CN105793399A - Method for producing ashless coal - Google Patents
Method for producing ashless coal Download PDFInfo
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- CN105793399A CN105793399A CN201480066265.XA CN201480066265A CN105793399A CN 105793399 A CN105793399 A CN 105793399A CN 201480066265 A CN201480066265 A CN 201480066265A CN 105793399 A CN105793399 A CN 105793399A
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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
Provided is a method for producing ashless coal, said method comprising a slurry preparation step in which a slurry is prepared by mixing coal and a solvent, the coal that is included in the slurry is dewatered, and the temperature of the slurry is increased. The slurry preparation step comprises a preparation/dewatering step and a preparation/temperature increase step. In the preparation/dewatering step, preparation of the slurry and dewatering of the coal are performed by mixing coal and a liquid solvent that is circulated during a circulation step. In the preparation/temperature increase step, the slurry is prepared and the temperature of the slurry is increased by mixing the slurry with solvent vapor that is circulated during the circulation step.
Description
Technical field
The present invention relates to the manufacture method of a kind of ashless coal.
Background technology
Existed for the manufacture method (such as patent documentation 1) of ashless coal in the past.The manufacture method of the ashless coal recorded in patent documentation 1 is method (claim 1 with reference to document) as described below." manufacture method of a kind of ashless coal, it has: slurry modulating process, solvent and coal is mixed and modulates slurry；Extraction process, is heated the slurry obtained in described slurry modulating process ... and extract the coal composition dissolving in solvent；Separation circuit, separates the coal composition insoluble in solvent from described extraction process in the slurry of gained；What separate from described separation circuit comprising recycling design in the slurry of the coal composition insoluble in solvent and obtaining the operation of ashless coal；With the operation making the solvent being recovered to be circulated in described slurry modulating process.”
Prior art literature
Patent documentation
Patent documentation 1: No. 4045229 publications of Japan Patent
Summary of the invention
Invention to solve the technical problem that
The manufacture method of ashless coal recorded in patent documentation 1 includes as described above " what separate from described separation circuit comprising recycling design in the slurry of the coal composition insoluble in solvent and obtaining the operation of ashless coal " (this operation is set to " ashless coal acquirement operation ").It is high temperature (such as 270 DEG C etc.) that ashless coal obtains institute's recovered solvent in operation.On the other hand, the manufacture method of ashless coal recorded in patent documentation 1 include " slurry of gained in described slurry modulating process is heated ... and extract the extraction process of the coal composition dissolving in solvent ".Before extraction process, the slurry being supplied in extraction process is heated (preheating).For this, it is considered to using the thermal energy obtaining recovered solvent in operation (high temperature side fluid) at the ashless coal heating source as the slurry (low temperature side fluid) being supplied in extraction process.Additionally, it is contemplated that utilize heat exchanger to carry out by the heating to low temperature side fluid of the high temperature side fluid.
But, in the heat exchange adopting heat exchanger, it is necessary between the heat exchanger entrance temperature and the heat exchanger outlet temperature of low temperature side fluid of high temperature side fluid, temperature difference is set.Therefore, in this heat exchange, obtain a part for the thermal energy that institute's recovered solvent (high temperature side fluid) has in operation at ashless coal and will not transfer heat in the slurry (low temperature side fluid) being supplied in extraction process.
For this, it is an object of the invention to provide the manufacture method of a kind of ashless coal, the heat exchange of its heat exchange and slurry and solvent by being effectively taking place coal and solvent such that it is able to effectively utilize the thermal energy of generation in the manufacture process of ashless coal.
