CN109563425A - The manufacturing method of ashless coal and the manufacturing device of ashless coal - Google Patents
The manufacturing method of ashless coal and the manufacturing device of ashless coal Download PDFInfo
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- CN109563425A CN109563425A CN201780049047.9A CN201780049047A CN109563425A CN 109563425 A CN109563425 A CN 109563425A CN 201780049047 A CN201780049047 A CN 201780049047A CN 109563425 A CN109563425 A CN 109563425A
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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
- C10L5/06—Methods of shaping, e.g. pelletizing or briquetting
-
- 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
-
- 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
-
- 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
Abstract
The manufacturing method of ashless coal of the invention has following process: the process of Mixture Density Networks and solvent；Make the process for the coal ingredient dissolution for dissolving in solvent in above-mentioned coal from via the resulting slurry of above-mentioned mixed processes；The coal ingredient obtained via above-mentioned dissolution process is dissolved in solution made of solvent, the process separated from above-mentioned slurry；Make the process of solvent evaporation from the above-mentioned solution separated via above-mentioned separation process, above-mentioned solution is separated in above-mentioned separation process and uses cyclone hydraulic separators.
Description
Technical field
The present invention relates to the manufacturing devices of the manufacturing method of ashless coal and ashless coal.
Background technique
Coal is widely used as the raw material of the fuel or chemicals of thermal power generation and boiler, as one of environmental cure,
It is strongly desired to develop the technology for expeditiously removing the ash content in coal.For example, multiple in the high efficiency using gas turbine combustion
It closes in electricity generation system, the fuel of the liquid fuel as substitution LNG etc. is attempted using except the ashless coal (HPC) to deash.Separately
Outside, the coking coal as the hard coke charcoal of blast furnace coke etc. is attempted to use ashless coal.
As the manufacturing method of ashless coal, proposition has using settling methods, and separation, which contains, from slurry dissolves in solvent
Coal ingredient (hereinafter also referred to as solvent soluble ingredient) solution method (such as Japanese Laid-Open 2005-120185 public affairs
Report).This method has following process: Mixture Density Networks and solvent and the slurry preparation section for preparing slurry；Heat slurry preparation section
In obtained slurry, the extraction process of extractant soluble ingredient.Furthermore in the method, it is also equipped with following process: from warp
The separation process of solution of the separation dissolved with solvent soluble ingredient in the slurry of solvent soluble ingredient is extracted by extraction process；
The ashless coal for separating solvent from the solution being separated via separation process and obtaining ashless coal obtains process.
In above-mentioned settling methods, using subsider, slurry is supplied to the subsider on one side, is discharged on one side from top
Solution containing solvent soluble ingredient, and the solid component concentrate containing solvent insoluble component is discharged from lower part, to carry out
Separation.In this settling methods, in order to inhibit being precipitated again for solvent soluble ingredient, and the slurry in subsider is heated in separation
Material.Therefore, upper up-flow occurs in the slurry in subsider.If the upflow velocity of this upper up-flow becomes larger, solid component concentrate
Sinking speed reduce, therefore separative efficiency reduce.
In order to reduce above-mentioned upflow velocity, the diameter (sectional area) of subsider is effectively increased.But it sinks if increasing
The diameter of slot drops, then manufacturing equipment becomes larger.Therefore, in the manufacturing method of above-mentioned existing ashless coal, the manufacture of ashless coal is set
Standby setting needs wide space.
[existing technical literature]
[patent document]
[patent document 1] Japanese Laid-Open 2005-120185 bulletin
Summary of the invention
It is done the present invention is based on above-mentioned such situation, it is intended that providing one kind can compare efficiently from slurry
The solution containing the coal ingredient for dissolving in solvent is separated to rate, and the ashless coal of the installation space of manufacturing equipment can be reduced
The manufacturing device of manufacturing method and ashless coal.
The invention done in order to solve the above problems is a kind of manufacturing method of ashless coal, has following process: mixing
The process of coal and solvent；From via the above-mentioned coal stated in the obtained slurry of mixed processes, make the coal ingredient for dissolving in solvent
The process of dissolution；There to be coal ingredient to be dissolved in solution made of solvent from above-mentioned slurry via above-mentioned dissolution process is obtained
Isolated process；With make from the above-mentioned solution isolated via above-mentioned separation process solvent evaporate process, at above-mentioned point
From in process, the separation of above-mentioned solution uses cyclone hydraulic separators.
In the manufacturing method of the ashless coal, via separation process from slurry separation containing dissolve in the coal of solvent at
The solution divided, uses cyclone hydraulic separators.Because cyclone hydraulic separators is separated with centrifugal force, sink with gravity is used
The case where drop, is compared, can the short time, above-mentioned solution is expeditiously separated from slurry.In addition, because cyclone hydraulic separators by
The flow velocity of slurry makes that centrifugal force occurs, so the flow velocity of the slurry in cyclone hydraulic separators is big.Therefore, the unit time passes through spinning liquid point
The amount of slurry from the unit area in device is more, therefore manufacturing equipment can be made more small-sized.Therefore, the manufacturing method of the ashless coal
Expeditiously solution of the separation containing the coal ingredient for dissolving in solvent from slurry can be compared in the manufacture of ashless coal, it can
Reduce the installation space of manufacturing equipment.
Above-mentioned mixed processes have following process: the process of heated solvent；Will via above-mentioned solvent heating process and
The above-mentioned solvent of heating transports the process into above-mentioned dissolution process；It is supplied in above-mentioned solvent conveying process into above-mentioned solvent
To the process of coal.The solvent supply coal being heated so into conveying, can make coal rapidly heat up, and can utilize solvent
Flowing coal and solvent are stirred.Thereby, it is possible to so that coal is easily soluble in solvent.In addition, using cyclone hydraulic separators, no
It is the process pressurization to separation process downstream, but the above-mentioned mixed processes pressurization in separation process upstream is carried out.Cause
This, is able to suppress the cost increase of the pressurization bring manufacturing equipment because of the process in separation process downstream, while can be improved nothing
The extraction yield of culm.
