AU2015293497B2 - Method for producing reformed coal and facility for producing reformed coal - Google Patents
Method for producing reformed coal and facility for producing reformed coal Download PDFInfo
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- AU2015293497B2 AU2015293497B2 AU2015293497A AU2015293497A AU2015293497B2 AU 2015293497 B2 AU2015293497 B2 AU 2015293497B2 AU 2015293497 A AU2015293497 A AU 2015293497A AU 2015293497 A AU2015293497 A AU 2015293497A AU 2015293497 B2 AU2015293497 B2 AU 2015293497B2
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- 239000003245 coal Substances 0.000 title claims abstract description 310
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 39
- 238000001035 drying Methods 0.000 claims abstract description 181
- 238000010438 heat treatment Methods 0.000 claims abstract description 54
- 238000001816 cooling Methods 0.000 claims abstract description 25
- 238000000034 method Methods 0.000 claims abstract description 17
- 238000001704 evaporation Methods 0.000 claims abstract description 15
- 238000002485 combustion reaction Methods 0.000 claims abstract description 14
- 238000003763 carbonization Methods 0.000 claims description 46
- 239000007789 gas Substances 0.000 claims description 17
- 239000002918 waste heat Substances 0.000 claims description 5
- 238000010000 carbonizing Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 8
- 238000000197 pyrolysis Methods 0.000 abstract 3
- 238000009434 installation Methods 0.000 description 60
- 239000000428 dust Substances 0.000 description 19
- 239000000843 powder Substances 0.000 description 8
- 238000010981 drying operation Methods 0.000 description 6
- 239000000446 fuel Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 239000003077 lignite Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- NRNCYVBFPDDJNE-UHFFFAOYSA-N pemoline Chemical compound O1C(N)=NC(=O)C1C1=CC=CC=C1 NRNCYVBFPDDJNE-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000012217 deletion Methods 0.000 description 1
- 230000037430 deletion Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 239000003476 subbituminous coal Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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
- C10L9/00—Treating solid fuels to improve their combustion
- C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B3/00—Drying solid materials or objects by processes involving the application of heat
- F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
- F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
- F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
- F26B3/084—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed with heat exchange taking place in the fluidised bed, e.g. combined direct and indirect heat exchange
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Microbiology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Drying Of Solid Materials (AREA)
Abstract
A method for producing modified coal, said method comprising: a first drying step (S11) for heating air taken from the outside, fluidizing high-water content coal using the heated air to give a fluidized coal bed, and evaporating moisture from the high-water content coal in the fluidized coal bed to give primarily dried coal; a second drying step (S12) for indirectly heating the primarily dried coal, further evaporating moisture from the primarily dried coal to give dried cool and, at the same time, recovering first steam evaporated from the primarily dried coal; a dry distillation step (S20) for dry distilling the dried coal to give modified coal and, at the same time, recovering, as exhaust gas, combustion exhaust gas that remains after supplying dry distillation heat required for dry distillation of the dried coal to thereby generate second steam; and a cooling step (S30) for cooling the modified coal. In the first drying step, the air is indirectly heated by the first steam. In the second drying step, the primarily dried coal is indirectly heated using the second steam.
Description
1
DESCRIPTION
Title of Invention
METHOD FOR PRODUCING REFORMED COAL AND FACILITY FOR PRODUCING REFORMED COAL
Technical Field [0001]
The present invention relates to a method for producing reformed coal and a facility for producing reformed coal that produce reformed coal from high-moisture coal.
Priority is claimed on Japanese Patent Application No. 2014-150073, filed July 23, 2014, the content of which is incorporated herein by reference.
Background Art [0002]
In recent years, methods for producing reformed coal that adjust a fuel ratio to 2 to 4 equivalent to low-volatile-component steam coal to obtain fuel that allows long-distance transportation, for example, by drying or carbonizing coal (high-moisture coal) with a large moisture content, such as brown coal or sub-bituminous coal, have been studied. In addition, the fuel ratio described herein means the weight ratio of a fixed carbon matter with poor combustibility to a volatile matter with good combustibility in coal. The reformed coal with a fuel ratio of 2 to 4 is, for example, burned for power generation in power plants.
In the methods for producing reformed coal from this kind of high-moisture coal. 2 drying of high-moisture coal is important, and the following methods are known as the methods for drying the high-moisture coal.
[0003]
For example, a method of providing a preheater that preheats high-moisture coal, 5 and improving fluidization of the high-moisture coal within a dryer is described in PTL 1. PTL 2 discloses that steam released from a dryer is compressed and is used for drying of high-moisture coal, and steam drain from the dryer is used for preheating and drying. 10 In addition to these, a WTA drying method described in NPL 1 is known as the same drying method.
Citation List Patent Literature 15 [0004] [PTL 1] Japanese Unexamined Patent Application, First Publication No. 2013-178026 [PTL 2] Japanese Unexamined Patent Application, First Publication No. 2013-178028 20 [NPL] [0005] [NPL 1] "A modern process for treating and drying lignite", WTA TECHNOLOGY, [searched on June 12, Heisei 26], Internet URL:https://www.rwe.com/web/cms/mediablob/en/234566/data/213182/6/rwe-power-ag/ 25 innovations/coal-innovation-centre/fluidized-bed-drying-with-internal-waste-heat-utilizat 3 2015293497 18 Μ 2017 utilization-wta/Brochure-WTA-Technology-A-modem-process-for-treating-and-drying-lignite.pdf.pdf
Summary of Invention [0006]
Brown coal as a representative of high-moisture coal has the property of being apt to ignite (spontaneous ignition) if the moisture content falls.
Therefore, for example, in a case where the high-moisture coal is indirectly heated with steam, and the high-moisture coal containing 50 to 60% of moisture is dried to such a degree that 10% of moisture is contained in a mass ratio, methods of drying the inside of the dryer in a steam atmosphere without oxygen have been put in practical use as countermeasures against ignition during a drying operation.
