2014-07-16 | Production method of reformed coal |
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US (1) | US20160160141A1 (en) |
JP (1) | JP2015030737A (en) |
CN (1) | CN105408459A (en) |
AU (1) | AU2014297503B2 (en) |
DE (1) | DE112014003532T5 (en) |
WO (1) | WO2015016062A1 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2020065341A1 (en) * | 2018-09-27 | 2020-04-02 | Arq Ip Limited | Processes for utilisation of purified coal compositions as a chemical and thermal feedstock and cleaner burning fuel |
US20220000081A1 (en) * | 2018-06-07 | 2022-01-06 | The Tru Shrimp Company | Raceways and systems thereof |
US11254886B2 (en) | 2016-04-04 | 2022-02-22 | Arq Ip Limited | Fuel oil / particulate material slurry compositions and processes |
US11319492B2 (en) | 2016-04-04 | 2022-05-03 | Arq Ip Limited | Solid-liquid crude oil compositions and fractionation processes thereof |
US20220403274A1 (en) * | 2018-09-27 | 2022-12-22 | Arq Ip Limited | Processes for utilisation of purified coal compositions as a chemical and thermal feedstock and cleaner burning fuel |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
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CN110423628A (en) * | 2019-09-09 | 2019-11-08 | 重庆润科新材料技术有限公司 | A kind of low order dry distillation of coal process units and method |
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JPS5896695A (en) * | 1981-12-02 | 1983-06-08 | Mitsubishi Heavy Ind Ltd | Process for dry deashing of coal |
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JPH09151386A (en) * | 1995-11-29 | 1997-06-10 | Mitsubishi Heavy Ind Ltd | Magnetic separation of powdered coal |
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CA2766333C (en) * | 2007-07-19 | 2016-08-23 | Microcoal Inc. | Method and system for separation of contaminants from coal |
CN102492518A (en) * | 2011-11-30 | 2012-06-13 | 中国五环工程有限公司 | Quality-improving process and apparatus for high-ash low rank coal |
-
2013
- 2013-07-31 JP JP2013158714A patent/JP2015030737A/en active Pending
-
2014
- 2014-07-16 WO PCT/JP2014/068852 patent/WO2015016062A1/en active Application Filing
- 2014-07-16 US US14/908,296 patent/US20160160141A1/en not_active Abandoned
- 2014-07-16 AU AU2014297503A patent/AU2014297503B2/en not_active Ceased
- 2014-07-16 CN CN201480042502.9A patent/CN105408459A/en active Pending
- 2014-07-16 DE DE112014003532.7T patent/DE112014003532T5/en not_active Withdrawn
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US4242102A (en) * | 1978-12-15 | 1980-12-30 | The Lummus Company | Production of gasified products from ash containing bitumen produced in coal liquefaction |
WO2011016370A1 (en) * | 2009-08-07 | 2011-02-10 | 三菱重工業株式会社 | Method for producing modified coal |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11254886B2 (en) | 2016-04-04 | 2022-02-22 | Arq Ip Limited | Fuel oil / particulate material slurry compositions and processes |
US11286438B2 (en) | 2016-04-04 | 2022-03-29 | Arq Ip Limited | Fuel oil / particulate material slurry compositions and processes |
US11319492B2 (en) | 2016-04-04 | 2022-05-03 | Arq Ip Limited | Solid-liquid crude oil compositions and fractionation processes thereof |
US11718794B2 (en) | 2016-04-04 | 2023-08-08 | Arq Ip Limited | Solid-liquid crude oil compositions and fractionation processes thereof |
US20220000081A1 (en) * | 2018-06-07 | 2022-01-06 | The Tru Shrimp Company | Raceways and systems thereof |
WO2020065341A1 (en) * | 2018-09-27 | 2020-04-02 | Arq Ip Limited | Processes for utilisation of purified coal compositions as a chemical and thermal feedstock and cleaner burning fuel |
US11407953B2 (en) * | 2018-09-27 | 2022-08-09 | Arq Ip Limited | Processes for utilisation of purified coal compositions as a chemical and thermal feedstock and cleaner burning fuel |
US20220403274A1 (en) * | 2018-09-27 | 2022-12-22 | Arq Ip Limited | Processes for utilisation of purified coal compositions as a chemical and thermal feedstock and cleaner burning fuel |
Also Published As
Publication number | Publication date |
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JP2015030737A (en) | 2015-02-16 |
AU2014297503A1 (en) | 2016-02-11 |
CN105408459A (en) | 2016-03-16 |
WO2015016062A1 (en) | 2015-02-05 |
AU2014297503B2 (en) | 2016-08-25 |
DE112014003532T5 (en) | 2016-04-14 |
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