The pressure of fluid feed port as above-mentioned cyclone hydraulic separators, preferably 1.1MPa or more and 5.0MPa are hereinafter, make
For the pressure of the fluid flow outlet of above-mentioned cyclone hydraulic separators, preferably 1.0MPa or more and 4.9MPa or less.Make above-mentioned spinning liquid point
The pressure of fluid feed port and fluid flow outlet from device within the above range, can inhibit bring manufacturing equipment of pressurizeing on one side
Cost increase, on one side improve ashless coal extraction efficiency.
The pressure of the above-mentioned fluid feed port of the pressure ratio of the fluid flow outlet of above-mentioned cyclone hydraulic separators is low, as its pressure
Difference, preferably 0.1MPa or more and 1.0MPa or less.Make above-mentioned pressure difference within the above range, can inhibit to make pressure difference on one side
Centrifugal force required for generating improves the separative efficiency of separation process on one side.
It is preferably low as the average grain diameter for the solvent insoluble component for including in the above-mentioned solution separated in above-mentioned separation process
In 20 μm.In the separation using cyclone hydraulic separators, the big solvent insoluble component of average grain diameter is selectively removed.Therefore,
Make the average grain diameter of the solvent insoluble component for including in above-mentioned solution lower than the above-mentioned upper limit, can reduce that above-mentioned solution includes is molten
Agent insoluble component, the purity is high of obtained ashless coal.
Another invention done for solving the above subject is a kind of manufacturing device of ashless coal, has following part:
The mixing unit of Mixture Density Networks and solvent；Make to dissolve in from the above-mentioned coal in the slurry obtained via above-mentioned mixing unit the coal of solvent at
Divide the dissolution portion of dissolution；Separation has coal ingredient to be dissolved in solution made of solvent what above-mentioned dissolution portion obtained from above-mentioned slurry
Separation of solid and liquid portion；With from via above-mentioned separation of solid and liquid part from above-mentioned solution in make solvent evaporate solvent separation unit,
Above-mentioned separation of solid and liquid portion, as above-mentioned solution equipment for separating liquid from solid and there is cyclone hydraulic separators.
In the manufacturing device of the ashless coal, separation of solid and liquid portion has as the separator from the above-mentioned solution of pulp separation
There is cyclone hydraulic separators.Cyclone hydraulic separators compared with the case where using gravitational settling, can the short time and expeditiously from slurry
Above-mentioned solution is separated, and more small-sized.Therefore, the manufacturing device of the ashless coal, can be relatively more efficient in the manufacture of ashless coal
The solution containing the coal ingredient for dissolving in solvent is separated to rate from slurry, and can reduce installation space.
One kind of the modification coal modified to coal here, so-called ashless coal (Hyper Coal, HPC), be using
Solvent eliminates the modification coal of ash content and non-solubility ingredient as far as possible from coal.But in the stream for not damaging ashless coal significantly
In the range of dynamic property and dilatancy, ashless coal can also contain ash content.In general, 7 mass % or more and 20 matter are contained in coal
% ash content below is measured, but according to circumstances, 5% mass or so can also be contained then containing 2 mass % or so in ashless coal
Ash content.In addition, so-called " ash content ", is the value according to JIS-M8812:2004 measurement.
In addition, so-called " average grain diameter ", refers to bent by the cumulative particle size distribution of the volume reference of the measurements such as laser diffractometry
50% value (50% partial size, D50) of line.
As described above, the manufacturing method and manufacturing device of ashless coal of the invention, can compare high efficiency from slurry
Solution of the ground separation containing the coal ingredient for dissolving in solvent, and the installation space of manufacturing equipment can be reduced.
Detailed description of the invention
Fig. 1 is the skeleton diagram for indicating the manufacturing device of ashless coal of first embodiment of the invention.
Fig. 2 is the schematical sectional view for indicating the composition in separation of solid and liquid portion of Fig. 1.
Specific embodiment
Hereinafter, the embodiment of manufacturing device and manufacturing method for ashless coal of the invention is described in detail.
(manufacturing device of ashless coal)
The manufacturing device of the ashless coal of Fig. 1 mainly has mixing unit 1, dissolution portion 2, separation of solid and liquid portion 3, the separation of the first solvent
Portion 4 and the second solvent separation unit 5.
< mixing unit >
Mixing unit 1 has solvent tank 11, pump 12, preheater 13 and coal feeder 14.In addition, mixing unit 1 has to dissolution
Portion 2 transports the conveying pipe 15 of the solvent of solvent tank 11.
(solvent tank)
Solvent tank 11 stores the solvent mixed with coal.
As long as above-mentioned solvent dissolution coal, it is not particularly limited, such as can be suitable for using the Bicyclic from coal
Compounds of group.The dinuclear aromatics is since basic structure is similar with coal texture molecule, so the compatibility with coal
Height can obtain relatively high extraction yield.As the dinuclear aromatics from coal, such as destructive distillation coal can be enumerated and made
When making coke, methylnaphthalene oil, naphtalene oil of the distilled oil as residual oil etc..
The boiling point of above-mentioned solvent is not particularly limited, such as the lower limit of the boiling point as above-mentioned solvent, and preferably 180 DEG C,
More preferably 230 DEG C.On the other hand, the upper limit as the boiling point of above-mentioned solvent, preferably 300 DEG C, more preferably 280 DEG C.If
The boiling point of above-mentioned solvent is lower than above-mentioned lower limit, then solvent is readily volatilized, therefore the preparation of the mixing ratio of the coal and solvent in slurry
It may be difficult with maintenance.Conversely, the separation of solvent soluble ingredient and solvent is tired if the boiling point of above-mentioned solvent is higher than the above-mentioned upper limit
Difficulty, therefore the rate of recovery of solvent is likely to decrease.