[0007]
However, in order to indirectly heat and dry the high-moisture coal, a large amount of heating steam is required. For this reason, if the high-moisture coal is not dried using inexpensive steam, there is a problem in that the drying cost of the high-moisture coal becomes high, and the production cost of the reformed coal also becomes high.
[0008]
Therefore, as methods of securing a large amount of heating steam, for example, methods of compressing steam that has evaporated during the drying of the high-moisture coal, and using this compressed steam for the drying of the high-moisture coal, thereby reducing the content of steam from the outside required for the drying of the high-moisture coal have been developed.
However, in order to compress steam, an expensive compressor and a tremendous amount of electricity for compression are required. Consequently, the steam for the drying of the high-moisture coal obtained in these related-art methods is expensive.
AH26(13353735_1):KEH 4 2015293497 18 Μ 2017 [0009]
There is a need to provide a method for producing reformed coal and a facility for producing reformed coal that can dry high-moisture coal without igniting the high-moisture coal, can cheaply obtain steam for drying the high-moisture coal, and/or can also reduce the amount of steam for drying the high-moisture coal.
[0009a]
It is an object of the present invention to at least substantially address one or more of the above needs, or at least provide a useful alternative to the above discussed methods.
[0010] A method for producing reformed coal related to an aspect of the invention is a method for producing reformed coal that produces reformed coal from high-moisture coal that is coal that contains 45% or more of moisture in a mass ratio. The method includes a first drying step of heating air taken in from the outside, fluidizing the high-moisture coal using the heated air to obtain a coal fluidized bed, and evaporating moisture from the high-moisture coal in the coal fluidized bed to obtain primarily dried coal; a second drying step of indirectly heating the primarily dried coal, further evaporating moisture from the primarily dried coal to obtain dried coal, and recovering first steam evaporated from the primarily dried coal; a carbonization step of carbonizing the dried coal to obtain reformed coal and recovering, as waste heat, combustion exhaust gas that remains after supplying carbonization heat required for carbonization of the dried coal, thereby generating second steam; and a cooling step of cooling the reformed coal. In the first drying step, the air is indirectly heated with the first steam. In the second drying step, the primarily dried coal is indirectly heated using the second steam.
[0011] A facility for producing reformed coal related to an aspect of the invention is a facility for producing reformed coal that produces reformed coal from high-moisture coal that is coal that contains 45% or more of moisture in a mass ratio. The facility includes a drying unit that evaporating moisture from the high-moisture coal to obtain dried coal; a carbonization unit that carbonize the dried coal to obtain the reformed coal; and a cooling unit that cooling the
AH26(13353735_1):KEH 5 2015293497 18 Μ 2017 reformed coal. The drying unit includes a first drying unit that heats air taken in from the outside, fluidizes the high-moisture coal using the heated air to obtain a coal fluidized bed, and evaporates moisture from the high-moisture coal in the coal fluidized bed to obtain primarily dried coal; and a second drying unit that indirectly heats the primarily dried coal, further evaporates moisture from the primarily dried coal to obtain dried coal, and recovers first steam evaporated from the primarily dried coal. The carbonization unit carbonize the dried coal and recovers, as waste heat, combustion exhaust gas that remains after supplying carbonization heat required for carbonization of the dried coal, thereby generating second steam. The first drying unit indirectly heats the air with the first steam. The second drying unit indirectly heats the primarily dried coal using the second steam.
[0012]
It is more preferable that in the first drying step, the coal fluidized bed be indirectly heated with the first steam.
[0013]
It is more preferable that the first drying unit indirectly heat the coal fluidized bed with the first steam.
[0014]
It is more preferable that the amount of moisture that evaporates in the second drying step from the primarily dried coal after the high-moisture coal becomes the primarily dried coal be twice as large as the amount of moisture that evaporates in the first drying step from the high-moisture coal.
[0015]
It is more preferable that in the first drying step, the air be indirectly heated with the second steam.
[0016]
AH26(13353735 1):KEH 6 2015293497 18 Μ 2017
According to at least one embodiment of the method for producing reformed coal and the facility for producing reformed coal in the invention, high-moisture coal may be dried without being ignited, steam for drying the high-moisture coal may be cheaply obtained, and/or the amount of steam for drying the high-moisture coal may be reduced.
Brief Description of Drawings [0016a]
Preferred embodiments of the present invention will now be described, by way of examples only, with reference to the accompanying drawings: [0017] FIG. 1 is a block diagram of a facility for producing reformed coal of a first embodiment of the invention. FIG. 2 is a block diagram of a carbonization installation of the production facility illustrated in FIG. 1. FIG. 3 is a flowchart illustrating a method for producing reformed coal of the first embodiment. FIG. 4 is an operation diagram illustrating a drying operation of a first drying
AH26(13353735_1):KEH 7 step based on a chart of low temperature and humidity for air and water. FIG 5 is a block diagram of a facility for producing reformed coal of a second embodiment of the invention. 5 Description of Embodiments [0018] (First Embodiment)
Hereinafter, a first embodiment of a facility for producing reformed coal (hereinafter also abbreviated as "production facility") related to the invention will be 10 described, referring to FIG. 4 from FIG. 1.
[0019]
As illustrated in FIG. 1, a production facility 1 of the present embodiment includes a drying installation (drying unit) 10 that evaporates moisture from high-moisture coal Ml to obtain dried coal M3, a carbonization installation 15 (carbonization unit) 30 that carbonize the dried coal M3, of which the moisture has evaporated in the drying installation 10, to obtain reformed coal M4, and a cooling installation (cooling unit) 40 that cools the reformed coal M4 obtained in the carbonization installation 30.
