CN105793399B - The manufacturing method of ashless coal - Google Patents
The manufacturing method of ashless coal Download PDFInfo
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- CN105793399B CN105793399B CN201480066265.XA CN201480066265A CN105793399B CN 105793399 B CN105793399 B CN 105793399B CN 201480066265 A CN201480066265 A CN 201480066265A CN 105793399 B CN105793399 B CN 105793399B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L5/00—Solid fuels
- C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
- C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2230/00—Function and purpose of a components of a fuel or the composition as a whole
- C10L2230/22—Function and purpose of a components of a fuel or the composition as a whole for improving fuel economy or fuel efficiency
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/08—Drying or removing water
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/22—Impregnation or immersion of a fuel component or a fuel as a whole
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/24—Mixing, stirring of fuel components
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/544—Extraction for separating fractions, components or impurities during preparation or upgrading of a fuel
Abstract
The manufacturing method of ashless coal has slurry modulating process, which mixes coal and solvent and modulate slurry, and carries out the dehydration of coal contained in slurry and the heating of slurry.Slurry modulating process has modulation dehydration procedure and modulation heating process.Modulation dehydration procedure mixes to carry out the modulation of slurry and the dehydration of coal by the solvent liquid and coal that make to recycle in circulating process.Modulation heating process mixes the modulation and heating to carry out slurry by the solvent vapour and slurry that make to recycle in circulating process.
Description
Technical field
The present invention relates to a kind of manufacturing methods of ashless coal.
Background technology
The previous manufacturing method (such as patent document 1) that there is ashless coal.The system of ashless coal described in patent document 1
Method is made as method as described below (with reference to the claim 1 with document)." a kind of manufacturing method of ashless coal, has：Slurry
Expect modulating process, solvent and coal are mixed and modulate slurry；Extraction process, to the slurry that is obtained in the slurry modulating process into
Row heats ... and extracts the coal ingredient for dissolving in solvent；Separation process is detached from the extraction process in the slurry of gained
Coal ingredient insoluble in solvent；It is recycled in the slurry comprising the coal ingredient insoluble in solvent detached from the separation process molten
Agent and the process for obtaining ashless coal；With the process that be recovered to solvent is made to be recycled in the slurry modulating process.”
Existing technical literature
Patent document
Patent document 1：No. 4045229 bulletins of Japan Patent
Invention content
Technical problems to be solved by the inivention
The manufacturing method of ashless coal described in patent document 1 includes " detaching from the separation process as described above
The slurry comprising coal ingredient insoluble in solvent in recycling design and obtain the process of ashless coal " (process is set as " ashless
Coal obtains process ").It is high temperature (such as 270 DEG C etc.) that ashless coal, which obtains institute's recovered solvent in process,.On the other hand, patent text
Offer the ashless coal described in 1 manufacturing method include " in the slurry modulating process gained slurry heat ... and
Extraction dissolves in the extraction process of the coal ingredient of solvent ".The slurry for being supplied in extraction process is added before extraction process
Hot (preheating).For this purpose, consider that supply will be used as by the thermal energy of recovered solvent (high temperature side liquid) in ashless coal obtains process
In the heating source of the slurry (low temperature side liquid) of extraction process.Additionally, it is contemplated that it is carried out using heat exchanger by high temperature side liquid
Heating to low temperature side liquid.
But in the heat exchange using heat exchanger, need in the heat exchanger entrance temperature of high temperature side liquid and low
Set temperature is poor between the heat exchanger outlet temperature of warm side liquid.Therefore, in the heat exchange, in ashless coal obtains process
A part for thermal energy will not transfer heat to the slurry for being supplied in extraction process possessed by institute's recovered solvent (high temperature side liquid)
In (low temperature side liquid).
For this purpose, the purpose of the present invention is to provide a kind of manufacturing method of ashless coal, by be effectively performed coal with it is molten
The heat exchange of agent and the heat exchange of slurry and solvent, generate so as to effectively utilize in the manufacturing process of ashless coal
Thermal energy.
For solving the means of technical problem
The manufacturing method of the ashless coal of the present invention has：Coal and solvent are mixed and modulate slurry by slurry modulating process, and
And carry out the dehydration of coal contained in above-mentioned slurry and the heating of above-mentioned slurry；Extraction process, in above-mentioned slurry modulating process
The slurry of gained is heated and extracts the coal ingredient for dissolving in solvent；Separation process, by the slurry of gained in above-mentioned extraction process
Material is separated into the solution comprising the coal ingredient for dissolving in solvent and the solid constituent that forms of the concentration of the coal ingredient insoluble in solvent is dense
Contracting liquid；Ashless coal obtains process, evaporates separation solvent in the solution isolated from above-mentioned separation process and obtains ashless coal；With
Circulating process makes above-mentioned ashless coal obtain the solvent cycle evaporated and isolated in process.Above-mentioned slurry modulating process has：Modulation
Dehydration procedure is mixed by the solvent liquid and coal that will be recycled in above-mentioned circulating process, so as to carry out the modulation of slurry and coal
Dehydration；With modulation heating process, mixed by the solvent vapour and slurry that will be recycled in above-mentioned circulating process, so as to be starched
The modulation and heating of material.
Invention effect
According to the above configuration, by the way that the heat exchange of coal and solvent and the heat exchange of slurry and solvent is effectively performed, from
And the thermal energy generated in the manufacturing process of ashless coal can be effectively utilized.
Description of the drawings
Fig. 1 is the schematic diagram of ashless coal manufacturing device 1.
Fig. 2 is the schematic diagram of the ashless coal manufacturing device 101 of comparative example.
Specific embodiment
The ashless coal manufacturing device 1 of the manufacturing method of ashless coal and the manufacturing method for carrying out ashless coal is carried out with reference to Fig. 1
Explanation.
Ashless coal manufacturing device 1 manufactures ashless coal (HPC for the coal (also referred to as " coal ") from raw material except deashing；
Hyper-coal device).Ashless coal manufacturing device 1 has coal slurry handling machine 11~37, the circulation path 41~46 and follows
Machine 51~91 on loop.
Coal slurry handling machine 11~37 is the machine for being handled coal and slurry (aftermentioned).At coal slurry
Reason machine 11~37 has coal supply pipeline 11 and steam discharging device 13.And then coal slurry handling machine 11~37 is from nothing
The upstream side of the manufacturing process of culm is risen has slurry modulation machine 20, preheater 31, extraction tank 33,35 and of separator successively
Solvent recovery unit 37.
Coal supply pipeline 11 supplies coal to slurry modulation machine 20 (coal supply step).Coal supply pipeline 11 is by coal from sending
In the supply (not shown) such as glassware to the modulation dehydration slot 21 (aftermentioned) of slurry modulation machine 20.The coal is such as bituminous coal or rudimentary
Coal (lignite, ub-bituminous coal).The extraction yield (ratio for being extracted into the soluble ingredient of the coal in solvent) of bituminous coal is higher than rudimentary coal.It is rudimentary
Coal is more cheap than bituminous coal.