(pump)
Pump 12 is disposed in conveying pipe 15, and the solvent of solvent tank 11 is transported to dissolution portion 2.
The type of said pump 12, as long as dissolution portion 2 can be sent to above-mentioned solvent via conveying pipe 15, without special
It limits, such as is able to use positive displacement pump or on-positive displacement pump.More specifically, as positive displacement pump, it is able to use diaphragm pump
With tubular type diaphragm pump etc., is pumped as on-positive displacement, be able to use centrifugal pump etc..
As the lower limit of the pressure (internal pressure of conveying pipe 15) when above-mentioned solvent to be sent to dissolution portion 2 by pump 12,
Preferably 1.1MPa, more preferably 1.5MPa.On the other hand, the upper limit as the internal pressure of above-mentioned conveying pipe 15, preferably
5MPa, more preferably 4MPa.If the internal pressure of above-mentioned conveying pipe 15 is lower than above-mentioned lower limit, the aftermentioned solvent into conveying
When supplying coal, the power of stirring solvent coal dies down, therefore the dissolution of coal may be insufficient.Conversely, if above-mentioned conveying pipe 15 it is interior
Portion's pressure is higher than the above-mentioned upper limit, then in order to ensure pressure resistance required for mixing unit 1, the cost increase of manufacturing equipment, in contrast,
So the improvement effect of obtained coal dissolution may be insufficient.
In addition, can also be transported in laminar condition by the above-mentioned solvent of 12 conveying of pump, but it is with turbulent condition conveying
It can.Solvent is so transported with turbulent condition, when supplying coal to solvent in conveying, the power of stirring solvent coal is improved, therefore coal is easy
It is mixed with solvent, and the dissolution of coal is promoted.Here, so-called " laminar condition ", refers to the shape that reynolds number Re is lower than 2100
State, it is so-called " turbulent condition ", refer to that reynolds number Re is 2100 or more, more preferably state of the reynolds number Re 4000 or more.
The lower limit of flow velocity as the above-mentioned solvent by 12 conveying of pump, preferably 0.5m/ seconds, is more selected as 1m/ seconds.Another party
Face, the upper limit of the flow velocity as above-mentioned solvent are selected as 10m/ seconds, are more selected as 5m/ seconds.If the flow velocity of above-mentioned solvent is lower than under above-mentioned
Limit, then conveying in solvent supply coal supply when, the power of stirring solvent coal dies down, therefore the dissolution of coal may be insufficient.
Conversely, if the flow velocity of above-mentioned solvent is higher than the above-mentioned upper limit, for making the cost increase of 12 strengths of pump, in contrast, acquired
Coal dissolution improvement effect may be insufficient.
(preheater)
Preheater 13 is disposed on the conveying pipe 15 in 12 downstream sides of pump, the solvent that heating is transported by pump 12.
As long as preheater 13 can heat the solvent passed through in preheater 13, just it is not particularly limited, such as electricity can be enumerated
Hinder heating type heating and load coil.Alternatively, it is also possible to use thermophore to be heated.Such as preheating can passed through
Heating tube is configured around the flow path of the solvent of device 13, to the thermophore of heating tube supply steam, oil etc., so that heating is pre-
The solvent passed through in hot device 13.
The lower limit of temperature as the solvent after the heating of preheated device 13, preferably 300 DEG C, more preferably 350 DEG C.It is another
Aspect, the upper limit of the temperature as above-mentioned solvent are not particularly limited out if it is leachable temperature, but preferably 480
DEG C, more preferably 450 DEG C.If the temperature of above-mentioned solvent is lower than above-mentioned lower limit, it cannot sufficiently weaken in dissolution portion 2 and constitute coal
Intermolecular key, dissolution rate are likely to decrease.Conversely, if the temperature of above-mentioned solvent is higher than the above-mentioned upper limit, for maintaining solvent
The heat of temperature unnecessarily become larger, therefore manufacturing cost is possible to increase.
The lower limit of heating speed as preheater 13, preferably 10 DEG C/min, more preferably 20 DEG C/min.Another party
Face, as the upper limit of above-mentioned heating speed, preferably 100 DEG C/min, more preferably 50 DEG C/min.If above-mentioned heating speed is low
In above-mentioned lower limit, then solvent is heated to predetermined temperature and spends the time, therefore the manufacture efficiency of ashless coal is likely to decrease.Instead
It, if above-mentioned heating speed is higher than the above-mentioned upper limit, the cost of energy for heating and manufacturing equipment etc. is possible to unnecessary
Ground increases.
It as the heating time of preheater 13, is not particularly limited, but for the relationship of above-mentioned temperature and heating speed
Consider, such as can be 10 minutes or more and 30 minutes or less.
< coal feeder >
Coal feeder 14 supplies coal to conveying pipe 15.As coal feeder 14, it is able to use and is used under normal pressure state
Normal pressure hopper, the well known coal scuttle of the pressurization hopper etc. used under normal pressure state and pressurized state.
As the coal supplied from coal feeder 14, it is able to use the coal of various qualities.It such as is suitable for extraction using ashless coal
Take the bituminous coal that rate is high, and more cheap colm (ub-bituminous coal and lignite).In addition, being suitable for if classifying by granularity to coal
Use the coal of tiny crushing.Here so-called " coal of tiny crushing ", means that the quality for example relative to coal totality, granularity are lower than
The coal that the mass ratio of the coal of 1mm is 80% or more.In addition, being also able to use lump coal as the coal supplied from coal feeder 14.