[0020] 20 In addition, the high-moisture coal Ml described herein means coal that contains 45% or more of total moisture in a mass ratio. Reference signs M3, M4, and reference sign M2 to be described below do not mean pipes, conveyors, or the like, but mean dried coal, reformed coal, and primarily dried coal to be supplied by the pipes, the conveyors, or the like. 25 [0021]
The drying installation 10 includes a first drying installation (first drying unit) 11 and a second drying installation (second drying unit) 12.
[0022]
The first drying installation 11 heats air M5 taken in from the outside, fluidizes the high-moisture coal Ml with the heated air M5 to obtain a coal fluidized bed M6, thereby executing a drying operation to turn the high-moisture coal Ml into primarily dried coal M2.
The second drying installation 12 indirectly heats the primarily dried coal M2 processed in the first drying installation 11 with steam in a carbonization step (hereinafter referred to as second steam) to be described below, and further evaporates moisture from the primarily dried coal M2 to obtain dried coal M3.
[0023]
The first drying installation 11 has an air fan 15 that takes in the air M5 from the outside, an air preheater 16 that heats the air M5 taken in by the air fan 15, an air heater 17 that further heats the air M5 heated by the air preheater 16, and an air fluidized bed dryer (hereinafter referred to as a dryer) 18 to which the air M5 heated by the air heater 17 is supplied.
[0024]
The high-moisture coal Ml is supplied to the dryer 18 in a predetermined constant weight per time. Additionally, an exhaust air dust collector (hereinafter referred to as a dust collector) 19 for recovering fine coal powder entrained in exhaust air is connected to the dryer 18.
[0025] A heating tube (heating pipe) 22 connected to (communicating with) one end part of a second steam supply pipe (hereinafter referred to as a supply pipe) 21 into 9 which second steam flows is disposed within the second drying installation 12.
The other end part of the supply pipe 21 is connected to the carbonization installation 30. At an end part of the heating tube 22 that is not connected to the supply pipe 21, steam-condensed water is gathered in a pipe (not illustrated) disposed substantially under the atmospheric pressure, and is returned as condensate for steam if necessary.
[0026]
The second drying installation 12 is connected to the dryer 18 of the first drying installation 11. The primarily dried coal M2 supplied into the second drying installation 12 from the dryer 18 is indirectly heated by coming into contact with an outer surface of the heating tube 22 installed inside the second drying installation 12, and is dried when the moisture in the primarily dried coal M2 evaporates. A pipe 23 branches from the supply pipe 21 and is connected to the air heater 17.
In order to heat the air M5 taken in from the outside with the air heater 17, steam (second steam to be described below) is supplied to the air heater 17 via the pipe 23.
[0027]
One end part of a first steam supply pipe (hereinafter referred to as a supply pipe) 24 into which steam in an indirect heating and drying step (hereinafter referred to as first steam) flows is connected to the second drying installation 12 via the dust collector 25.
The other end part of the supply pipe 24 extends to the air preheater 16 and is connected to the air preheater 16. Accordingly, the first steam is supplied from the second drying installation 12 via the supply pipe 24 to the air preheater 16. The air M5 taken in from the outside is indirectly heated with the first steam in the air preheater 16.
[0028] 10
As illustrated in FIG 2, the carbonization installation 30 has, for example, a well-known external heat type rotary kiln 31, a secondary combustion unit 32 connected to the rotary kiln 31, a steam-generating unit 33 connected to the secondary combustion unit 32, a dust removal unit 34 connected to the steam-generating unit 33, a suction fan 35 connected to the dust removal unit 34, and an exhaust gas treatment unit 36 connected to the suction fan 35.
[0029]
The rotary kiln 31 is connected to the second drying installation 12 of the drying installation 10. The rotary kiln 31 is set to be in an environment of hundreds of degrees Celsius where oxygen is not present therein, and carbonize the dried coal M3 supplied from the second drying installation 12 therein, and obtains the reformed coal M4. The reformed coal M4 is supplied to the cooling installation 40.
In addition, the secondary combustion unit 32, the steam-generating unit 33, the dust removal unit 34, the suction fan 35, and the exhaust gas treatment unit 36 will be described below.
[0030]
The cooling installation 40 cools the reformed coal M4 carbonized in the carbonization installation 30 to a temperature at which the reformed coal does not ignite due to catalytic oxidation with air, for example, tens of degrees Celsius.
[0031]
Next, a method for producing the reformed coal M4 (also hereinafter abbreviated as a "production method") of the present embodiment using the production facility 1 configured as described above will be described.
[0032] FIG. 3 is a flowchart illustrating the method for producing of the present 11 embodiment.
This production method includes a drying step S10 of evaporating moisture from high-moisture coal Ml to obtain dried coal M3, a carbonization step S20 of carbonizing the dried coal M3 after the drying step S10, to obtain reformed coal M4, and 5 a cooling step S30 of cooling the reformed coal M4 after the carbonization step S20.
[0033]
The drying step S10 includes an air fluidized bed drying step (hereinafter referred to as a first drying step) Sll of drying the high-moisture coal Ml to obtain primarily dried coal M2, and an indirect heating and drying step (hereinafter referred to 10 as a second drying step) S12 of further drying the primarily dried coal M2 to obtain the dried coal M3.
[0034]
In the first drying step Sll, air M5 taken in from the outside is heated, the coal fluidized bed M6 is obtained by fluidizing the high-moisture coal Ml with the heated air 15 M5, and primarily dried coal M2 is obtained by evaporating and drying moisture from the high-moisture coal Ml during flow. In the second drying step S12, the dried coal M3 is obtained by further evaporating moisture from the primarily dried coal M2 after the first drying step Sll.
[0035] 20 In the first drying step Sll, air M5 is taken in from the outside by the air fan 15.