Steam discharging device 13 will modulate dehydration slot 21 (aftermentioned) by flowing into purge gas into coal supply pipeline 11
The discharge (steam discharge process) out of coal supply pipeline 11 of the steam of middle generation.Above-mentioned purge gas is in coal supply pipeline 11
In the gas of gaseous state, for example, nitrogen (purging nitrogen).Steam discharging device 13 is to inhibit coal supply pipeline 11
Blockage problem and set.Above-mentioned " blockage problem " may generate as described below.It is carried out in modulation dehydration slot 21 (aftermentioned)
The heating and dehydration of coal, as a result generate steam.The major part of the steam is vapor, and a part for the steam is solvent vapour
(solvent of gaseous state).If the steam is entered in coal supply pipeline 11, which is cooled as condensed liquid, this is solidifying
Contracting liquid is attached to the inner surface of coal supply pipeline 11.If coal is attached on the condensed liquid, coal, which can block coal supply pipeline 11, (to be made
Flow path is narrow or completely plugged flow path).In that way it is possible to lead to the problem of above-mentioned " blocking ".Steam discharging device 13 has valve 13a
With purge gas feedway 13b.
Valve 13a is configured on coal supply pipeline 11.The object being passed through in coal supply pipeline 11 is controlled by the opening and closing of valve 13a
The flowing of matter (coal, steam and purge gas).It is preferred that multiple (such as 2) valve 13a are configured in series on coal supply pipeline 11.
In the case of multiple valve 13a are configured on coal supply pipeline 11, compared with the situation of 1 only is configured, can more inhibit steam into
Enter into coal supply pipeline 11.Valve 13a is such as revolving valve.
Purge gas feedway 13b supplies purge gas to coal supply pipeline 11 (purge gas supply step).
In the case of 2 valve 13a are configured in series on coal supply pipeline 11, purge gas feedway 13b supplies purge gas
It is given between 2 valve 13a.
Slurry modulates machine 20 and mixes coal and solvent and modulate slurry (coal-solvent slurry), and carries out the de- of slurry
Water and heating (slurry modulating process).
The solvent being supplied in slurry modulation machine 20 is the solvent for dissolving coal.The solvent preferably makes in extraction tank
The high solvent of the ratio (extraction yield) of the soluble ingredient of the coal extracted in 33.From the viewpoint of extraction yield, the solvent is preferred
Stablize even if in a heated state, and preferably there is larger dissolving power (excellent with the compatibility of coal) to coal.The solvent is excellent
It is selected as making the high solvent of the solvent recovering rate in solvent recovery unit 37.From the viewpoint of solvent recovering rate, the solvent is preferred
It can be using easily being recycled the methods of distillation.Pressure reduction from extraction tank 33 and separator 35 is extracting
The viewpoints such as the extraction yield in slot 33 are set out, and the boiling point of solvent is for example preferably 180~300 DEG C, more preferably 230~280 DEG C.It should
Solvent is such as coal derivative.The solvent is mainly obtains solvent from coal carbonization product purification.The solvent is for example comprising virtue
The solvent (aromatic solvent) of fragrant compounds of group.The main component of the solvent is 2 cyclic aromatic series.2 cyclic aromatic series for such as naphthalene,
Methyl naphthalene, dimethylnaphthalene, trimethyl-naphthalene etc..The other compositions of the solvent are the naphthalenes for being respectively provided with aliphatic lateral chain, anthracene class, fluorenes
Class attached alkylbenzene of xenyl, long-chain fat race side chain etc. to them.Specifically, for example, the solvent is methyl naphthalene
Oil, naphtalene oil etc..The dry distillation of coal is is manufactured the distilled oil as by-product oil during coke by methylnaphthalene oil, naphtalene oil.Slurry preparer
Device 20 has modulation dehydration slot 21 and modulation heating machine 23.
Solvent liquid (solvent of liquid condition) and coal by being mixed modulation and coal to carry out slurry by modulation dehydration slot 21
Dehydration (modulation dehydration procedure).The solvent liquid of supply to modulation dehydration slot 21 is to be followed by a part for the circulation path 41~46
The solvent liquid of ring.The coal of supply to modulation dehydration slot 21 is supplied from coal supply pipeline 11.Solvent in modulation dehydration slot 21
The mixing of liquid and coal is for example carried out by the way that coal is put into the solvent liquid modulated in dehydration slot 21.Slot 21 is dehydrated by modulation
In solvent liquid and coal mixing, so as to modulate slurry.S/C (the Slurry/Coal of slurry modulated in modulation dehydration slot 21；
The quality of slurry relative to the coal of drying regime mass ratio) be for example, about 2.0.
Modulation dehydration slot 21 carries out the dehydration of coal in the following way.Modulation dehydration slot 21 is by the way that solvent liquid and coal are mixed
It closes and solvent liquid is made to be in direct contact with coal.Modulation dehydration slot 21 is in direct contact to make directly to carry out between solvent liquid and coal by this
Heat exchange.Modulation dehydration slot 21 makes coal heat up and evaporates the moisture (water containing coal) in coal by the heat exchange.Supply
Temperature to the solvent liquid of modulation dehydration slot 21 is more than the temperature carried out needed for the dehydration and the boiling point of insufficient solvent.Supply is extremely
The temperature of the solvent liquid of modulation dehydration slot 21 is, for example, more than 230 DEG C, is preferably 235 DEG C or more, and for example, 240 DEG C with
Under.The temperature of supply to the solvent liquid of modulation dehydration slot 21 is 237 DEG C in the example depicted in figure 1 (hereinafter, with reference to Fig. 1 to temperature
The concrete example of degree illustrates).
(modulation heats up for the modulation and heating that modulation heating machine 23 carries out slurry by the way that solvent vapour and slurry are mixed
Process).Modulation heating machine 23 adjusts the concentration of slurry according to the entrance concentration of extraction tank 33.To the entrance concentration of extraction tank 33
It is set in advance.Without heating up in modulation, the machine of the concentration for adjusting slurry is set between machine 23 and extraction tank 33,
There is no such machine in ashless coal manufacturing device 1.The S/C of slurry modulated in modulation heating machine 23 is for example, about 4.0.It adjusts
System heating machine 23 makes slurry be warming up to then slurry modulation machine 20 and supply the machine of slurry and (is referred to as " machine after slurry modulation
Device ") inlet temperature until.The inlet temperature of " machine after slurry modulation " is set in advance." machine after slurry modulation "
Specially preheater 31 is extraction tank 33 in the case where being not provided with preheater 31.Without in modulation heating machine 23 and " slurry
Setting does not have such machine for adjusting the machine of the temperature of slurry in ashless coal manufacturing device 1 between machine after material modulation "
Device.Modulation heating machine 23 has Venturi scrubber 23a and modulation heating slot 23b.
Venturi scrubber 23a mixes solvent vapour and slurry (the first modulation heating process).Supply to venturi is washed
The solvent vapour for washing device 23a is the solvent vapour recycled by a part (details is as described later) for the circulation path 41~46.