For solving the means of technical problem
The manufacture method of the ashless coal of the present invention has: slurry modulating process, coal and solvent is mixed and modulates slurry, and carries out the dehydration of coal contained in above-mentioned slurry and the intensification of above-mentioned slurry；Extraction process, is heated the slurry of gained in above-mentioned slurry modulating process and extracts the coal composition that dissolves in solvent；Separation circuit, by the solid constituent concentrated solution of solution that the pulp separation of gained in above-mentioned extraction process is the coal composition comprising and dissolving in solvent and the concentration of the coal composition insoluble in solvent；Ashless coal obtains operation, and from above-mentioned separation circuit, in isolated solution, evaporation separates solvent and obtains ashless coal；And circulating process, make above-mentioned ashless coal obtain and operation is evaporated the circulation of isolated solvent.Above-mentioned slurry modulating process has: modulation dehydration procedure, is mixed by the solvent liquid that will circulate in above-mentioned circulating process and coal, thus carrying out the modulation of slurry and the dehydration of coal；With modulation heating process, mixed by the solvent vapour that will circulate in above-mentioned circulating process and slurry, thus carrying out modulation and the intensification of slurry.
Invention effect
According to above-mentioned composition, by being effectively taking place the heat exchange of the coal heat exchange with solvent and slurry and solvent, such that it is able to effectively utilize the thermal energy produced in the manufacture process of ashless coal.
Accompanying drawing explanation
Fig. 1 is the schematic diagram that ashless coal manufactures device 1.
Fig. 2 is the schematic diagram of the ashless coal manufacture device 101 of comparative example.
Detailed description of the invention
Ashless coal manufacture device 1 with reference to the Fig. 1 manufacture method to ashless coal and the manufacture method carrying out ashless coal illustrates.
Ashless coal manufactures device 1 and manufactures ashless coal (HPC for removing ash from the coal of raw material (also referred to as " coal ")；Hyper-coal) device.Ashless coal manufactures device 1 and possesses machine 51～91 on coal slurry handling machine 11～37, circulation road 41～46 and circulation road.
Coal slurry handling machine 11～37 is the machine for coal and slurry (aftermentioned) are processed.Coal slurry handling machine 11～37 possesses coal supply pipeline 11 and steam discharging device 13.And then, coal slurry handling machine 11～37 possesses slurry modulation machine 20, preheater 31, extraction tank 33, segregation apparatus 35 and solvent recovery unit 37 successively from the upstream side of the manufacturing process of ashless coal.
Coal supply is modulated machine 20 (coal supply step) to slurry by coal supply pipeline 11.Coal is modulated the modulation dehydration groove 21 (aftermentioned) of machine 20 by coal supply pipeline 11 from (not shown) supply to slurries such as feed appliances.This coal is such as bituminous coal or rudimentary coal (brown coal, ub-bituminous coal).The extraction yield (ratio of the soluble ingredient of the coal being extracted in solvent) of bituminous coal is higher than rudimentary coal.Rudimentary coal is more cheap than bituminous coal.
Steam discharging device 13 purges gas by flowing in coal supply pipeline 11 and in coal supply pipeline 11, middle for modulation dehydration groove 21 (aftermentioned) steam produced is discharged (steam discharge operation).Above-mentioned purging gas is the gas in coal supply pipeline 11 in gaseous state, for instance for nitrogen (purging nitrogen).Steam discharging device 13 is to arrange to suppress the blockage problem of coal supply pipeline 11.Above-mentioned " blockage problem " is likely to produce as described below.Carrying out heating and the dehydration of coal in modulation dehydration groove 21 (aftermentioned), result produces steam.The major part of this steam is steam, and a part for this steam is solvent vapour (solvent of gaseous state).If this steam enters in coal supply pipeline 11, then this steam is cooled and becomes condensed liquid, and this condensed liquid is attached to the inner surface of coal supply pipeline 11.If coal is attached on this condensed liquid, then coal can block coal supply pipeline 11 (making stream narrow and small or completely plugged stream).In that way it is possible to produce above-mentioned " problem of blocking ".Steam discharging device 13 possesses valve 13a and purges gas supply device 13b.
Valve 13a is configured on coal supply pipeline 11.The flowing of the material (coal, steam and purging gas) passing in coal supply pipeline 11 is controlled by the opening and closing of valve 13a.Preferably in coal supply pipeline 11 in series configures multiple (such as 2) valve 13a.When configuring multiple valve 13a on coal supply pipeline 11, compared with the situation only configuring 1, steam more can be suppressed to enter in coal supply pipeline 11.Valve 13a is such as revolving valve.