In addition, as will be described below, the first steam is supplied from the second drying installation 12 through the supply pipe 24 to the dust collector 25 and is further supplied from the dust collector 25 through the supply pipe 24 to the air preheater 16.
Accordingly, the taken-in air M5 is indirectly heated by the first steam by coming into 25 contact with an outer surface of the supply pipe 24 within the air preheater 16. 12 [0036]
The air M5 heated in the air preheater 16 is further supplied to the air heater 17. In addition, as will be described below, the second steam is supplied from the carbonization installation 30 through the pipe 23 to the air heater 17. Accordingly, the 5 taken-in air M5 is indirectly heated with the second steam by coming into contact with an outer surface of the pipe 23 within the air heater 17.
That is, the air M5 heated in the air preheater 16 is still more indirectly heated in the air heater 17.
[0037] 10 In addition, the first steam and the second steam used in the air preheater 16 and the air heater 17, respectively, are discharged to the outside as steam-condensed water or returned as condensate for steam if necessary.
[0038]
In addition, in the present embodiment, cases where the air M5 is indirectly 15 heated by coming into contact with the outer surface of the supply pipe 24 within the air preheater 16 and coming into contact with the outer surface of the pipe 23 within the air heater 17 are exemplified.
However, the configuration for indirectly heating the air M5 is not limited to the supply pipes 24 and 23. For example, indirect heat exchangers of a multi-tube type 20 (shell and tube type), and a plate type, or the like can be appropriately selected and used. The same may be said of the heating tube 22 of the second drying installation 12, and a heating tube 52 of the dryer 18 to be described below.
[0039]
The air M5 heated in the air heater 17 is supplied to the dryer 18. The 25 temperature of the air M5 when being supplied to the dryer 18 just has to be a 13 temperature that does not reach an ignition point even if the high-moisture coal Ml oxidizes and generates heat, and is preferably 120°C or lower from a viewpoint of prevention of ignition.
[0040] 5 The high-moisture coal Ml is supplied to the dryer 18. The average particle diameter of the high-moisture coal Ml is, for example, 3 mm. In this example, the high-moisture coal Ml before performing the first drying step Sll in which the high-moisture coal is supplied to the dryer 18 contains 60% of moisture in a mass ratio, and the remaining 40% is composed of about 20% of a volatile matter and about 20% of 10 a fixed carbon matter, and some ash content.
[0041]
The high-moisture coal Ml supplied to the dryer 18 is fluidized with the air M5 supplied to the dryer 18, and becomes the coal fluidized bed M6. The high-moisture coal Ml within the coal fluidized bed M6 is heated by the heated air M5, and thereby, 15 moisture evaporates from the high-moisture coal Μ1. When moisture evaporates from the high-moisture coal Ml in this way, the high-moisture coal Ml that constitutes the coal fluidized bed M6 becomes the primarily dried coal M2.
[0042]
In addition, the air M5 supplied to the dryer 18 is humidified together with the 20 evaporated moisture from the high-moisture coal Ml. The air M5 humidified within the dryer 18 becomes exhaust air that has entrained fine coal powder or the like, is discharged out of the dryer 18, and is supplied to the dust collector 19. This exhaust air is separated into exhaust air, fine coal powder, and the like by the dust collector 19. The fine coal powder or the like separated in the dust collector 19 is recovered, is 25 agglomerated if necessary, and is returned to the primarily dried coal M2. Meanwhile, 14 the exhaust air (air) from which the fine coal powder or the like has been separated is discharged from the dust collector 19 to the outside.
[0043]
The temperature inside the coal fluidized bed M6 of the dryer 18 is desirably a 5 temperature at which oxidization and heat generation of the high-moisture coal Ml caused by oxygen in the air M5 do not occur, and is preferably 60°C or lower. That is, it is preferable that the dryer 18 perform drying before the amount of moisture of the primarily dried coal M2 reaches a critical moisture content. For example, it is preferable to perform a drying operation in a range until moisture falls to 20% in a 10 weight ratio, as an example, that is, in a constant-rate drying speed zone.
In addition, in a case where the primarily dried coal M2 is dried up to the amount of moisture lower than the critical moisture content, it is preferable to set the internal temperature of the coal fluidized bed M6 to as relatively low a temperature as 60°C or lower to perform drying of the high-moisture coal Ml. 15 [0044]
After the drying operation of the coal fluidized bed M6 in the dryer 18 ends, the first drying step Sll is ended, proceeds to the second drying step S12, and the primarily dried coal M2 processed in the dryer 18 is supplied to the second drying installation 12.
[0045] 20 In the second drying step S12, the primarily dried coal M2 is indirectly heated via the heating tube 22 by the second steam to be supplied through the supply pipe 21 within the second drying installation 12. Within the second drying installation 12, the primarily dried coal M2 is indirectly heated by coming into contact with the outer surface of the heating tube 22. 25 By the above configuration, the primarily dried coal M2 is heated by the heating 15 tube 22 disposed within the second drying installation 12, and moisture evaporates from the primarily dried coal M2.
[0046]
In the drying step S10, drying is performed until the high-moisture coal Ml 5 becomes the dried coal M3.
In this case, it is preferable from a viewpoint of thermal efficiency to set the amount of moisture that evaporates until the primarily dried coal M2 becomes the dried coal M3 in the second drying step S12 such that the total amount of the first steam obtained from the moisture that evaporates in the second drying step S12 balances with 10 (becomes equal to) the total amount of steam required for drying from the high-moisture coal Ml to the primarily dried coal M2 in the first drying step Sll.
[0047]
It is preferable that the amount of the moisture that evaporates in the second drying step S12 from the primarily dried coal M2 after a given amount of the 15 high-moisture coal Ml becomes the primarily dried coal M2 in the first drying step Sll be twice as large as the amount of the moisture that evaporates in the first drying step Sll from the given amount of the high-moisture coal Ml.