It supplies and is supplied to the slurry of Venturi scrubber 23a from modulation dehydration slot 21.It supplies to the slurry of Venturi scrubber 23a
It is modulated and dewatered slurry to be dehydrated in slot 21 in modulation.Venturi scrubber 23a is by by slurry and solvent vapour
It mixes and slurry is made to be in direct contact with solvent vapour.Venturi scrubber 23a is in direct contact to make solvent vapour and slurry by this
Heat exchange is directly carried out between material.Venturi scrubber 23a (utilizes solvent vapour putting when condensing using the latent heat of solvent vapour
Heat) slurry is heated.In the case of being dehydrated in modulation and not completing the dehydration of coal in slot 21, Venturi scrubber 23a leads to
Cross the dehydration for slurry being heated and being carried out the coal in slurry.Venturi scrubber 23a makes slurry become microgranular, and will
Microgranular slurry and solvent vapour mixing.Venturi scrubber 23a by increasing the flow velocity of microgranular slurry and solvent vapour,
And microgranular slurry is made to generate shearing force with solvent vapour and mix microgranular slurry and solvent vapour.It is explained, it can be with
Instead of Venturi scrubber 23a or use on this basis by solvent vapour and slurry mix in addition to Venturi scrubber
Device (the first modulation heat riser).Above-mentioned " device in addition to Venturi scrubber " is including such as static mixer.It is static
Mixing machine is using the element (component of the shape after plate is distorted, spiral helicine component) for the inside for being configured at pipe by microgranular slurry
Material and solvent vapour are stirred and mix.
The mixture mixed in Venturi scrubber 23a is further mixed (the second modulation by modulation heating slot 23b
Heating process).Modulation heating slot 23b makes slurry and the further heat exchange of solvent by the mixing.Solvent can be inhibited
The mode of gasification (solvent vapour damage) in modulation heating slot 23b to pressurizeing, such as pressurizeed with 50kPaG.
Preheater 31 is by the slurry modulated (in slurry modulation machine 20) in modulation heating machine 23 in supply to extraction
It is heated in advance (preheating procedure) before slot 33.It is explained, can also there is no preheater 31.
Extraction tank 33 is heated to extract the coal for dissolving in solvent by modulating slurry in the slurry of gained in machine 20
Ingredient (solvent soluble ingredient) (extraction process).Extraction tank 33 extracts the organic principle in coal.The details of the extraction is as follows
It is described.For supplying to the slurry of extraction tank 33, it is stirred using the blender for being set to extraction tank 33, is heated on one side on one side
It is maintained at set point of temperature (aftermentioned).As a result, from slurry extractant soluble ingredient.But solvent is not only included in extract
Soluble ingredient, also comprising the ingredient (solvent insoluble component) (such as ash grades) insoluble in solvent.
The heating temperature of slurry in the extraction tank 33 is the temperature that solvent soluble ingredient is enable to be dissolved in solvent.Specifically
For, the heating temperature of slurry is, for example, 300 DEG C or more, preferably 360 DEG C or more.The heating temperature of slurry is, for example, 420 DEG C
Below, it is preferably less than 400 DEG C.Slurry heating temperature less than 300 DEG C in the case of, for weaken coal intermolecular knot
It is also and insufficient for conjunction, therefore solvent soluble ingredient is lower to the meltage of solvent.Slurry heating temperature more than 420 DEG C
In the case of, the pyrolysis of coal becomes active, cause generated thermal decomposition free radical in conjunction with therefore solvent is solvable
The extraction yield of ingredient reduces.
The extraction carried out in the extraction tank 33 is preferably in the presence of inactive gas (such as preferably cheap nitrogen)
It carries out.In order to carry out the extraction, need solvent being limited to liquid phase (solvent not being made to volatilize).In order to which solvent is limited to liquid phase,
Need to make the pressure (pressure, the operating pressure that apply to solvent and slurry) in extraction tank 33 higher than the vapour pressure of solvent.Extraction
Temperature, the vapour pressure of used solvent when pressure in slot 33 additionally depends on extraction, it is preferred that for 1.0~2.0MPa.
Separator 35 is (molten for the solution comprising the coal ingredient for dissolving in solvent by the pulp separation of gained in extraction tank 33
Liquid portion, supernatant, overflow) and the solid constituent concentrate (underflow that forms of coal ingredient concentration insoluble in solvent
(underflow)) (separation process).The method of the separation is such as settling methods, filtration method or centrifugal separation.Gravity
Sedimentation be by by slurry be held in slot and using gravity make solvent insoluble component sedimentation and be separated into solution and solid into
Divide the mode of concentrate.Hereinafter, the separation in separator 35 is illustrated using settling methods come situation about carrying out.It is right
(or heating) and pressurization are kept the temperature in separator 35.The heat preservation (or heating) and pressurization be dissolved out in order to prevent from coal it is molten
Agent soluble ingredient is precipitated and carries out again.Temperature in separator 35 is, for example, 300~380 DEG C.In separator 35
Pressure is, for example, 1.0~3.0MPa.Separator 35 is, for example, 2 segmentations (quantity of gravitation settler is 2).The separation of 2 segmentations
Device 35 has the first gravitation settler 35a and the second gravitation settler 35b.It is explained, separator 35 can be 1 segmentation
(quantity of gravitation settler is 1).It is explained, separator 35 is completely separated into supernatant and solid constituent concentrate
Ideal, but sometimes also can a part for supernatant be mixed into solid constituent (the coal ingredient insoluble in solvent) or
Supernatant is mixed into a part for solid constituent concentrate.
Recycling design in the solution that solvent recovery unit 37 is isolated from separator 35.Solvent recovery unit 37 is
For obtaining the device of ashless coal, extract residue (aftermentioned) in the solution that is detached from separator 35.Solvent recovery unit 37
Have the first solvent recovery unit 37a and the second solvent recovery unit 37b.
First solvent recovery unit 37a is obtains for evaporation separation solvent in the solution isolated from separator 35
To the device of ashless coal (HPC) (for carrying out the device that ashless coal obtains process).Ashless coal is completely without moisture and almost
Coal without ash content.Contained ash content is below 5 weight %, is preferably below 3 weight % in ashless coal.The calorific value of ashless coal
Higher than feed coal, ignitability, completely burned are good, therefore are used as the high efficiency fuel of such as boiler etc..Ashless coal
Mobility (softening meltbility) it is higher than feed coal, as the raw material of iron coke for example processed or a part (mixed coal) for raw material
To use.
The method of the evaporation separation of the solvent carried out in first solvent recovery unit 37a includes such as way of distillation, evaporation
Method etc..Evaporation is included such as spray drying process.The way of distillation is included such as flash method, Thin film evaporation techniques.For example, first is molten
Agent retracting device 37a is the flash tank (flasher) for carrying out flash method.In addition, for example, the first solvent recovery unit 37a
To be used to carry out the thin-film distillation slot of Thin film evaporation techniques.In addition, for example, the first solvent recovery unit 37a for have flash tank and
The device of thin-film distillation slot (such as downstream side for being configured at flash tank).
(flash method)
It is carried out in the following way using the evaporation separation of the solvent of flash method.Make the pressure ratio separator in flash tank
(such as 70kPaG) low in 35.In this case, solution separated in separator 35 is ejected into flash tank.Moreover, solution
In solvent separation is evaporated from solution.