Purge gas supply device 13b and will purge gas supply (purging gas supply step) to coal supply pipeline 11.When in series configuring 2 valve 13a on coal supply pipeline 11, purge gas supply device 13b and purging gas is supplied between 2 valve 13a.
Coal and solvent are mixed and modulate slurry (coal-solvent slurry) by slurry modulation machine 20, and carry out the dehydration of slurry and heat up (slurry modulating process).
The solvent being supplied in this slurry modulation machine 20 is the solvent making coal dissolve.This solvent is preferably the solvent that the ratio (extraction yield) of the soluble ingredient of coal making to extract in extraction tank 33 is high.From the view point of extraction yield, even if this solvent is preferably also stable in a heated state, and preferably coal is had bigger dissolving power (excellent with the affinity of coal).This solvent is preferably and makes the solvent that the solvent recovering rate in solvent recovery unit 37 is high.From the view point of solvent recovering rate, this solvent is preferably able to utilize the methods such as distillation easily to reclaim.From viewpoints such as the pressure reduction in extraction tank 33 and segregation apparatus 35, the extraction yields in extraction tank 33, the boiling point of solvent is such as preferably 180～300 DEG C, is more preferably 230～280 DEG C.This solvent is such as coal derivative.This solvent is for mainly obtaining solvent from coal carbonization product purification.This solvent is the solvent (aromatic solvent) such as comprising aromatic compound.This solvent be mainly composed of 2 cyclic aromatic series.This 2 cyclic aromatic series is such as naphthalene, methyl naphthalene, dimethylnaphthalene, trimethyl-naphthalene etc..Other compositions of this solvent are be respectively provided with the naphthalene class of aliphatic lateral chain, anthracene class, fluorenes class or they be addition of the alkylbenzene etc. of xenyl, long-chain fat race side chain.Specifically, for instance, this solvent is methylnaphthalene oil, naphtalene oil etc..The distilled oil as by-product oil when methylnaphthalene oil, naphtalene oil are that the dry distillation of coal manufactures coke.Slurry modulation machine 20 possesses modulation dehydration groove 21 and modulation intensification machine 23.
Modulation dehydration groove 21 carries out the modulation of slurry and the dehydration (modulation dehydration procedure) of coal by solvent liquid (solvent of liquid condition) and coal being mixed.Supply to the solvent liquid modulating dehydration groove 21 is by circulating the solvent liquid that the part on road 41～46 circulates.Supply to the coal modulating dehydration groove 21 supplies from coal supply pipeline 11.The mixing of solvent liquid and coal in modulation dehydration groove 21 is such as undertaken by being put into by coal in the solvent liquid in modulation dehydration groove 21.By modulating the mixing of the solvent liquid in dehydration groove 21 and coal, thus modulating slurry.S/C (the Slurry/Coal of the slurry of modulation in modulation dehydration groove 21；The quality of slurry is relative to the mass ratio of the coal of drying regime) it is such as about 2.0.
This modulation dehydration groove 21 carries out the dehydration of coal in such a way.Modulation dehydration groove 21 makes solvent liquid directly contact with coal by being mixed with coal by solvent liquid.Modulation dehydration groove 21 is directly contacted by this and makes to be made directly heat exchange between solvent liquid and coal.Modulation dehydration groove 21 makes coal heat up and make the moisture (water containing coal) in coal evaporate by this heat exchange.Supply is the boiling point carrying out more than the temperature needed for this dehydration and not enough solvent to the temperature of the solvent liquid modulating dehydration groove 21.Supply is such as more than 230 DEG C to the temperature of the solvent liquid modulating dehydration groove 21, is preferably more than 235 DEG C, and is such as less than 240 DEG C.Supply is 237 DEG C (following, with reference to Fig. 1, the concrete example of temperature to be illustrated) to the temperature of the solvent liquid modulating dehydration groove 21 in the example depicted in figure 1.