So-called herein " lump coal " means that the quality for example relative to coal totality, granularity are 50% in the mass ratio of the coal of 5mm or more
Above coal.The coal facies ratio of lump coal and tiny crushing, the granularity of coal is larger, therefore can make point in aftermentioned separation of solid and liquid portion 3
From efficient activity.Here, so-called " granularity (partial size) ", refers to what the sieve test according to JIS-Z8815 (1994) routinely measured
Value.In addition, in the classification of the granularity progress by coal, such as it is able to use the metal of JIS-Z8801-1 (2006) defined
Mesh screen processed.
In addition, from the viewpoint of shortening dissolution time is such, it is as the coal supplied from coal feeder 14, it is preferable to use big
Measure the coal containing colm.The lower limit of ratio as the colm in the coal totality of supply, preferably 80 mass %, more preferably
For 90 mass %.If the ratio for the colm for including in the coal of supply dissolves out solvent soluble ingredient lower than above-mentioned lower limit
Time is possible to elongated.
The lower limit of carbon content rate as above-mentioned colm, preferably 70 mass %.On the other hand, as above-mentioned colm
The upper limit of carbon content rate, preferably 85 mass %, more preferably 82 mass %.If the carbon containing ratio of above-mentioned colm is lower than under above-mentioned
Limit, then the dissolution rate of solvent soluble ingredient is likely to decrease.Conversely, if the carbon containing ratio of above-mentioned colm is higher than the above-mentioned upper limit,
The cost of the coal then supplied is possible to get higher.
Above-mentioned coal preheats in advance.By preheating above-mentioned coal in advance, supplied to conveying pipe 15, when being mixed with solvent, energy
Enough preventing the temperature of slurry reduces.As the preheating temperature of above-mentioned coal, be not particularly limited, for example, can for 200 DEG C or more and
300 DEG C or less.
In addition, as from coal feeder 14 to conveying pipe 15 supply coal, mixed solvent also can be used and it is slurried after
Coal.It is supplied to conveying pipe 15 by the coal after will be slurried from coal feeder 14, in conveying pipe 15, coal and solvent are easy to mix
It closes, quickly coal can be made to dissolve.
The lower limit of the coal concentration in terms of anhydrous coal benchmark in above-mentioned coal slurry, preferably 20 mass %, more preferably 30
Quality %.On the other hand, the upper limit as above-mentioned coal concentration, preferably 70 mass %, more preferably 60 mass %.If above-mentioned coal
Concentration is lower than above-mentioned lower limit, then the amount of dissolution for the solvent soluble ingredient being dissolved in aftermentioned dissolution portion 2 is relative to slurry processing
Quantitative change is few, therefore the manufacture efficiency of ashless coal is likely to decrease.Conversely, if above-mentioned coal concentration is higher than the above-mentioned upper limit, it is slurried
The easy hybridization effect of coal and solvent afterwards is possible to become inadequate.
(conveying pipe)
Conveying pipe 15 transports the solvent of solvent tank 11 to dissolution portion 2.In addition, being supplied to conveying pipe 15 from coal feeder 14
Coal, mix in the conveying pipe 15 with the solvent after the heating flowed in conveying pipe 15, rapidly heated up.Here, so-called " anxious
Speed heating ", such as refer to and be heated with 10 DEG C/sec or more and 1000 DEG C/sec or less Zuo You of heating speed.As a result, making
For the temperature of solvent and the slurry of the mixture of coal, in the several seconds to reaching relatively uniform temperature between ten several seconds.In addition, above-mentioned
The temperature of slurry is compared to the temperature of the solvent after heating, and only the sensible heat amount of low coal is so more, and for example, 350 DEG C or more and 420 DEG C
Left and right below.
As the lower limit of the coal concentration in terms of anhydrous coal benchmark in above-mentioned slurry, preferably 5 mass %, more preferably 10
Quality %.On the other hand, the upper limit as above-mentioned coal concentration, preferably 40 mass %, more preferably 30 mass %.If above-mentioned coal
Concentration is lower than above-mentioned lower limit, then the amount of dissolution of the solvent soluble ingredient gone out in aftermentioned dissolution portion 2 is relative to slurry treating capacity
It tails off, therefore the manufacture efficiency of ashless coal is likely to decrease.Conversely, if above-mentioned coal concentration is higher than the above-mentioned upper limit, in solvent on
Solvent soluble ingredient saturation is stated, therefore the dissolution rate of above-mentioned solvent soluble ingredient is likely to decrease.
< dissolution portion >
In dissolution portion 2, keep the coal ingredient for dissolving in solvent molten in the above-mentioned coal from the slurry that above-mentioned mixing unit 1 obtains
Out.Above-mentioned dissolution portion 2 has extraction tank 21.
Via above-mentioned conveying pipe 15, slurry is fed into extraction tank 21.In above-mentioned extraction tank 21, the slurry is kept on one side
Temperature, the coal ingredient for dissolving in solvent is dissolved from coal on one side.In addition, above-mentioned extraction tank 21 has blender 21a.It utilizes
Blender 21a is stirred slurry, can promote above-mentioned dissolution.
The lower limit of internal pressure as above-mentioned extraction tank 21, preferably 1.1MPa, more preferably 1.5MPa.Another party
Face, the upper limit of the internal pressure as above-mentioned extraction tank 21, preferably 5MPa, more preferably 4MPa.If above-mentioned extraction tank 21
Internal pressure is lower than above-mentioned lower limit, then solvent is evaporated and reduced, and the dissolution of coal may be insufficient.Conversely, if above-mentioned extraction tank
21 internal pressure is higher than the above-mentioned upper limit, then for maintaining the cost increase of pressure, in contrast, the dissolution of obtained coal mentions
High effect has been possible to insufficient.