That is, for example, in a case where the high-moisture coal Ml of which the moisture content is 60% in a weight ratio is dried in the drying step S10 until the dried 20 coal M3 of which the moisture content is 10% in a weight ratio is obtained, it is preferable that the high-moisture coal Ml of which the moisture content thereof is 60% in a weight ratio be dried in the first drying step Sll, and be turned into primarily dried coal M2 of which the moisture content is 50% in a weight ratio.
[0048] 25 Moreover, by setting the temperature of the air M5 when the dryer 18 is supplied 16 to, for example, 120°C or lower, setting the temperature inside the dryer 18 to, for example, 60°C or lower, and by setting the moisture content of the primarily dried coal M2 at the end of the first drying step Sll to 50% in a weight ratio, the high-moisture coal Ml can be dried without being ignited even in an atmosphere of the air M5 in the first 5 drying step Sll.
[0049]
The second steam supplied to the heating tube 22 installed within the second drying installation 12 through a conduit of the supply pipe 21 is condensed within the heating tube 22, and is discharged as steam-condensed water. 10 The first steam that is the moisture that has evaporated from the primarily dried coal M2 is recovered, and is supplied to the dust collector 25 through the supply pipe 24. Accordingly, even if, for example, fine coal powder or the like is entrained in the first steam, the first steam, the fine coal powder, and the like can be separated within the dust collector 25. The separated first steam is supplied from the dust collector 25 through 15 the supply pipe 24 to the air preheater 16. That is, the first steam obtained in the second drying step S12 as illustrated in FIG. 3 is used in the first drying step Sll.
[0050]
In addition, a portion of the first steam supplied from the dust collector 25 through the supply pipe 24 to the air preheater 16 branches from the supply pipe 24, for 20 example on the way, and is supplied to the second drying installation 12. Accordingly, in the second drying step 12, the primarily dried coal M2 can be dried in an atmosphere of steam as in the related art.
In addition, when a portion of the first steam is supplied to the second drying installation 12, a flow rate using ventilation means, such as a fan (not illustrated) or the 25 like, may be raised. Accordingly, the primarily dried coal M2 can be indirectly heated 17 while being fluidized within the second drying installation 12.
In addition, the fine coal powder or the like separated in the dust collector 25 may be returned to the dried coal M3 supplied from the second drying installation 12 to the carbonization installation 30, for example after being agglomerated if necessary. 5 [0051]
If the drying treatment of the primarily dried coal M2 in the second drying installation 12 ends and the dried coal M3 is produced, the dried coal M3 produced in the second drying installation 12 is supplied to the carbonization installation 30.
Accordingly, the second drying step S12 ends and proceeds to the carbonization 10 step S20.
[0052]
In the carbonization step S20, the dried coal M3 is carbonized as mentioned above in the carbonization installation 30. In this carbonization operation, a gas or tar component is generated by the volatile matter of the dried coal M3 being thermally 15 decomposed within the rotary kiln 31 illustrated in FIG. 2.
The gas or tar component that has been generated inside the rotary kiln 31 is discharged from the inside of the rotary kiln 31 to the outside, and is combusted together with air supplied in order to heat the rotary kiln 31 outside. Accordingly, the quantity of heat (carbonization heat) required for carbonization of the dried coal M3 can be obtained. 20 This carbonization heat is supplied to the rotary kiln 31.
[0053]
In addition, the gas or tar component that has remained without being combusted in the rotary kiln 31 is supplied from the rotary kiln 31 to the secondary combustion unit 32. A high-temperature combustion exhaust gas can be obtained by 25 still more completely combusting the gas or tar component in the secondary combustion 18 unit 32.
In the steam-generating unit 33, the second steam can be obtained by recovering waste heat using this combustion exhaust gas.
[0054]
This second steam may be low-pressure steam that has a relatively low pressure (for example, 0.4 MPaG or higher (mega-pascal gage)). The combustion exhaust gas is suctioned by the suction fan 35 through dust removal treatment performed by the dust removal unit 34. Moreover, the combustion exhaust gas is discharged from the carbonization installation 30 through exhaust gas treatment, such as desulfurization performed by the exhaust gas treatment unit 36.
[0055]
As illustrated in FIG. 1, the second steam passes through the supply pipe 21 and the heating tube 22, and is supplied to the second drying installation 12. That is, the second steam obtained in the carbonization step S20 as illustrated in FIG. 3 is used in the second drying step S12. A portion of the second steam that flows through the supply pipe 21 is supplied to the air heater 17 through the pipe 23 illustrated in FIG. 1.
[0056]
After the production of the reformed coal M4 in the carbonization installation 30 ends, the reformed coal M4 produced in the carbonization installation 30 is supplied to the cooling installation 40. Accordingly, the carbonization step S20 ends and proceeds to the cooling step S30.
In addition, the temperature of the reformed coal M4 when the carbonization step S20 has ended is preferably, for example, 400°C or higher and 650°C or lower and more preferably 450°C or higher and 600°C or lower, with respect to a fuel ratio of 2 to 19 4.
[0057]
In the cooling step S30, the reformed coal M4 produced in the carbonization installation 30 is cooled up to about tens of degrees Celsius by a well-known cooling 5 system.
According to the above process, the reformed coal M4 equivalent to low-volatile-component steam coal of which the fuel ratio is 2 to 4 can be produced.
[0058] (Example) 10 Here, an example of the invention will be described in more detail through illustration of a specific example. However, the invention is not limited to the following example. FIG. 4 is a chart of low temperature and humidity for air and water. A horizontal axis of FIG 4 represents the temperature (dry-bulb temperature) of air, and a 15 vertical axis represents the humidity (absolute humidity, kg-steam/kg-dry air) of air. Additionally, in FIG. 4, an upwardly and rightwardly slanting curve represents relative humidity.