Modulation intensification machine 23 is by mixing solvent vapour and slurry and carry out the modulation of slurry and heat up (modulation heating process).Modulation intensification machine 23 regulates the concentration of slurry according to the entrance concentration of extraction tank 33.The entrance concentration of extraction tank 33 is set in advance.Without being arranged to regulate the machine of the concentration of slurry between modulation intensification machine 23 and extraction tank 33, manufacturing in device 1 at ashless coal does not have this kind of machine.In modulation intensification machine 23, the S/C of the slurry of modulation is such as about 4.0.Till modulation intensification machine 23 makes slurry be warming up to the inlet temperature of machine (being called " after slurry modulation machine ") that then slurry modulation machine 20 supplies slurry.The inlet temperature of " after slurry modulation machine " is set in advance." after slurry modulation machine " is specially preheater 31, when being not provided with preheater 31, for extraction tank 33.Without being arranged to regulate the machine of the temperature of slurry between modulation intensification machine 23 and " after slurry modulation machine ", manufacturing in device 1 at ashless coal does not have this kind of machine.Modulation intensification machine 23 possesses Venturi scrubber 23a and modulation intensification groove 23b.
Solvent vapour and slurry are mixed (the first modulation heating process) by Venturi scrubber 23a.Supply is by circulating the solvent vapour that the part (details is as described later) on road 41～46 circulates to the solvent vapour of Venturi scrubber 23a.Supply supplies to the slurry of Venturi scrubber 23a from modulation dehydration groove 21.Supplying to the slurry of Venturi scrubber 23a is be modulated in modulation dehydration groove 21 and slurry after dehydration.Venturi scrubber 23a makes slurry directly contact with solvent vapour by being mixed with solvent vapour by slurry.Venturi scrubber 23a is directly contacted by this and makes to be made directly between solvent vapour and slurry heat exchange.Venturi scrubber 23a utilizes the latent heat (heat release when utilizing solvent vapour condensing) of solvent vapour that slurry is heated.When being not fully complete the dehydration of coal in modulating dehydration groove 21, Venturi scrubber 23a carries out the dehydration of the coal in slurry by slurry is heated.Venturi scrubber 23a makes slurry become microgranular, and microgranular slurry and solvent vapour is mixed.Microgranular slurry and solvent vapour are mixed by Venturi scrubber 23a by making the flow velocity of microgranular slurry and solvent vapour increase and to make microgranular slurry produce shearing force with solvent vapour.It is explained, it is possible to replace Venturi scrubber 23a or use the device (the first modulation heat riser) except Venturi scrubber solvent vapour and slurry mixed on this basis.Above-mentioned " device except Venturi scrubber " includes such as static mixer.Static mixer utilizes the element (component of shape after being distorted by plate, spiral helicine component) of the inside being configured at pipe microgranular slurry and solvent vapour be stirred and mix.
The mixture of mixing in Venturi scrubber 23a is carried out mixing (the second modulation heating process) by modulation intensification groove 23b further.Modulation intensification groove 23b makes slurry and the further heat exchange of solvent by this mixing.To pressurize to modulating in intensification groove 23b in the way of the gasification (solvent vapour damage) that can suppress solvent, for instance pressurize with 50kPaG.
The slurry modulated (in slurry modulation machine 20) in modulation intensification machine 23 was heated (preheating procedure) in supply in advance by preheater 31 before extraction tank 33.It is explained, it is also possible to there is no preheater 31.
Extraction tank 33 extracts the coal composition (solvent-soluble composition) (extraction process) dissolving in solvent by the slurry of gained in slurry modulation machine 20 is heated.Extraction tank 33 extracts the organic principle in coal.The details of this extraction is as described below.For the slurry of supply to extraction tank 33, the blender being arranged at extraction tank 33 is utilized to be stirred, while heating is maintained at set point of temperature (aftermentioned).Thus, from slurry extractant soluble ingredient.But, extract not only comprises solvent-soluble composition, also comprises the composition (solvent insoluble component) (such as ash grades) insoluble in solvent.