In addition, be not particularly limited as the dissolution time in dissolution portion 2, but from the extraction quantity of solvent soluble ingredient and
It can be 10 minutes or more and 70 minutes or less from the perspective of extraction efficiency.
Slurry after the dissolution of the soluble coal ingredient in dissolution portion 2 is sent to separation of solid and liquid portion 3 via supply pipe 22.
< separation of solid and liquid portion >
In separation of solid and liquid portion 3, by solution and solvent obtained in above-mentioned dissolution portion 2, being dissolved in containing coal ingredient solvent
The solid component concentrate of insoluble component is separated from above-mentioned slurry.In addition, so-called solvent insoluble component, mainly by insoluble in extraction
The ash content and insoluble coal for taking solvent are constituted, and refer to extraction surplus also comprising extraction solvent.
As shown in Fig. 2, above-mentioned separation of solid and liquid portion 3 has cyclone hydraulic separators 31, and cover the cyclone hydraulic separators 31 and inside
The shell 32 of high pressure can be reached.
(cyclone hydraulic separators)
Cyclone hydraulic separators 31, as above-mentioned solution equipment for separating liquid from solid and use.The such as Fig. 2 of cyclone hydraulic separators 31 institute
Show in this way, by cylindric main part 31a and the circular cone that is connected in such a way that vertex is outstanding in the lower section of main part 31a
The separation unit 31b of shape is constituted.
Above-mentioned cyclone hydraulic separators 31 has fluid feed port 31c in the side of aforementioned body portion 31a.In addition, above-mentioned spinning liquid
Conical tip of the separator 31 in the upper surface of aforementioned body portion 31a and the lower section of separation unit 31b is respectively provided with fluid flow outlet
31d.The external supply pipe imported and slurry is supplied from dissolution portion 2 from shell 32 is connected in above-mentioned fluid feed port 31c
22.In addition, fluid flow outlet 31d above is connected with the external export to shell 32 and with the first solvent separation unit 4 for confession
To the supply pipe 33 at end.In addition, the fluid flow outlet 31d in lower section is connected with the external export to shell 32 and molten with second
Agent separation unit 5 is the supply pipe 34 of supply side.
The size of cyclone hydraulic separators 31, according to the treating capacity of slurry be suitable for selection, such as main part 31a diameter be 1m with
Upper and 2m is hereinafter, total height of main part 31a and separation unit 31b is 1m or more and the left and right 3m or less.In addition, the processing of slurry
When measuring more, multiple cyclone hydraulic separators 31 can also be used side by side.
Cyclone hydraulic separators 31 does not possess mechanical driving portion, is supplied using the slave fluid of the side in main part 31a
The vortex for the slurry that mouth 31c is imported makes centrifugal force, to be separated by solid-liquid separation.Specifically, cyclone hydraulic separators 31 can be with
As under type is separated by solid-liquid separation by centrifugal force.It is flowed into the slurry of the fluid feed port 31c of cyclone hydraulic separators 31 and includes
Particle, the speed of the slurry based on inflow, under the action of the centrifugal force, it is big more being directed towards the side partial size of separation unit 31b more
Heavy, medium particle diameter is smaller lighter more being directed towards, and so arranges in the inside of separation unit 31b in satellite shape.Separation unit 31b's
Near side, sinking occurs along the side, and takes the stream, and the big particle of partial size is mainly directed into the fluid stream of lower section
It exports 31d and is discharged.On the other hand, in central part, otherwise it is upper up-flow, and takes the stream, solvent-laden partial size is small
The fluid flow outlet 31d that particle mainly arrives top is discharged.Therefore, above-mentioned cyclone hydraulic separators 31 can be such that slurry supplies from fluid
Mouthful 31c is flowed into, and above-mentioned solution is discharged from the fluid flow outlet 31d of top, makes above-mentioned solid component concentrate from below
Fluid flow outlet 31d discharge.
The average grain diameter of solvent insoluble component contained in the above-mentioned solution being discharged from the fluid flow outlet 31d of top, it is excellent
Choosing is lower than 20 μm, more preferably less than 15 μm.If the average grain diameter for the solvent insoluble component for including in above-mentioned solution is in the above-mentioned upper limit
More than, then solvent insoluble component contained by solution is unable to fully reduce, and the purity of obtained ashless coal is likely to decrease.It is another
Aspect, the lower limit of the average grain diameter as the solvent insoluble component for including in above-mentioned solution, is not particularly limited, and usually 10 μm
Left and right.It is insoluble for separating solvent if the average grain diameter for the solvent insoluble component for including in above-mentioned solution is lower than above-mentioned lower limit
The cost of ingredient is possible to rise.It, can be by adjusting in addition, the average grain diameter for the solvent insoluble component for including in above-mentioned solution
The size of the centrifugal force of cyclone hydraulic separators 31, that is, slurry inflow flow velocity and controlled.
The lower limit of the pressure of fluid feed port 31c as above-mentioned cyclone hydraulic separators 31, preferably 1.1MPa, more preferably
1.8MPa.As the upper limit of pressure of above-mentioned fluid feed port 31c, preferably 5MPa, more preferably 3MPa.If above-mentioned fluid supplies
It is lower than above-mentioned lower limit to the pressure of mouth 31c, then can't improve enough the pressure of mixing unit 1 and dissolution portion 2, the extraction effect of ashless coal
Rate is likely to decrease.Conversely, making pressure rise and cause to extract if the pressure of above-mentioned fluid feed port 31c is higher than the above-mentioned upper limit
The improvement effect of efficiency is taken to be saturated, for the rising of the cost of manufacturing device, obtained effect is possible to become smaller.