In the dryer 18, description will be made on the assumption of a drying operation before the amount of moisture of the primarily dried coal M2 reaches the 20 critical moisture content. In air fluidized bed drying, the amount of vaporization of moisture from coal becomes equal to the amount of moisture carried out of a system by air. Thus, the amount of moisture carried out by air is illustrated using the chart of low temperature and humidity.
[0059]
25 If the temperature of external air is set to 25°C, this air is in the state of Point A 20 if the relative humidity is 100%. If the air in the state of Point A is heated to, for example, 70°C, the temperature rises with the amount of steam included in the air being constant, and air is brought into a state of Point B1.
[0060] 5 If the air in the state of this Point B1 is supplied to the dryer 18 of the drying installation 10, the air is adiabatically cooled while fluidizing high-moisture coal, moves along an adiabatic cooling line (a downwardly and rightwardly straight line in FIG. 4), and thereby is brought into a state of Point Cl where the temperature is about 35°C and the relative humidity is 95%. That is, the air at an outlet of the dryer 18 is brought into 10 the state of Point C1.
When the state of the air becomes the state of Point Cl from the state Point Bl, the amount of moisture of 0.014 (kg-steam/kg-dry air) corresponding to a length LI of the vertical axis between Point Bl and Point Cl can be removed from the high-moisture coal due to evaporation (moisture can be taken into air). 15 In addition, although a case where the relative humidity of the air becomes 95% due to the adiabatic cooling is described herein, the relative humidity is not limited to 95%. The relative humidity is influenced by, for example, the operation conditions of a dryer.
[0061] 20 If the air in the state of Point A is heated to, for example, 120°C, the air is brought into a state of Point B2. If the air in the state of this Point B2 is supplied to the dryer 18, the air is adiabatically cooled to about 42°C and a relative humidity of 95%, and is brought into a state of Point C2.
When the state of the air becomes the state of Point C2 from the state of Point 21 B2, the moisture of 0.031 (kg-steam/kg-dry air) corresponding to a length L2 of the vertical axis between Point B2 and Point C2 can be evaporated.
[0062]
In addition, since a possibility that the high-moisture coal ignite becomes high in 5 practice, it is difficult to heat air to the following temperature, but an example will be described just for reference.
If the air in the state of Point A is heated to, for example, 220°C out of a range described in FIG. 4, and the air in this state is supplied to the dryer 18, the air is adiabatically cooled and is brought into a state of Point C3 where the relative humidity is 10 95%. In this case, the moisture of 0.058 (kg-steam/kg-dry air) corresponding to length L3 can be evaporated.
[0063]
As described above, according to the production facility 1 and the production method for reformed coal of the present embodiment, the drying step S10 has the first 15 drying step S11 and the second drying step S12.
Then, the air taken in from the outside in the first drying step SI 1 using the first steam generated in the second drying step S12 is indirectly heated, and the primarily dried coal M2 is indirectly heated in the second drying step SI2 using the second steam produced through the exhaust heat recovery in the carbonization step S20. 20 [0064]
In this way, the inexpensive second steam produced through the exhaust heat recovery in the carbonization step S20 can be used for the second drying step S12. Additionally, in the drying step S10, in order to use the first steam generated in the second drying step S12 for a drying heat source in the first drying step SI 1, the 25 high-moisture coal Ml can be dried in two steps including the first drying step Sll and 22 the second drying step SI2.
[0065]
In the present embodiment, the first steam generated in the second drying step S12 is utilized for internal circulation. For this reason, the amount of steam utilized for 5 internal circulation can be reduced, and the amount of steam required to dry the high-moisture coal Ml can be reduced by 30% compared to the related-art production methods described in for example, PTLs 1 and 2.
In this way, a tremendous amount of electricity is not required for drying of the high-moisture coal Ml, and the amount of steam for drying the high-moisture coal Ml 10 can be reduced. Moreover, since the temperature inside the dryer 18 is as relatively low as 60°C or lower, drying can be performed without igniting the high-moisture coal Ml.
[0066]
The amount of moisture that evaporates in the second drying step S12 is made to be twice as large as the amount of moisture that evaporates in the first drying step SI 1 15 from a given amount of the high-moisture coal Μ1. Accordingly, the total amount of the first steam obtained in the second drying step S12, the total amount of the steam required for the drying in the first drying step SI 1 become equal to each other, and consequently, the thermal efficiency in this production method can be enhanced.
[0067] 20 In the first drying step S11, the temperature of the air M5 can be more reliably raised by indirectly heating the air M5 taken in from the outside with the second steam.
In addition, although the air M5 taken in from the outside is supplied to the dryer 18 in the drying step S10, instead of the air M5, for example, inert (inactive) gases, such as nitrogen, may be used. 25 [0068] 23 (Second Embodiment)
Next, a second embodiment of the invention will be described, referring to FIGS. 4 and 5. However, in the present embodiment, the same parts as those of the first embodiment will be designated by the same reference signs and the description thereof 5 will be omitted, and only differences will be described.
[0069]
As illustrated in FIG. 5, the production facility 2 of the present embodiment has a connecting pipe 51 connected to the supply pipe 24, and the heating tube (heating pipe) 52 connected to the connecting pipe 51 and disposed within the dryer 18, in addition to 10 the respective components of the production facility 1 of the first embodiment.
[0070]
The heating tube 52 is disposed so as to become horizontal to, for example, a portion (the surface of the coal fluidized bed M6) in which the coal fluidized bed M6 is formed. The coal fluidized bed M6 within the dryer 18 comes into contact with an outer 15 surface of the heating tube 52. The first steam that passes through the supply pipe 24 is supplied to the heating tube 52 through the connecting pipe 51. Accordingly, the coal fluidized bed M6 is indirectly heated with the first steam by coming into contact with the outer surface of the heating tube 52.