The heating-up temperature of the slurry in this extraction tank 33 is the temperature enabling solvent-soluble composition to be dissolved in solvent.Specifically, the heating-up temperature of slurry is such as more than 300 DEG C, is preferably more than 360 DEG C.The heating-up temperature of slurry is such as less than 420 DEG C, is preferably less than 400 DEG C.When the heating-up temperature of slurry is less than 300 DEG C, go back and insufficient for the intermolecular combination weakening coal, the therefore solvent-soluble composition meltage step-down to solvent.When the heating-up temperature of slurry is more than 420 DEG C, the pyrolysis of coal comes to life, cause generate thermal decomposition free radical in conjunction with, therefore solvent-soluble composition extraction yield reduce.
The extraction carried out in this extraction tank 33 carries out under the existence preferably in inactive gas (such as preferably cheap nitrogen).In order to carry out this extraction, it is necessary to solvent to be limited to liquid phase (not making solvent volatilize).In order to solvent is limited to liquid phase, it is necessary to make the vapour pressure higher than solvent of the pressure (to solvent and the pressure of slurry applying, operation pressure) in extraction tank 33.Temperature when pressure in extraction tank 33 additionally depends on extraction, the solvent used vapour pressure, but be preferably 1.0～2.0MPa.
Segregation apparatus 35 is by the solid constituent concentrated solution (underflow (underflow)) (separation circuit) of solution (solution portion, supernatant, overflow) that the pulp separation of gained in extraction tank 33 is the coal composition comprising and dissolving in solvent and the concentration of the coal composition insoluble in solvent.The method of this separation is such as settling methods, Filtration or centrifugal separation etc..Settling methods is by being held in groove by slurry and utilizing gravity to make the sedimentation of solvent insoluble component be separated into solution and the mode of solid constituent concentrated solution.Hereinafter, situation about the extraction and application settling methods in segregation apparatus 35 being carried out illustrates.To being incubated (or heating) and pressurization in segregation apparatus 35.This insulation (or heating) and pressurization are to prevent from carrying out from the precipitating out again of solvent-soluble composition of coal dissolution.Temperature in segregation apparatus 35 is such as 300～380 DEG C.Pressure in segregation apparatus 35 is such as 1.0～3.0MPa.Segregation apparatus 35 is such as 2 segmentations (quantity of gravitation settler is 2).The segregation apparatus 35 of 2 segmentations possesses the first gravitation settler 35a and the second gravitation settler 35b.Being explained, segregation apparatus 35 can be 1 segmentation (quantity of gravitation settler is 1).It is explained, segregation apparatus 35 is completely separated into supernatant and solid constituent concentrated solution is ideal, but sometimes also can be mixed into solid constituent (the coal composition insoluble in solvent) in a part for supernatant or be mixed into supernatant in the part of solid constituent concentrated solution.
Solvent recovery unit 37 is recycling design from solution isolated segregation apparatus 35.Solvent recovery unit 37 is the device for obtaining ashless coal, extract residue (aftermentioned) from the solution separated segregation apparatus 35.Solvent recovery unit 37 possesses the first solvent recovery unit 37a and the second solvent recovery unit 37b.
First solvent recovery unit 37a is for being used for evaporating the device (obtaining the device of operation for carrying out ashless coal) separating solvent and obtain ashless coal (HPC) from segregation apparatus 35 in isolated solution.Ashless coal is entirely without moisture and the coal being practically free of ash.Ash contained in ashless coal is below 5 weight %, is preferably below 3 weight %.The caloric value of ashless coal is higher than feed coal, and ignitability, complete flammability are good, and therefore the high efficiency fuel as such as boiler etc. uses.The mobility (softening meltbility) of ashless coal is higher than feed coal, uses as the raw material of such as ferrum coke processed or a part (mixed coal) for raw material.