The lower limit of pressure as the fluid flow outlet 31d above and below above-mentioned cyclone hydraulic separators 31, preferably
1.0MPa, more preferably 1.2MPa.On the other hand, the upper limit of pressure as above-mentioned fluid flow outlet 31d, preferably
4.9MPa, more preferably 3MPa, further preferably 1.4MPa.If the pressure of above-mentioned fluid flow outlet 31d is lower than above-mentioned lower limit,
Then a side of the vapour pressure of solvent is smaller than the pressure of above-mentioned fluid flow outlet 31d, and solvent is easy gasification.Accordingly, it is difficult to by above-mentioned
Solution maintains liquid condition, is possible to difficult by the separation of solid and liquid that cyclone hydraulic separators 31 carries out.Conversely, if above-mentioned fluid flows out
The pressure of mouth 31d is higher than the above-mentioned upper limit, then needs to improve what the first solvent separation unit 4 in 3 downstream of separation of solid and liquid portion waited
Pressure resistance, therefore the cost of manufacturing equipment is possible to rise.
The pressure of the fluid flow outlet 31d of above-mentioned cyclone hydraulic separators 31, it is preferably lower than the pressure of fluid feed port 31c, make
The lower limit of pressure difference, preferably 0.1MPa, more preferably 0.4MPa thus.On the other hand, the upper limit as above-mentioned pressure difference, it is excellent
It is selected as 1MPa, more preferably 0.8MPa.If above-mentioned pressure difference be lower than above-mentioned lower limit, the above-mentioned solution in separation of solid and liquid portion 3 with it is upper
The separative efficiency for stating solid component concentrate is likely to decrease.Conversely, if above-mentioned pressure difference is higher than the above-mentioned upper limit, for making to press
Centrifugal force required for power difference generates becomes excessive, and the cost of the manufacturing equipment in separation of solid and liquid portion 3 is possible to rise.
The lower limit of flow velocity as the slurry for being flowed into above-mentioned cyclone hydraulic separators 31, preferably 3m/ seconds, more preferably 5m/
Second.On the other hand, the upper limit as the flow velocity of above-mentioned slurry, preferably 15m/ seconds, more preferably 10m/ seconds.If above-mentioned slurry
Flow velocity is lower than above-mentioned lower limit, then centrifugal force is insufficient, it may not be possible to sufficiently remove solvent insoluble component.Conversely, if above-mentioned slurry
Flow velocity is higher than the above-mentioned upper limit, the then rising relative to the cost of manufacturing device, and obtained separating effect is possible to be unable to fully
It improves.
(shell)
Shell 32 is used to make cyclone hydraulic separators 31 work in high pressure, such as can be the made of metal of stainless steel etc..In addition, outer
The pressure of the inside of shell 32 is suitable for setting according to the operating condition of cyclone hydraulic separators 31, such as can be with cyclone hydraulic separators 31
The pressure of fluid feed port 31c is equivalent.
< the first solvent separation unit >
First solvent separation unit 4 evaporates solvent from the above-mentioned solution separated via above-mentioned separation of solid and liquid portion 3.By this
The evaporation of solvent is isolated ashless coal (HPC).
The obtained ashless coal, ash content is 5 mass % hereinafter, preferably 3 mass % are hereinafter, be practically free of ash content, complete
There is no moisture entirely, in addition, for example showing the thermal discharge higher than feed coal.In addition, raw material of the ashless coal as hard coke charcoal
Especially important quality, i.e. softening meltbility is greatly improved, such as shows mobility much more excellent than feed coal.Cause
This, ashless coal can be used as the mixed coal of coke raw material.
As making solvent evaporate isolated method, it is able to use including the general way of distillation and evaporation (spray drying process
Deng) including separation method.By the solvent separated from above-mentioned solution, can obtain being substantially free of ash content from above-mentioned solution
Ashless coal.
< the second solvent separation unit >
In second solvent separation unit 5, steam solvent from the above-mentioned solid component concentrate separated via separation of solid and liquid portion 3
Hair is isolated extract residue (RC).
Extract residue does not show softening meltbility, but is detached from containing oxygen functional group.Therefore, extract residue is as mixed coal in use, not
It can hinder the softening meltbility of others coal included in the mixed coal.Therefore the mixed coal can be used as the mixed coal of coke raw material
A part use.In addition, mixed coal can not also be recycled and be discarded.
It is same as the separation method of the first solvent separation unit 4 as the method for separating solvent from solid component concentrate,
It is able to use the general way of distillation and evaporation (spray drying process etc.).By the separation and recycling of solvent, can by solid at
Concentrate is divided to obtain the extract residue after the solvent insoluble component containing ash content etc. is concentrated.
(manufacturing method of ashless coal)
The manufacturing method of the ashless coal has mixed processes, dissolution process, separation process, the first evaporization process and second
Evaporization process.The manufacturing method of the ashless coal, the manufacturing device for being able to use the ashless coal of Fig. 1 carry out.
< mixed processes >
In mixed processes, Mixture Density Networks and solvent.In above-mentioned mixed processes, have solvent heating process, solvent conveying process
With coal supply step.
(solvent heating process)
The heated solvent in solvent heating process.Specifically, the solvent being stored in solvent tank 11 is flowed via pump 12
Conveying pipe 15 is moved, the solvent flowed in the conveying pipe 15 is heated during through preheater 13.
(solvent conveying process)
In solvent conveying process, the above-mentioned solvent heated via above-mentioned solvent heating process is transported to above-mentioned dissolution work
Sequence.Specifically, by transporting pipe 15, solvent is fed into dissolution portion 2.
(coal supply step)
In coal supply step, coal is supplied to above-mentioned solvent in above-mentioned solvent conveying process.Specifically, it is supplied from coal
Device 14 supplies coal, Mixture Density Networks and solvent to the conveying pipe 15 of the solvent flow after above-mentioned heating and becomes slurry.It is supplied to conveying
The coal of pipe 15 is rapidly heated up by solvent, in addition, in the stirring solvent coal that conveying pipe 15 flows, therefore coal is easy dissolution, obtains molten
Agent and the well-mixed slurry of coal.