In addition, one end part of the heating tube 52 is connected to the connecting 20 pipe 51. The first steam becomes steam-condensed water via the other end part of the heating tube 52, and is discharged to the outside.
[0071]
The production method of the present embodiment using the production facility 2 configured as described above will be described. 25 In the first drying step S11, the first steam that has flowed into the supply pipe 24 24 from the second drying installation 12 further flows into the connecting pipe 51 and the heating tube 52. Accordingly, the coal fluidized bed M6 can be indirectly heated with the first steam via the heating tube 52.
Accordingly, the high-moisture coal Ml is indirectly heated not only with the air 5 M5, which has been taken in from the outside and heated, but also with the first steam.
[0072] (Example)
Here, an example of the invention will be described in more detail through illustration of a specific example. However, the invention is not limited to the following 10 example.
[0073]
In FIG. 4, if the air in the state of Point A is heated to, for example, 120°C, the air is brought into the state of Point B2. When the coal fluidized bed M6 is heated in the heating tube 52 provided within the dryer 18, the air in the state of Point B2 is 15 brought into the state of the aforementioned Point C3 if heating is performed such that a heating heat quantity ratio between the quantity of heat by heating air and the quantity of heat by the indirect heating using the heating tube 52 becomes 1:1 (the length L3 in FIG. 4 becomes twice as large as the length L2).
For this reason, if a heat source having a higher temperature than the wet bulb 20 temperature of 49°C that is the temperature of an intersection point between a line that passes through Point C3 and is parallel to the vertical axis, and the horizontal axis, is used, this heat source can be used instead of the first steam.
[0074]
In this way, in a case where the heating heat quantity ratio between the quantity 25 of heat by the heating air and the quantity of heat by the indirect heating using the 25 heating tube 52 is 1:1, even in the first steam of about 110°C, the effect that is the same as that in a case where external air is preheated from 120°C to 220°C outside the production facility 2 and that the moisture of 0.058 (kg-steam/kg-dry air) can be evaporated is obtained. 5 [0075]
In addition, the effect equivalent to the quantity of heat when the coal fluidized bed M6 is indirectly heated in the heating tube 52 becomes a drying effect that is the same as that in a case where external air is heated as much as the quantity of heat that balances with the quantity of heat when the coal fluidized bed M6 is heated from 120°C. 10 Additionally, the heating heat quantity' ratio between the quantity of heat by the heating air and the quantity of heat by the indirect heating using the heating tube 52 may be other than 1:1.
[0076]
As described above, according to the production facility 2 and the production 15 method for reformed coal of the present embodiment, the high-moisture coal Μ1 can be dried without being ignited, and steam for drying the high-moisture coal Ml can be inexpensive exhaust heat recovery steam (second steam). Additionally, the amount of steam can also be reduced.
[0077] 20 Moreover, in the first drying step S11, the coal fluidized bed M6 is indirectly heated with the first steam via the heating tube 52. Therefore, by performing indirect heating not only with the air M5 but also with the first steam, a larger amount of moisture can be evaporated from the high-moisture coal Ml while maintaining the humidity inside the dryer 18 at a relatively low humidity. 25 In this way, by including the heating tube 52, the amount of air required for 26 drying can be reduced, and the production facility 2 can be miniaturized.
[0078]
Although the first and second embodiments of the invention have been described above in detail with reference to the drawings, specific configurations are not limited to 5 these embodiments, and changes, combinations, deletions, or the like of the configuration are also included without departing from the scope of the invention. Moreover, the respective configurations shown in the respective embodiments can be appropriately combined together and used.
[0079] 10 For example, in the first embodiment and the second embodiment, in order to make the humidity of the air M5 higher when being supplied to the dryer 18, the air M5 may be heated with the steam obtained outside the production facility. Meanwhile, when the humidity of the air M5 when being supplied to the dryer 18 is sufficiently high, the air M5 may not be heated with the second steam. 15 [0080]
Additionally, in the first embodiment and the second embodiment, the primarily dried coal M2 is obtained by evaporating moisture from the high-moisture coal Ml, and the dried coal M3 is obtained by further evaporating moisture from the primarily dried coal M2. However, in a case where the drying condition (the evaporation condition of 20 moisture) of each drying installation is ascertained, the drying condition may be estimated, for example, by directly measuring the amount of moisture of each coal of the primarily dried coal M2 and the dried coal M3, or on the basis of the drying temperature within each drying installation, a residence time obtained from a pressure difference between coal beds, or the like. However, the invention is not limited to these methods. 25 [0081] 27
Additionally, in a case where an excessive second steam is present in the production facility, the second steam may be made to flow through the heating tube 52.
The production facility need not include the air heater 17. In this case, the temperature of the air M5 for drying becomes, for example, a maximum of 100°C, and preferably 70 to 90°C.
Industrial Applicability [0082]
According to the invention, high-moisture coal can be dried without being ignited, steam for drying the high-moisture coal can be cheaply obtained, and the amount of steam for drying the high-moisture coal can also be reduced. Therefore, the invention has industrial applicability.