(Thin film evaporation techniques)
It is carried out in the following way using the evaporation separation of the solvent of Thin film evaporation techniques.It is separated molten in separator 35
Liquid is directed in thin-film distillation slot.Moreover, the curette (also referred to as wiper) being contained in thin-film distillation slot is by film
The inner wall of distillation tank forms the film of distillation object (separated solution in separator 35) to carry out continuous still.Film steams
Pressure in sluice is, for example, 0.1MPaG.In order to solvent be made suitably to evaporate in thin-film distillation slot, and to thin-film distillation
The wall surface of slot is heated.The heating of the wall surface of thin-film distillation slot can be carried out using such as deep fat, can also be utilized for example
Electric heater carries out.In the case where the heating of the wall surface of thin-film distillation slot is carried out using deep fat, in thin-film distillation slot
The inside of wall surface and outside (in addition, side in such as inside and outside) setting casing (coil serving).It is flowed into the casing
Deep fat.As a result the wall surface of thin-film distillation slot is heated.The heating of the wall surface of thin-film distillation slot needs such as situations below.The
One solvent recovery unit 37a has the thin-film distillation slot in the downstream side of flash tank and flash tank sometimes.At this point, using in flash tank
Distillation and reduce the temperature of solution.Therefore, it in order to solvent be made suitably to evaporate in thin-film distillation slot, and carries out thin
The heating of the wall surface of membrane distillation slot.
Second solvent recovery unit 37b is for evaporation point in separated solid constituent concentrate from separator 35
Exsolution agent and obtain extract residue (RC；Residue coal) device of (also referred to as residual coal) (obtains work for carrying out extract residue
The device of sequence).The coal that extract residue is formed for solvent insoluble component (ash grades) concentration, the mixed coal of the raw material as such as coke
A part use.It is similary with the method that the evaporation of the solvent in the first solvent recovery unit 37a detaches, the second solvent recovery
The method of the evaporation separation of solvent in device 37b includes the way of distillation, evaporation etc..It is explained, second can not also be set
Solvent recovery unit 37b.
The circulation path 41~46 makes the solvent for evaporating separation in 37 grade of solvent recovery unit be recycled (circulating process).It follows
Loop 41~46 is the flow path (piping) for solvent to be recycled.The circulation path 41~46 has first circulation road 41,
Two the circulation paths 42, third the circulation path 43, the 4th the circulation path 44, the 5th the circulation path 45 and the 6th the circulation path 46.
First circulation road 41 make to evaporate in the first solvent recovery unit 37a the solvent of separation modulation be dehydrated in slot 21 into
Row cycle (first circulation process).First circulation road 41 imports the solvent taken out from the top of the first solvent recovery unit 37a
In modulation dehydration slot 21.
Second circulation road 42 makes to evaporate the solvent of separation in the first solvent recovery unit 37a in modulation heats up machine 23
It is recycled (second circulation process).Second circulation road 42 makes the solvent for evaporating separation in the first solvent recovery unit 37a exist
It is recycled in Venturi scrubber 23a.Second circulation road 42 makes to evaporate the solvent of separation in the first solvent recovery unit 37a
Directly recycled in (without recuperation of heat or heating) Venturi scrubber 23a.Piping crushing in second circulation road 42
The sum of (such as 20kPaG) and the operating pressure (such as 50kPaG) in Venturi scrubber 23a and the first solvent recovery unit
Operating pressure (such as 70kPaG) in 37a is equal.Therefore, the operating pressure in the first solvent recovery unit 37a is based on literary mound
In the sum of operating pressure in washer 23a and the piping crushing in second circulation road 42 set.
Third the circulation path 43 makes the solvent for evaporating separation in the first solvent recovery unit 37a be carried out in separator 35
It recycles (third circulating process).The solvent that third the circulation path 43 makes to evaporate separation in the first solvent recovery unit 37a is second
It is recycled in gravitation settler 35b.By supplying solvent from third the circulation path 43 to the second gravitation settler 35b, (high temperature is molten
Agent condensed liquid), so as to provide the solvent supply amount needed for the second gravitation settler 35b.
4th the circulation path 44 make to evaporate in the second solvent recovery unit 37b the solvent of separation modulation be dehydrated in slot 21 into
Row cycle (the 4th circulating process).4th the circulation path 44 imports the solvent taken out from the top of the second solvent recovery unit 37b
In modulation dehydration slot 21.It is explained, imports in the steam of the 4th the circulation path 44 from the second solvent recovery unit 37b and not only include
Solvent but also include nitrogen.
5th the circulation path 45 makes the steam generated in slurry modulation machine 20 be recycled the (the 5th in modulation dehydration slot 21
Circulating process).The steam generated in slurry modulation machine 20 includes solvent and water, compared with solvent, includes more water.5th follows
Loop 45 makes the steam generated in modulation dehydration slot 21 be recycled in modulation dehydration slot 21.5th the circulation path 45 makes modulation liter
The steam generated in warm slot 23b is dehydrated in slot 21 in modulation and is recycled.It is explained, in slurry modulation machine 20 in Fig. 1
" A " that top is recorded partly is associated with " A " part recorded in the figure in the left of cooler 81.
6th the circulation path 46 makes the solvent vapour generated in extraction tank 33 be recycled in modulation dehydration slot 21, and (the 6th follows
Ring process).
Machine 51~91 is the machine for being configured in the circulation path 41~46 (in addition on second circulation road 42) in the circulation path.
Machine 51~91 includes following machine in the circulation path.The machine being configured on first circulation road 41 includes recycling design slot 51.Match
It is placed in the machine in third the circulation path 43 and includes row's thimble-tube boiler 61, heat exchanger 63 and preheater successively from upstream side
65.The machine in the 4th the circulation path 44 is configured to include bag filter 71 successively from upstream side, arrange thimble-tube boiler 73, is cold
But device 75, heat exchanger 77 and recycling design slot 51.The machine being configured in the 5th the circulation path 45 includes successively from upstream side
Cooler 81, oil-water separation tank 83, heat exchanger 77 and recycling design slot 51.Machine in the 6th the circulation path 46 is configured at from upper
It swims side and rises and include oily heating device 91, heat exchanger 63, heat exchanger 77, oil-water separation tank 83, heat exchanger 77 and recycling successively
Flux bath 51.
Recycling design slot 51 modulates the solvent liquid (solvent liquid modulating process) for being supplied to modulation dehydration slot 21.Supply is extremely
The solvent of recycling design slot 51 is the solvent (solvent vapour) for being passed through first circulation road 41, is in the first solvent more specifically
The solvent vapour of separation is evaporated in retracting device 37a.The solvent vapour that separation is evaporated in first solvent recovery unit 37a is straight
(without recuperation of heat or heating) supply is connect to recycling design slot 51.In addition, the solvent of supply to recycling design slot 51 is inflow
The solvent of 4th the circulation path 44, the 5th the circulation path 45 and the 6th the circulation path 46, more specifically, for using heat exchanger 77 (after
State) carry out the solvent liquid after heat exchange.
Arrange the heat (third the circulation path heat extraction recovery process) that the recycling of thimble-tube boiler 61 flows into the solvent of third the circulation path 43.
The solvent of supply to row's thimble-tube boiler 61 is the solvent (solvent vapour) for being passed through third the circulation path 43, is the more specifically
The solvent vapour of separation is evaporated in one solvent recovery unit 37a.The solvent of separation is evaporated in first solvent recovery unit 37a
Steam is directly fed to row's thimble-tube boiler 61.Arrange heat of the thimble-tube boiler 61 using supply to the solvent of row's thimble-tube boiler 61
Energy manufactures saturated vapor (steam).Row's thimble-tube boiler 61 makes supply to the temperature for the solvent vapour for arranging thimble-tube boiler 61
Degree reduces, and makes the solvent vapour condensing.It arranges thimble-tube boiler 61 and such as 2.2MPaG is manufactured with the speed of such as 19.30t/h
Saturated vapor.It is explained, row's thimble-tube boiler 61 can be replaced with the heat extraction and recovery device in addition to boiler.It can be with
This point is replaced similarly to use aftermentioned 73 grade of row's thimble-tube boiler with the heat extraction and recovery device in addition to boiler.It removes
Heat extraction and recovery device other than boiler includes the device for example for being heated to deep fat (with reference to aftermentioned oily heating device 91)
Deng.