The method that the evaporation of the solvent carried out in this first solvent recovery unit 37a separates includes the such as way of distillation, evaporation etc..Evaporation includes such as spray drying method etc..The way of distillation includes such as flash method, Thin film evaporation techniques etc..Such as, the first solvent recovery unit 37a is for carrying out the flash tank of flash method (flasher).It addition, such as, the first solvent recovery unit 37a is the membrane distillation groove for carrying out Thin film evaporation techniques.It addition, such as, the first solvent recovery unit 37a is the device possessing flash tank and membrane distillation groove (being configured at the such as downstream of flash tank).
(flash method)
The evaporation adopting the solvent of flash method separates and carries out in such a way.Make in the pressure ratio segregation apparatus 35 in flash tank low (such as 70kPaG).Like this, the solution separated in segregation apparatus 35 is ejected in flash tank.And, the solvent in solution evaporates separation from solution.
(Thin film evaporation techniques)
The evaporation adopting the solvent of Thin film evaporation techniques separates and carries out in such a way.The solution separated in segregation apparatus 35 is directed in membrane distillation groove.And, it is contained in the curette in membrane distillation groove (also referred to as wiper) by forming the thin film of distillation object (solution separated in segregation apparatus 35) at the inwall of membrane distillation groove and carries out continuous still.Pressure in membrane distillation groove is such as 0.1MPaG.In order to make solvent suitably evaporate in membrane distillation groove, and the wall of membrane distillation groove is heated.The heating of the wall of membrane distillation groove can utilize such as deep fat to carry out, it is also possible to utilizes such as electric heater to carry out.In when the adding heat utilization deep fat to carry out of wall of membrane distillation groove, sleeve pipe (coil serving) is set in the inner side of wall of membrane distillation groove and outside (it addition, the side in such as inner side and outside).Deep fat is flowed in this sleeve pipe.The wall of membrane distillation groove is heated by result.The heating of the wall of membrane distillation groove needs such as situations below.First solvent recovery unit 37a has the membrane distillation groove in the downstream of flash tank and flash tank sometimes.Now, the distillation in flash tank is utilized to make the temperature of solution reduce.Therefore, in order to make solvent suitably evaporate in membrane distillation groove, and the heating of the wall of membrane distillation groove is carried out.
Second solvent recovery unit 37b is that in the solid constituent concentrated solution for separating from segregation apparatus 35, evaporation separation solvent obtains extract residue (RC；Residuecoal) device (obtaining the device of operation for carrying out extract residue) (also referred to as residual coal).Extract residue is the coal of solvent insoluble component (ash grades) concentration, and the part as the mixed coal of the raw material of such as coke uses.The method that evaporation with the solvent in the first solvent recovery unit 37a separates is same, and the method that the evaporation of the solvent in the second solvent recovery unit 37b separates includes the way of distillation, evaporation etc..It is explained, it is also possible to be not provided with the second solvent recovery unit 37b.
Circulation road 41～46 makes to be evaporated the solvent separated in solvent recovery unit 37 grade and is circulated (circulating process).Circulation road 41～46 is for solvent carries out the stream (pipe arrangement) recycled.Circulation road 41～46 possesses the first circulation road 41, second and circulates circulation road, circulation road the 44, the 5th, circulation road the 43, the 4th, road the 42, the 3rd 45 and the 6th circulation road 46.
First circulation road 41 makes to be evaporated the solvent separated in the first solvent recovery unit 37a and is circulated (the first circulating process) in modulation dehydration groove 21.The solvent taken out from the top of the first solvent recovery unit 37a is imported in modulation dehydration groove 21 by the first circulation road 41.
Second circulation road 42 makes to be evaporated the solvent separated in the first solvent recovery unit 37a and is circulated (the second circulating process) in modulation intensification machine 23.Second circulation road 42 makes to be evaporated the solvent separated in the first solvent recovery unit 37a and is circulated in Venturi scrubber 23a.Second circulation road 42 makes to be evaporated the solvent separated in the first solvent recovery unit 37a and is directly circulated in (not carrying out recuperation of heat or intensification) Venturi scrubber 23a.Pipe arrangement crushing (such as 20kPaG) in second circulation road 42 is equal with the operation pressure (such as 70kPaG) in the first solvent recovery unit 37a with operation pressure (such as 50kPaG) sum in Venturi scrubber 23a.Therefore, the operation pressure in the first solvent recovery unit 37a is set based on the pipe arrangement crushing sum in the operation pressure in Venturi scrubber 23a and the second circulation road 42.