< dissolves out process >
In dissolution process, make the coal for dissolving in solvent from the above-mentioned coal in the slurry obtained via above-mentioned mixed processes
Ingredient dissolution.Specifically, the slurry prepared via mixed processes is supplied to extraction tank 21, is stirred on one side by blender 21a,
It is extracted on one side with predetermined temperature holding.
< separation process >
In separation process, the coal ingredient obtained via above-mentioned dissolution process is dissolved in solution made of solvent, from upper
It states in slurry and separates.Specifically, the slurry being discharged from extraction tank 21 is supplied, and by cyclone hydraulic separators in separation of solid and liquid portion 3
31 pulp separations supplied are at above-mentioned solution and solid component concentrate.
The first evaporization process of < >
In the first evaporization process, evaporate solvent from the above-mentioned solution separated in above-mentioned separation process.Specifically,
It will be supplied to the first solvent separation unit 4 via the isolated solution in separation of solid and liquid portion 3, evaporates solvent in the first solvent separation unit 4.
Above-mentioned solution is separated into solvent and ashless coal as a result,.
The second evaporization process of < >
In the second evaporization process, steam solvent from the above-mentioned solid component concentrate separated in above-mentioned separation process
Hair.Specifically, the separated solid component concentrate in separation of solid and liquid portion 3 is supplied to the second solvent separation unit 5, and second
Solvent separation unit 5 makes solvent evaporate and be separated into solvent and extract residue
(advantage)
About the manufacturing method of the ashless coal, containing the coal ingredient for dissolving in solvent from pulp separation by separation process
Cyclone hydraulic separators 31 is used in solution.In addition, separation of solid and liquid portion 3 is as from pulp separation in the manufacturing device of the ashless coal
It states the separator of solution and there is cyclone hydraulic separators 31.Because cyclone hydraulic separators 31 is separated using centrifugal force, with
Compared using the case where gravitational settling, can the short time and above-mentioned solution is expeditiously separated from slurry.In addition, because spinning liquid
Separator 31 makes centrifugal force using the flow velocity of slurry, so the flow velocity of the slurry in cyclone hydraulic separators 31 is big.Therefore, unit
Time is more by the amount of the slurry of the unit area in cyclone hydraulic separators 31, so manufacturing equipment can be made more small-sized.Therefore,
The manufacturing method of the ashless coal and the manufacturing device of the ashless coal can compare efficient in the manufacture of ashless coal from slurry
The solution containing the coal ingredient for dissolving in solvent is separated to rate, and installation space can be reduced.
[other embodiments]
In addition, the manufacturing device of ashless coal of the invention and the manufacturing method of ashless coal, are not limited by above embodiment.
In the above-described embodiment, it illustrates as mixing unit and the case where the downstream side of pump is arranged by preheater, but
Pumping the arranging sequence with preheater may be reversed.
In addition, in the above-described embodiment, the structure of display is, as mixing unit, coal is supplied simultaneously in the solvent of Xiang Jiare
It is mixed in conveying pipe, but mixing unit is also possible to other structures.As the structure of other mixing unit, such as can arrange
The structure of act is that mixing unit has preparation vessel, and the coal supplied by coal feeder and the solvent supplied from solvent tank are in this preparation vessel
In mixed.It is heated by the slurry being mixed to get by preheater, is sent to dissolution portion.
In addition, in the above-described embodiment, as the manufacturing method of ashless coal, illustrating the feelings for having the second evaporization process
Condition, still, such as when not utilizing extract residue, this second evaporization process can be omitted.When without the second evaporization process, ashless coal
Manufacturing device may not possess the second solvent separation unit.
In the above-described embodiment, illustrate to only use cyclone hydraulic separators in separation of solid and liquid portion separate solution and solid at
The case where dividing concentrate, but gravitation settler can also be set in the downstream side of cyclone hydraulic separators.Gravitation settler is arranged such,
Remaining solvent insoluble component in the solution through cyclone hydraulic separators separation can further be removed.In addition, in cyclone hydraulic separators
Downstream side be arranged gravitation settler when, it should the amount of slurry handled through cyclone hydraulic separators can also be reduced, thus with do not use
The case where cyclone hydraulic separators, is compared, and the size of gravitation settler can be reduced.Therefore, the installation space of manufacturing equipment can drop
It is low.
In detail and the present invention is illustrated referring to specific embodiment, but do not depart from the spirit and scope of the present invention to add
With various changes and modifications, this will be apparent that for a person skilled in the art.
The application is based on Japanese patent application (Patent 2016-156005) filed on August 8th, 2016, and content is herein
It is incorporated into as reference.
[industrial availability]
As described above, the manufacturing method and manufacturing device of ashless coal of the invention can dissolve in solvent for containing
The solution of coal ingredient compares the installation space for separating in expeditiously slurry, and capable of reducing manufacturing equipment.
[explanation of symbol]
1 mixing unit
11 solvent tanks
12 pumps
13 preheaters
14 coal feeders
15 conveying pipes
2 dissolution portions
21 extraction tanks
21a blender
22 supply pipes
3 separation of solid and liquid portions
31 cyclone hydraulic separators
31a main part
31b separation unit
31c fluid feed port
31d fluid flow outlet
32 shells
33,34 supply pipe
4 first solvent separation units
5 second solvent separation units
Claims (6)
1. a kind of manufacturing method of ashless coal, has following process:
The process of Mixture Density Networks and solvent；
Make the process for the coal ingredient dissolution for dissolving in solvent in above-mentioned coal from via the obtained slurry of above-mentioned mixed processes；
The work that solution made of solvent is separated from above-mentioned slurry will be dissolved in via the obtained coal ingredient of above-mentioned dissolution process
Sequence；With
The process for evaporating solvent from the above-mentioned solution separated via above-mentioned separation process,
Above-mentioned solution is separated in above-mentioned separation process uses cyclone hydraulic separators.