Heat exchanger 63 makes the solvent of inflow third the circulation path 43 heat up (third the circulation path heating process).Supply to heat is handed over
The low temperature side liquid (fluid for the side being warmed) of parallel operation 63 is the solvent for flowing into third the circulation path 43, more specifically, is
Solvent liquid in thimble-tube boiler 61 is arranged after heat exchange.It supplies to the high temperature side liquid (side being warmed of heat exchanger 63
Fluid) to flow into the solvent of the 6th the circulation path 46, be molten after recuperation of heat in oily heating device 91 (aftermentioned) more specifically
Agent (solvent vapour).
Preheater 65 is supplying the solvent for flowing into third the circulation path 43 to being heated (the before separator 35 in advance
Three the circulation path preheating procedures).It is that the solvent (solvent after heat exchange is carried out using heat exchanger 63 to supply to the solvent of preheater 65
Liquid).Preheater 65 makes the required temperature that solvent is warming up in separator 35 (the second gravitation settler 35b).
Solvent for flowing into the 4th the circulation path 44 etc. is filtered (filter progress) by bag filter 71.It supplies to pocket type mistake
The solvent of filter 71 by the second solvent recovery unit 37b evaporation separation solvent (solvent vapour).
Row's thimble-tube boiler 73 is recycled the heat for the solvent for flowing into the 4th the circulation path 44, and (the 4th the circulation path heat extraction is recycled
Process).The solvent of supply to row's thimble-tube boiler 73 is the solvent (solvent vapour) being filtered using bag filter 71.Row
Thimble-tube boiler 73 manufactures saturated vapor using the thermal energy of solvent.Thimble-tube boiler 73 is arranged with the speed of such as 6.03t/h
Manufacture the saturated vapor of such as 0.70MPaG.
Cooler 75 is cooled down the solvent for flowing into the 4th the circulation path 44 (the 4th the circulation path cooling process).Cooler 75
Solvent is cooled down using such as cooling water.It is by the molten of 73 recuperation of heat of row's thimble-tube boiler to supply to the solvent of cooler 75
Agent (solvent vapour).Cooler 75 is fed to the solvent vapour cooling of cooler 75 and makes its condensing.
Heat exchanger 77 is the solvent heating (the 4th the circulation path heating process) for flowing into the 4th the circulation path 44.Heat exchanger 77
It is the solvent heating (the 5th the circulation path heating process) for flowing into the 5th the circulation path 45.Heat exchanger 77 makes the 6th the circulation path 46 of inflow
Solvent heating (the 6th the circulation path heating process).It supplies to the low temperature side liquid of heat exchanger 77 to flow into the 4th the circulation path 44
Solvent, more specifically, for using 75 solvent after cooling of cooler (solvent liquid).It supplies to the low temperature side of heat exchanger 77
Fluid is the solvent for flowing into the 5th the circulation path 45 and the 6th the circulation path 46, is in oil-water separation tank 83 (aftermentioned) more specifically
Solvent (solvent liquid) after middle water-oil separating.It is the molten of the 6th the circulation path 46 of inflow to supply to the high temperature side liquid of heat exchanger 77
Agent, more specifically, to utilize the solvent after the progress heat exchange of heat exchanger 63 and in oil-water separation tank 83 before water-oil separating
(solvent vapour).
Cooler 81 carries out the steam (steam comprising solvent and water as described above) for flowing into the 5th the circulation path 45 cold
But (the 5th the circulation path cooling process).Cooler 81 is cooled down steam using such as cooling water.Cooler 81 is cold by steam
But and make its condensing.
Oil-water separation tank 83 detaches solvent (oil) and water (water-oil separating process) from the fluid for flowing into 45 grade of the 5th the circulation path.
It supplies to the fluid that the fluid of oil-water separation tank 83 is the 5th the circulation path 45 of inflow, is cold using cooler 81 more specifically
But the liquid after.It supplies to the fluid that the fluid of oil-water separation tank 83 is the 6th the circulation path 46 of inflow, more specifically, to utilize
Solvent (solvent liquid) after 77 heat exchange of heat exchanger.Separated water is as waste water (WW in oil-water separation tank 83；waste
Water it) is discharged from oil-water separation tank 83.
Oily heating device 91 makes deep fat heating (oil using the thermal energy for the solvent (solvent vapour) for flowing into the 6th the circulation path 46
Heating process).The solvent of supply to oily heating device 91 is the solvent vapour generated in extraction tank 33.What oily heating device 91 was heated up
Deep fat is utilized as the heat source of other processes.The deep fat is utilized as the heat source of such as solvent recovery unit 37.The deep fat
Such as described above for the heating of the wall surface of the thin-film distillation slot of solvent recovery unit 37.It is explained, oil can be risen
Warm device 91 is replaced with the heat extraction and recovery device (such as boiler etc.) in addition to the device that deep fat is made to heat up.
(the ashless coal manufacturing device 101 of comparative example)
In order to carry out the comparison of aftermentioned " comparison of practicality amount " etc., dress is manufactured to the ashless coal of comparative example shown in Fig. 2
101 are put to illustrate.Difference of the ashless coal manufacturing device 101 from ashless coal manufacturing device 1 (with reference to Fig. 1) is (to practicality amount
Compare the influential difference of tool) as shown in following [difference a]~[difference e].It is explained, ashless coal is manufactured and is filled
Put the 101 composition label same symbols shared (with reference to Fig. 1) with ashless coal manufacturing device 1.
[difference a]
Ashless coal manufacturing device 1 shown in FIG. 1 has modulation dehydration slot 21 and modulation heating machine 23.It replaces, Fig. 2
Shown ashless coal manufacturing device 101 has slurry preparation vessel 121, dehydration slot 122 and heating slot 123 successively from upstream side.
Coal and solvent are mixed to modulate slurry by slurry preparation vessel 121.Dehydration slot 122 is to the slurry modulated in slurry preparation vessel 121
In coal be dehydrated.Heating slot 123 makes dewatered slurry heating in dehydration slot 122.
[difference b]
Ashless coal manufacturing device 1 shown in FIG. 1 has steam discharging device 13 on coal supply pipeline 11, shown in Fig. 2
Ashless coal manufacturing device 101 does not have steam discharging device 13 (with reference to Fig. 1).Therefore, it is impossible to press down in steam discharging device 13
" blockage problem " (above-mentioned) of coal supply pipeline 11 processed.Therefore, in order to avoid the steaming in the moisture in coal of slurry preparation vessel 121
Hair, and the solvent for being fed to slurry preparation vessel 121 is cooled down (such as 107 DEG C).Specifically, utilize following [difference
Point c]~the composition of [difference e] and process cool down solvent.