3rd circulation road 43 makes to be evaporated the solvent separated in the first solvent recovery unit 37a and is circulated (the 3rd circulating process) in segregation apparatus 35.3rd circulation road 43 makes to be evaporated the solvent separated in the first solvent recovery unit 37a and is circulated in the second gravitation settler 35b.By circulating road 43 to the second gravitation settler 35b donor solvent (high-temperature solvent condensed liquid) from the 3rd, thus providing the solvent quantity delivered needed for the second gravitation settler 35b.
4th circulation road 44 makes to be evaporated the solvent separated in the second solvent recovery unit 37b and is circulated (the 4th circulating process) in modulation dehydration groove 21.The solvent taken out from the top of the second solvent recovery unit 37b is imported in modulation dehydration groove 21 by the 4th circulation road 44.It is explained, imports from the second solvent recovery unit 37b the steam on the 4th circulation road 44 and not only comprise solvent but also comprise nitrogen.
5th circulation road 45 makes the steam produced in slurry modulation machine 20 be circulated (the 5th circulating process) in modulation dehydration groove 21.The steam produced in slurry modulation machine 20 comprises solvent and water, compared with solvent, comprises more water.5th circulation road 45 makes the steam produced in modulation dehydration groove 21 be circulated in modulation dehydration groove 21.5th circulation road 45 makes the steam produced in modulation intensification groove 23b be circulated in modulation dehydration groove 21.It is explained, Fig. 1 modulates at slurry " A " part recorded in the left of cooler 81 in " A " part and this figure of recording above machine 20 and is associated.
6th circulation road 46 makes the solvent vapour produced in extraction tank 33 be circulated (the 6th circulating process) in modulation dehydration groove 21.
Circulation road on machine 51～91 be configured at circulation road 41～46 on (except second circulation road 42 on except) machine.On circulation road, machine 51～91 includes following machine.The machine being configured on the first circulation road 41 includes recycling design groove 51.The machine being configured on the 3rd circulation road 43 includes heat extraction recovery boiler 61, heat exchanger 63 and preheater 65 successively from upstream side.The machine being configured on the 4th circulation road 44 includes bag filter 71, heat extraction recovery boiler 73, cooler 75, heat exchanger 77 and recycling design groove 51 successively from upstream side.The machine being configured on the 5th circulation road 45 includes cooler 81, oil-water separation tank 83, heat exchanger 77 and recycling design groove 51 successively from upstream side.The machine being configured on the 6th circulation road 46 includes oil heating device 91, heat exchanger 63, heat exchanger 77, oil-water separation tank 83, heat exchanger 77 and recycling design groove 51 successively from upstream side.
Recycling design groove 51 modulation is for the solvent liquid (solvent liquid modulating process) to modulation dehydration groove 21 supply.Supply to the solvent of recycling design groove 51 be the solvent (solvent vapour) passing into the first circulation road 41, more specifically, by the solvent vapour of institute's evaporation separation in the first solvent recovery unit 37a.First solvent recovery unit 37a is evaporated the solvent vapour directly (not carrying out recuperation of heat or intensification) separated supply to recycling design groove 51.It addition, supply is to the solvent that solvent is circulation road, inflow the 4th circulation road the 44, the 5th 45 and the 6th circulation road 46 of recycling design groove 51, more specifically, for the solvent liquid after utilizing heat exchanger 77 (aftermentioned) to carry out heat exchange.