Reference Signs List [0083] 1,2: PRODUCTION FACILITY (FACILITY FOR PRODUCING REFORMED COAL) 10: DRYING INSTALLATION (DRYING UNIT) 11: FIRST DRYING INSTALLATION (FIRST DRYING UNIT) 12: SECOND DRYING INSTALLATION (SECOND DRYING UNIT) 30: CARBONIZATION INSTALLATION (CARBONIZATION UNIT) 40: COOLING INSTALLATION (COOLING UNIT)
51: CONNECTING PIPE Ml: HIGH-MOISTURE COAL M2: PRIMARILY DRIED COAL 28
M3: DRIED COAL M4: REFORMED COAL M5: AIR 5
M6: COAL FLUIDIZED BED S10: DRYING STEP S11: FIRST DRYING STEP (AIR FLUIDIZED BED DRYING STEP)
S12: SECOND DRYING STEP (INDIRECT HEATING AND DRYING STEP)
S20: CARBONIZATION STEP 10 S30: COOLING STEP
Claims (6)
1. A method for producing reformed coal that produces reformed coal from high-moisture coal that is coal that contains 45% or more of moisture in a mass ratio, the method comprising: a first drying step of heating air taken in from the outside, fluidizing the high-moisture coal using the heated air to obtain a coal fluidized bed, and evaporating moisture from the high-moisture coal in the coal fluidized bed to obtain primarily dried coal; a second drying step of indirectly heating the primarily dried coal, further evaporating moisture from the primarily dried coal to obtain dried coal, and recovering first steam evaporated from the primarily dried coal; a carbonization step of carbonizing the dried coal to obtain reformed coal and recovering, as waste heat, combustion exhaust gas that remains after supplying carbonization heat required for carbonization of the dried coal, thereby generating second steam; and a cooling step of cooling the reformed coal, wherein in the first drying step, the air is indirectly heated with the first steam, and wherein in the second drying step, the primarily dried coal is indirectly heated using the second steam.
2. The method for producing reformed coal according to Claim 1, wherein in the first drying step, the coal fluidized bed is indirectly heated with the first steam.
3. The method for producing reformed coal according to Claim 1 or 2, wherein the amount of moisture that evaporates in the second drying step from the primarily dried coal after the high-moisture coal becomes the primarily dried coal is twice as large as the amount of moisture that evaporates in the first drying step from the high-moisture coal.
4. The method for producing reformed coal according to Claim 1, wherein in the first drying step, the air is indirectly heated with the second steam.
5. A facility for producing reformed coal that produces reformed coal from high-moisture coal that is coal that contains 45% or more of moisture in a mass ratio, the facility comprising: a drying unit that evaporating moisture from the high-moisture coal to obtain dried coal; a carbonization unit that carbonize the dried coal to obtain the reformed coal; and a cooling unit that cooling the reformed coal, wherein the drying unit includes: a first drying unit that heats air taken in from the outside, fluidizes the high-moisture coal using the heated air to obtain a coal fluidized bed, and evaporates moisture from the high-moisture coal in the coal fluidized bed to obtain primarily dried coal; and a second drying unit that indirectly heats the primarily dried coal, further evaporates moisture from the primarily dried coal to obtain dried coal, and recovers first steam evaporated from the primarily dried coal, wherein the carbonization unit carbonize the dried coal and recovers, as waste heat, combustion exhaust gas that remains after supplying carbonization heat required for carbonization of the dried coal, thereby generating second steam, wherein the first drying unit indirectly heats the air with the first steam, and wherein the second drying unit indirectly heats the primarily dried coal using the second steam.
6. The facility for producing reformed coal according to Claim 5, wherein the first drying unit indirectly heats the coal fluidized bed with the first steam.
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| JP2014150073A JP6322509B2 (en) | 2014-07-23 | 2014-07-23 | Modified coal production method and modified coal production apparatus |
| JP2014-150073 | 2014-07-23 | ||
| PCT/JP2015/065461 WO2016013293A1 (en) | 2014-07-23 | 2015-05-28 | Method for producing modified coal and device for producing modified coal |
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| CN106440669A (en) * | 2016-11-30 | 2017-02-22 | 陈锦权 | Normal-pressure and negative-pressure combined drying equipment using self-produced superheated steam and material drying method thereof |
| CN107869896A (en) * | 2017-10-25 | 2018-04-03 | 长沙科悦企业管理咨询有限公司 | Steam-type medicinal material sterilizing and drying device |
| JP6419375B1 (en) * | 2018-05-16 | 2018-11-07 | 新日鉄住金エンジニアリング株式会社 | Drying apparatus and drying method |
| JP7416654B2 (en) * | 2020-03-30 | 2024-01-17 | 日鉄エンジニアリング株式会社 | Modified coal manufacturing method and manufacturing equipment |
| CN114517116A (en) * | 2022-02-14 | 2022-05-20 | 三门峡市精捷自动化设备有限公司 | Low-volatile coal body thermal steaming and cold quenching process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5962696A (en) * | 1982-10-01 | 1984-04-10 | Hitachi Ltd | Improvement of coal |
| JPS6262892A (en) * | 1985-09-13 | 1987-03-19 | Hitachi Ltd | Modification of low-grade coal |
| WO2012147752A1 (en) * | 2011-04-28 | 2012-11-01 | 三菱重工業株式会社 | Fluidized bed drying apparatus and integrated coal gasification combined cycle system |
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| CN203700277U (en) * | 2014-01-22 | 2014-07-09 | 鞍山兴德工程技术有限公司 | Gas-flow ejecting dense-phase fast carbonization upgrading system for low-rank coal |
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2014
- 2014-07-23 JP JP2014150073A patent/JP6322509B2/en active Active
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5962696A (en) * | 1982-10-01 | 1984-04-10 | Hitachi Ltd | Improvement of coal |
| JPS6262892A (en) * | 1985-09-13 | 1987-03-19 | Hitachi Ltd | Modification of low-grade coal |
| WO2012147752A1 (en) * | 2011-04-28 | 2012-11-01 | 三菱重工業株式会社 | Fluidized bed drying apparatus and integrated coal gasification combined cycle system |
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| JP2016023280A (en) | 2016-02-08 |
| AU2015293497A1 (en) | 2017-02-16 |
| CN106661476B (en) | 2019-11-01 |
| JP6322509B2 (en) | 2018-05-09 |
| CN106661476A (en) | 2017-05-10 |
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