[difference c]
Ashless coal manufacturing device 101 has first circulation road 141.First circulation road 141 is and ashless coal system shown in FIG. 1
Make the 42 corresponding flow path of first circulation road 41 and second circulation road of device 1.First circulation road 141 shown in Fig. 2 is for inciting somebody to action
The solvent vapour that separation is evaporated in first solvent recovery unit 37a is supplied to the flow path of slurry preparation vessel 121.In first circulation
Configuration is dehydrated slot 122 and heating slot 123 successively from upstream side on road 141.First circulation road 141 makes the first solvent recovery unit
The solvent (solvent vapour) that separation is evaporated in 37a flows into dehydration slot 122 and heating slot 123.First circulation road is flowed into as a result,
141 solvent carries out heat exchange indirectly with the slurry in dehydration slot 122 and in heating slot 123.That is, as dehydration slot 122 and
Heat up slot 123 in slurry dehydration and heating heating source, using evaporated in the first solvent recovery unit 37a detach
The thermal energy of solvent vapour.
[difference d]
Ashless coal manufacturing device 101 has row's thimble-tube boiler 153 and cooler 155.Arrange thimble-tube boiler 153 and cooling
Device 155 is configured at first circulation road 141.Row's thimble-tube boiler 153 utilizes the solvent (solvent liquid) after heat exchange in the slot 123 that heats up
Thermal energy manufacture saturated vapor.Thimble-tube boiler 153 is arranged with the saturated vapor of the speed manufacture 0.50MPaG of 8.18t/h.
Cooler 155 cools down the solvent (solvent liquid) arranged in thimble-tube boiler 153 after recuperation of heat using cooling water.
[difference e]
Ashless coal manufacturing device 101 has row's thimble-tube boiler 193 and cooler 195.Arrange thimble-tube boiler 193 and cooling
Device 195 is configured in the 6th the circulation path 46.In ashless coal manufacturing device 101, the 6th the circulation path 46 makes to generate in extraction tank 33
Steam recycled in slurry preparation vessel 121.After row's thimble-tube boiler 193 in oily heating device 91 using making deep fat heat up
The thermal energy of solvent (solvent vapour) manufacture saturated vapor.Thimble-tube boiler 193 is arranged to manufacture with the speed of 1.72t/h
The saturated vapor of 0.5MPaG.The solvent (solvent liquid) arranged in thimble-tube boiler 193 after recuperation of heat is used cooling by cooler 195
Water is cooled down.It is explained, row's thimble-tube boiler 73 of ashless coal manufacturing device 101 is manufactured with the speed of 6.88t/h
The saturated vapor of 0.50MPaG.
(comparison of practicality amount)
The manufacturing method (using the situation of ashless coal manufacturing device 1 shown in FIG. 1) of the ashless coal of present embodiment is opposite
It is as follows in the practicality amount of the manufacturing method (situation for using ashless coal manufacturing device 101) of the ashless coal of comparative example.
Saturated vapor occurrence quantity：Increase about 50%
Cooling water usage amount：Cut down about 30wt%
(saturated vapor occurrence quantity)
Saturated vapor yield in ashless coal manufacturing device 1 shown in FIG. 1 is row's thimble-tube boiler 61 and heat extraction recycling
The total amount of saturated vapor manufactured by boiler 73.Saturated vapor yield in ashless coal manufacturing device 101 shown in Fig. 2 is row
Thimble-tube boiler 153, row's thimble-tube boiler 193 and the total amount for arranging the saturated vapor manufactured by thimble-tube boiler 73.By above-mentioned ratio
Relatively result is understood：In the case where using ashless coal manufacturing device 1 shown in FIG. 1, compared with comparative example, heat extraction can be recycled
The vapor volume that can be recycled in boiler increases.
(cooling water usage amount)
Cooling water usage amount in ashless coal manufacturing device 1 is cooler 75 and the cooling water usage amount in cooler 81
Total amount.Cooling water usage amount in ashless coal manufacturing device 101 shown in Fig. 2 is cooler 155, cooler 195 and cooler
The total amount of cooling water usage amount in 75.From above-mentioned comparison result：Using ashless coal manufacturing device 1 shown in FIG. 1
In the case of, compared with comparative example, the usage amount of the cooling water used in cooler can be cut down.As a result：Compared with comparative example,
The operating cost of ashless coal manufacturing device 1 can be cut down.
(effect)
Then, the effect of the manufacturing method of the ashless coal using present embodiment is illustrated.Hereinafter, will in order to carry out
Each process and the machine (machine corresponding with each process) that uses marks parantheses after the title of process.
(effect 1)
The manufacturing method (ashless coal manufacturing device 1) of ashless coal has slurry modulating process (slurry modulates machine 20), extraction
Process (extraction tank 33), separation process (separator 35), ashless coal is taken to obtain process (the first solvent recovery unit 37a) and follow
Ring process (first circulation road 41, second circulation road 42).Coal and solvent is are mixed by slurry modulating process (slurry modulates machine 20)
It closes and modulates slurry, and the process for carrying out dehydration and the heating of slurry.Extraction process (extraction tank 33) is to modulate work to slurry
The process that the slurry of gained is heated and extracts the coal ingredient for dissolving in solvent in sequence (slurry modulates machine 20).Separation process
(separator 35) is to include the coal ingredient for dissolving in solvent by the pulp separation of gained in extraction process (extraction tank 33)
Solution and the process of solid constituent concentrate that forms of coal ingredient concentration insoluble in solvent.Ashless coal obtains process, and (first is molten
Agent retracting device 37a) for solution evaporation separation solvent separated from separation process (separator 35) obtain ashless coal
Process.Circulating process (first circulation road 41, second circulation road 42) is makes ashless coal obtain process (the first solvent recovery unit
The process that the solvent of separation is recycled is evaporated in 37a).Slurry modulating process (slurry modulates machine 20) has modulation dehydration
Process (modulation dehydration slot 21) and modulation heating process (modulation heating machine 23).
[forming 1-1]
It is molten by will be recycled in circulating process (first circulation road 41) to modulate dehydration procedure (modulation dehydration slot 21)
The process that agent liquid and coal mix and carry out the modulation of slurry and the dehydration of coal.
[forming 1-2]
Heating process (modulation heating machine 23) is modulated by will be recycled in circulating process (second circulation road 42)
The process that solvent vapour and slurry mix and carry out modulation and the heating of slurry.
The mixing of solvent and coal is carried out in the modulation dehydration procedure (modulation dehydration slot 21) of above-mentioned [forming 1-1].Due to
Solvent is made to be in direct contact with coal using the mixing, therefore solvent directly carries out heat exchange with coal.In addition, above-mentioned [forming 1-2]
Modulation heating process (modulation heating machine 23) in carry out mixing of solvent and slurry.Due to making solvent and slurry using the mixing
Material is in direct contact, therefore solvent directly carries out heat exchange with slurry.With the heat exchange of indirect (such as the heat using heat exchanger
Exchange) it compares, the efficiency of these direct heat exchanges is more preferable.Specifically, for example, in the heat exchange for using heat exchanger
In, heat exchanger entrance temperature and low temperature side liquid in high temperature side liquid (fluid for the side being warmed) is needed (to be warmed
Side fluid) heat exchanger outlet temperature between set temperature it is poor.On the other hand, in above-mentioned [forming 1-1] and [structure
Into 1-2] in the direct heat exchange that is carried out, above-mentioned temperature difference can be considered as zero.Therefore, it can be effectively performed
The heat exchange of coal and solvent and the heat exchange of slurry and solvent (being set as the effect [effect 1-1]).