2. the manufacturing method of ashless coal according to claim 1, wherein
Above-mentioned mixed processes have:
The process of heated solvent；
The above-mentioned solvent heated via above-mentioned solvent heating process is transported to the process into above-mentioned dissolution process；With
The process of coal is supplied into above-mentioned solvent in above-mentioned solvent conveying process.
3. according to claim 1 or the manufacturing method of ashless coal as claimed in claim 2, wherein
The pressure of the fluid feed port of above-mentioned cyclone hydraulic separators be 1.1MPa or more and 5.0MPa hereinafter,
The pressure of the fluid flow outlet of above-mentioned cyclone hydraulic separators is 1.0MPa or more and 4.9MPa or less.
4. the manufacturing method of ashless coal according to claim 1, wherein
The pressure of the pressure ratio fluid feed port of the fluid flow outlet of above-mentioned cyclone hydraulic separators is low, and pressure difference is 0.1MPa or more
And 1.0MPa or less.
5. the manufacturing method of ashless coal according to claim 1, wherein
The average grain diameter of solvent insoluble component contained in the above-mentioned solution separated as above-mentioned separation process is lower than 20 μm.
6. a kind of manufacturing device of ashless coal, has as follows:
The mixing unit of Mixture Density Networks and solvent；
From the dissolution portion for the coal ingredient dissolution for obtaining making to dissolve in solvent in the above-mentioned coal in slurry via above-mentioned mixing unit；
The obtained coal ingredient in above-mentioned dissolution portion is dissolved in the separation of solid and liquid that solution made of solvent is separated from above-mentioned slurry
Portion；With
From via above-mentioned separation of solid and liquid part from above-mentioned solution in make solvent evaporate solvent separation unit,
In above-mentioned separation of solid and liquid portion, as above-mentioned solution equipment for separating liquid from solid and have cyclone hydraulic separators.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2016156005A JP2018024732A (en) | 2016-08-08 | 2016-08-08 | Production method of ashless coal and production apparatus for ashless coal |
| JP2016-156005 | 2016-08-08 | ||
| PCT/JP2017/027178 WO2018030161A1 (en) | 2016-08-08 | 2017-07-27 | Method for producing ash-free coal and apparatus for producing ash-free coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109563425A true CN109563425A (en) | 2019-04-02 |
Family
ID=61162944
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780049047.9A Pending CN109563425A (en) | 2016-08-08 | 2017-07-27 | The manufacturing method of ashless coal and the manufacturing device of ashless coal |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP2018024732A (en) |
| KR (1) | KR20190026007A (en) |
| CN (1) | CN109563425A (en) |
| WO (1) | WO2018030161A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114621799A (en) * | 2020-12-10 | 2022-06-14 | 株式会社神户制钢所 | Method for producing ashless coal |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2021155771A (en) * | 2020-03-25 | 2021-10-07 | 住友金属鉱山株式会社 | Treatment method for ore slurry, and hydrometallurgical method for nickel oxide ore |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52132001A (en) * | 1976-04-30 | 1977-11-05 | Nippon Kokan Kk <Nkk> | Reformation of coal |
| JPS5927984A (en) * | 1982-08-06 | 1984-02-14 | Mitsubishi Heavy Ind Ltd | Liquefaction of coal |
| JPS61247791A (en) * | 1985-04-22 | 1986-11-05 | エイチアールアイ・インコーポレーテツド | Catalytic two-stage coal hydrogenating and hydroforming method |
| CN102304405A (en) * | 2011-08-01 | 2012-01-04 | 山东科技大学 | Lignite upgrading device and method |
| CN105051169A (en) * | 2013-03-28 | 2015-11-11 | 株式会社神户制钢所 | Ashless-coal production device, and ashless-coal production method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4045229B2 (en) | 2003-10-15 | 2008-02-13 | 株式会社神戸製鋼所 | Production method of ashless coal |
-
2016
- 2016-08-08 JP JP2016156005A patent/JP2018024732A/en active Pending
-
2017
- 2017-07-27 CN CN201780049047.9A patent/CN109563425A/en active Pending
- 2017-07-27 WO PCT/JP2017/027178 patent/WO2018030161A1/en active Application Filing
- 2017-07-27 KR KR1020197003662A patent/KR20190026007A/en not_active Application Discontinuation
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52132001A (en) * | 1976-04-30 | 1977-11-05 | Nippon Kokan Kk <Nkk> | Reformation of coal |
| JPS5927984A (en) * | 1982-08-06 | 1984-02-14 | Mitsubishi Heavy Ind Ltd | Liquefaction of coal |
| JPS61247791A (en) * | 1985-04-22 | 1986-11-05 | エイチアールアイ・インコーポレーテツド | Catalytic two-stage coal hydrogenating and hydroforming method |
| CN102304405A (en) * | 2011-08-01 | 2012-01-04 | 山东科技大学 | Lignite upgrading device and method |
| CN105051169A (en) * | 2013-03-28 | 2015-11-11 | 株式会社神户制钢所 | Ashless-coal production device, and ashless-coal production method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114621799A (en) * | 2020-12-10 | 2022-06-14 | 株式会社神户制钢所 | Method for producing ashless coal |
| CN114621799B (en) * | 2020-12-10 | 2024-02-09 | 株式会社神户制钢所 | Method for producing ashless coal |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2018024732A (en) | 2018-02-15 |
| WO2018030161A1 (en) | 2018-02-15 |
| KR20190026007A (en) | 2019-03-12 |
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