And then in the modulation dehydration procedure (modulation dehydration slot 21) of above-mentioned [form 1-1], by solvent liquid (liquid) and
Coal (solid) mixes.Solvent liquid (liquid) and the same solvent vapour of heat exchange (gas) of coal (solid) and the heat exchange of coal (solid)
Compared to efficiency more preferably.In addition, in the modulation heating process (modulation heating machine 23) of above-mentioned [forming 1-2], by solvent vapour
(gas) and the slurry mixture of liquid (solid with) mix.Solvent vapour (gas) and slurry (mixture of solid and liquid)
Heat exchange with solvent vapour (gas), efficiency is more preferably compared with the heat exchange of coal (solid).Therefore, [1- is formed by above-mentioned
1] and [form 1-2], the heat exchange of coal and solvent can be effectively performed and the heat exchange of slurry and solvent (acts on this
It is set as [effect 1-2]).By above-mentioned [effect 1-1] and [effect 1-2], the manufacture in ashless coal can be effectively utilized
The thermal energy generated in journey.
(effect 2)
[forming 2]
It is pre- according to the entrance concentration as extraction process (extraction tank 33) to modulate heating process (modulation heating machine 23)
The entrance concentration first set adjusts the concentration of slurry.
By above-mentioned [forming 2], without (modulation heating machine 23 and extraction after heating process is modulated and before extraction process
Between slot 33) adjust slurry concentration.Therefore, with needing to set to adjust slurry after extraction process and before extraction process
The situation of the machine of concentration is compared, and can cut down number of machines.As a result equipment (the nothing for the manufacturing method for carrying out ashless coal can be cut down
Culm manufacturing device 1) equipment cost.
(effect 3)
[forming 3]
Slurry is made to be warming up to then slurry modulating process, and (slurry modulates machine to modulation heating process (modulation heating machine 23)
20) until inlet temperature, that is, preset inlet temperature of the process (such as preheater 31) carried out.
By above-mentioned [form 3], without after heating process modulate and then before the process of slurry modulating process progress
(between modulation heating machine 23 and such as preheater 31) adjusts the temperature of slurry.Therefore, with needing to set to rise in modulation
Then the situation for adjusting after warm process and before the process of slurry modulating process progress the machine of the temperature of slurry is compared, Ke Yixiao
Subtract number of machines.As a result the equipment cost of the equipment (ashless coal manufacturing device 1) for the manufacturing method for carrying out ashless coal can be cut down.
(effect 4)
[forming 4]
The mixing for modulating solvent vapour and slurry in heating process (modulation heating machine 23) utilizes Venturi scrubber
23a is carried out.
Reliably carried out in the Venturi scrubber 23a of above-mentioned [form 4] solvent vapour (gas) and slurry (solid with
The mixture of liquid) mixing.Therefore, the heat exchange of solvent vapour and slurry can be more effectively carried out.
(effect 5)
There is the manufacturing method (ashless coal manufacturing device 1) of ashless coal coal supply step (coal supply pipeline 11) and steam to arrange
Go out process (steam discharging device 13).Coal supply step (coal supply pipeline 11) is that (will be supplied used in slurry modulating process
To slurry modulation machine 20) process that is supplied by coal supply pipeline 11 of coal.
[forming 5]
Steam discharge process (steam discharging device 13) is that will be adjusted by flowing into purge gas into coal supply pipeline 11
The process that the steam generated in dehydration procedure (modulation dehydration slot 21) processed is discharged out of coal supply pipeline 11.
By above-mentioned [forming 5], the steam in coal supply pipeline 11 can be inhibited to become condensed liquid.Therefore, coal is attached to
The condensed liquid, so as to inhibit the blocking of coal supply pipeline 11.In addition, by above-mentioned [forming 5], coal supply pipe can be inhibited
Steam in line 11 becomes condensed liquid, and there is no need to prevent the generation of the steam in modulation dehydration procedure (modulation dehydration slot 21).
It is therefore not necessary to the solvent for being fed to modulation dehydration procedure (modulation dehydration slot 21) is cooled to (the modulation dehydration of modulation dehydration procedure
Slot 21) in do not generate the degree of steam.Therefore, with needing to set cooler (such as the cooler of Fig. 2 for carrying out the cooling
155) situation is compared, and can cut down number of machines (or scale of machine).As a result the manufacturing method for carrying out ashless coal can be cut down
Equipment (ashless coal manufacturing device 1) equipment cost.
(variation)
The above embodiment can carry out various modifications.For example, the temperature of solvent, slurry is exemplified in Fig. 1.It but can
With by the different temperature of the temperature of solvent, slurry is set as from Fig. 1 is illustrated temperature.
In addition, for example, represent that the state of solvent is (solvent liquid, molten with the arrow of the arrow of solid line and dotted line to distinguish in Fig. 1
Agent steam).But it is also possible to the state of solvent is set as the state different from state shown in FIG. 1.Wherein, supply is extremely modulated
The solvent for being dehydrated slot 21 is solvent liquid, and it is solvent vapour to supply to the solvent of Venturi scrubber 23a.
In addition, for example, it can suitably change the sequence (order of connection of each machine) of each process, each process (each machine)
Whether there is.[example 1] can no third the circulation path 43, the 4th the circulation path 44, the 5th the circulation path 45, the 6th the circulation path 46 and be configured at
Machine in these the circulation paths all or part of.[example 2] flows into the solvent of the 6th the circulation path 46 by 77 heat of heat exchanger
It is supplied after exchange to oil-water separation tank 83.But the solvent for flowing into the 6th the circulation path 46 can be by 77 heat exchange of heat exchanger
After supply to cooler 81.
It in addition, for example, can be by some or all of structure of the ashless coal manufacturing device 101 of comparative example shown in Fig. 2
It combines or replaces into some or all of composition with ashless coal manufacturing device 1 shown in FIG. 1.It specifically, for example, can be with
Row's thimble-tube boiler 193 in 6th the circulation path 46 shown in Fig. 2 is configured to the of ashless coal manufacturing device 1 shown in FIG. 1
In six the circulation paths 46.
With reference to detailed and specific embodiment, the present invention is described, but those skilled in the art are clear that：
The spirit and scope of the present invention can not departed from the present invention is made various changes and modifications.The application is based in December, 2013
Japanese patent application (Japanese Patent Application 2013-267439) filed in 25 days and propose, content is used as with reference to being incorporated herein.
Industrial availability
According to the present invention, by the way that the heat exchange of coal and solvent and the heat exchange of slurry and solvent is effectively performed, so as to
The thermal energy generated in the manufacturing process of ashless coal can be effectively utilized, and ashless coal can be manufactured inexpensively.
The explanation of symbol
1 ashless coal manufacturing device
11 coal supply pipelines
13 steam discharging devices
20 slurries modulate machine
21 modulation dehydration slots
23 modulation heating machines
23a Venturi scrubbers
33 extraction tanks
35 separators
37 solvent recovery units
41~46 the circulation paths
Claims (5)
1. a kind of manufacturing method of ashless coal, has following process：
Coal and solvent are mixed and modulate slurry by slurry modulating process, and carry out coal contained in the slurry dehydration and
The heating of the slurry；
Extraction process heats the slurry of gained in the slurry modulating process and extracts and dissolve in the solvent
Coal ingredient；
Separation process, by the pulp separation obtained in the extraction process be comprising dissolve in the coal of the solvent into
The solid constituent concentrate that the solution divided and the coal ingredient concentration insoluble in the solvent form；
Ashless coal obtains process, is evaporated in the solution isolated from the separation process and detaches the solvent and obtain ashless
Coal；With
Circulating process makes the ashless coal obtain the solvent cycle evaporated and isolated in process,
The slurry modulating process has：
Dehydration procedure is modulated, the slurry is carried out by the solvent liquid that will be recycled in the circulating process and coal mixing
Modulation and the coal dehydration, wherein, the temperature of solvent liquid of supply to modulation dehydration is the temperature carried out needed for the dehydration
Above and the boiling point of insufficient solvent；With
Heating process is modulated, by the solvent vapour that will be recycled in the circulating process and slurry mixing and described in progress
The modulation and heating of slurry.
2. the manufacturing method of ashless coal according to claim 1, wherein, it is described to modulate heating process to become the extraction
The mode of the entrance concentration of process, that is, preset entrance concentration adjusts the concentration of the slurry.
3. the manufacturing method of ashless coal according to claim 1 or 2, wherein, the modulation heating process makes the slurry
Until being warming up to the then i.e. preset inlet temperature of inlet temperature for the process that the slurry modulating process carries out.
4. the manufacturing method of ashless coal according to claim 1, wherein, the solvent in the modulation heating process steams
Gas is carried out with the mixing of the slurry using Venturi scrubber.
5. the manufacturing method of ashless coal according to claim 1, has：
Coal supply step supplies the coal used in the slurry modulating process using coal supply pipeline；With
Steam discharges process, by flowing into purge gas into the coal supply pipeline, so as to described modulate in dehydration procedure
The steam of generation is discharged out of described coal supply pipeline.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2013-267439 | 2013-12-25 | ||
| JP2013267439A JP5982666B2 (en) | 2013-12-25 | 2013-12-25 | Production method of ashless coal |
| PCT/JP2014/082579 WO2015098505A1 (en) | 2013-12-25 | 2014-12-09 | Method for producing ashless coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105793399A CN105793399A (en) | 2016-07-20 |
| CN105793399B true CN105793399B (en) | 2018-06-08 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480066265.XA Active CN105793399B (en) | 2013-12-25 | 2014-12-09 | The manufacturing method of ashless coal |
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| Country | Link |
|---|---|
| US (1) | US20160272910A1 (en) |
| JP (1) | JP5982666B2 (en) |
| KR (1) | KR101822772B1 (en) |
| CN (1) | CN105793399B (en) |
| AU (1) | AU2014371509B2 (en) |
| CA (1) | CA2928393A1 (en) |
| WO (1) | WO2015098505A1 (en) |
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| JP6827884B2 (en) * | 2017-05-24 | 2021-02-10 | 株式会社神戸製鋼所 | Ash-free coal manufacturing method and ash-free coal manufacturing equipment |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3970541A (en) * | 1973-12-17 | 1976-07-20 | Coal Industry (Patents) Limited | Gas extraction of coal |
| US4387015A (en) * | 1982-09-30 | 1983-06-07 | International Coal Refining Company | Coal liquefaction quenching process |
| CN2722997Y (en) * | 2004-07-24 | 2005-09-07 | 李建平 | Device for extracting fat soluble material |
| CN101511977A (en) * | 2006-10-12 | 2009-08-19 | 株式会社神户制钢所 | Method for production of ashless coal |
| CN101918519A (en) * | 2008-01-09 | 2010-12-15 | 株式会社神户制钢所 | Apparatus and process for producing solid fuel |
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| US4222847A (en) * | 1978-12-15 | 1980-09-16 | Gulf Oil Corporation | Coal liquefaction process with improved slurry recycle system |
| JPH01148382A (en) | 1987-12-02 | 1989-06-09 | Hanwa:Kk | Equipment for preventing scattering and diffusion of fine powder of insulating material |
| JP4045229B2 (en) * | 2003-10-15 | 2008-02-13 | 株式会社神戸製鋼所 | Production method of ashless coal |
| JP4805802B2 (en) * | 2006-12-13 | 2011-11-02 | 株式会社神戸製鋼所 | Method and apparatus for producing solid fuel |
| JP5334433B2 (en) * | 2008-03-19 | 2013-11-06 | 株式会社神戸製鋼所 | Production method of ashless coal |
| JP4708463B2 (en) * | 2008-09-29 | 2011-06-22 | 株式会社神戸製鋼所 | Production method of ashless coal |
| JP4660608B2 (en) * | 2009-06-22 | 2011-03-30 | 株式会社神戸製鋼所 | Carbon material manufacturing method |
| US8093306B2 (en) * | 2010-12-22 | 2012-01-10 | Rentech, Inc. | Integrated biorefinery for production of liquid fuels |
| JP2012172076A (en) * | 2011-02-22 | 2012-09-10 | Mitsubishi Heavy Ind Ltd | Coal upgrading system, dewatering system of carbon-containing substance, and solvent circulation system for upgrading of carbon-containing substance |
| JP2013249360A (en) * | 2012-05-31 | 2013-12-12 | Kobe Steel Ltd | Method for producing ashless coal |
-
2013
- 2013-12-25 JP JP2013267439A patent/JP5982666B2/en active Active
-
2014
- 2014-12-09 AU AU2014371509A patent/AU2014371509B2/en active Active
- 2014-12-09 CN CN201480066265.XA patent/CN105793399B/en active Active
- 2014-12-09 CA CA2928393A patent/CA2928393A1/en not_active Abandoned
- 2014-12-09 KR KR1020167016514A patent/KR101822772B1/en active IP Right Grant
- 2014-12-09 US US15/034,044 patent/US20160272910A1/en not_active Abandoned
- 2014-12-09 WO PCT/JP2014/082579 patent/WO2015098505A1/en active Application Filing
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3970541A (en) * | 1973-12-17 | 1976-07-20 | Coal Industry (Patents) Limited | Gas extraction of coal |
| US4387015A (en) * | 1982-09-30 | 1983-06-07 | International Coal Refining Company | Coal liquefaction quenching process |
| CN2722997Y (en) * | 2004-07-24 | 2005-09-07 | 李建平 | Device for extracting fat soluble material |
| CN101511977A (en) * | 2006-10-12 | 2009-08-19 | 株式会社神户制钢所 | Method for production of ashless coal |
| CN101918519A (en) * | 2008-01-09 | 2010-12-15 | 株式会社神户制钢所 | Apparatus and process for producing solid fuel |
Also Published As
| Publication number | Publication date |
|---|---|
| JP5982666B2 (en) | 2016-08-31 |
| CA2928393A1 (en) | 2015-07-02 |
| AU2014371509B2 (en) | 2016-12-22 |
| AU2014371509A1 (en) | 2016-06-23 |
| KR101822772B1 (en) | 2018-01-26 |
| CN105793399A (en) | 2016-07-20 |
| WO2015098505A1 (en) | 2015-07-02 |
| JP2015124237A (en) | 2015-07-06 |
| KR20160089438A (en) | 2016-07-27 |
| US20160272910A1 (en) | 2016-09-22 |
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