Heat extraction recovery boiler 61 reclaims the heat (the 3rd circulation road heat extraction recovery process) of the solvent flowing into the 3rd circulation road 43.Supply to the solvent of heat extraction recovery boiler 61 be the solvent (solvent vapour) passing into the 3rd circulation road 43, more specifically, by the solvent vapour of institute's evaporation separation in the first solvent recovery unit 37a.First solvent recovery unit 37a is evaporated the solvent vapour separated and is directly fed to heat extraction recovery boiler 61.Heat extraction recovery boiler 61 utilizes supply to manufacture saturated vapor (steam) to the thermal energy of the solvent of heat extraction recovery boiler 61.Heat extraction recovery boiler 61 makes supply reduce to the temperature of the solvent vapour of heat extraction recovery boiler 61, and makes this solvent vapour condensing.Heat extraction recovery boiler 61 manufactures the saturated vapor of such as 2.2MPaG with the speed of such as 19.30t/h.It is explained, it is possible to the heat extraction recovery boiler 61 heat extraction and recovery device except boiler is replaced.This point can be replaced to use too for heat extraction recovery boiler 73 grade described later with the heat extraction and recovery device except boiler.Heat extraction and recovery device except boiler include such as deep fat is heated device (with reference to described later oil heating device 91) etc..
Heat exchanger 63 makes the solvent that inflow the 3rd circulates road 43 heat up (the 3rd circulation road heating process).Supply the solvent that low temperature side fluid (fluid of the side being warmed) is inflow the 3rd circulation road 43 to heat exchanger 63, more specifically, for the solvent liquid after heat exchange in heat extraction recovery boiler 61.Supply the solvent that high temperature side fluid (fluid of the side being warmed) is inflow the 6th circulation road 46 to heat exchanger 63, more specifically, for the solvent (solvent vapour) after recuperation of heat in oil heating device 91 (aftermentioned).
The solvent flowing into the 3rd circulation road 43 was heated (the 3rd circulation road preheating procedure) in advance by preheater 65 before supply to segregation apparatus 35.Supply is the solvent (solvent liquid) after utilizing heat exchanger 63 to carry out heat exchange to the solvent of preheater 65.It is temperature required that preheater 65 makes that solvent is warming up in segregation apparatus 35 (the second gravitation settler 35b).
The solvent etc. flowing into the 4th circulation road 44 is filtered (filter progress) by bag filter 71.Supply to bag filter 71 solvent by the second solvent recovery unit 37b institute evaporation separation solvent (solvent vapour).
The heat flowing into the solvent on the 4th circulation road 44 is carried out reclaiming (the 4th circulation road heat extraction recovery process) by heat extraction recovery boiler 73.Supply is the solvent (solvent vapour) utilizing bag filter 71 to be filtered to the solvent of heat extraction recovery boiler 73.Heat extraction recovery boiler 73 utilizes the thermal energy of solvent to manufacture saturated vapor.Heat extraction recovery boiler 73 manufactures the saturated vapor of such as 0.70MPaG with the speed of such as 6.03t/h.
The solvent flowing into the 4th circulation road 44 is carried out cooling down (the 4th circulation road refrigerating work procedure) by cooler 75.Cooler 75 uses such as cooling water that solvent is cooled down.Supply is by the solvent (solvent vapour) of heat extraction recovery boiler 73 recuperation of heat to the solvent of cooler 75.Cooler 75 is fed to the solvent vapour cooling of cooler 75 and makes it condensing.
Heat exchanger 77 is that the solvent flowing into the 4th circulation road 44 heats up (the 4th circulation road heating process).Heat exchanger 77 is that the solvent flowing into the 5th circulation road 45 heats up (the 5th circulation road heating process).Heat exchanger 77 makes the solvent that inflow the 6th circulates road 46 heat up (the 6th circulation road heating process).Supply the solvent that low temperature side fluid is inflow the 4th circulation road 44 to heat exchanger 77, more specifically, for the solvent (solvent liquid) after utilizing cooler 75 to cool down.Supply the solvent that low temperature side fluid is inflow the 5th circulation road 45 and the 6th circulation road 46 to heat exchanger 77, more specifically, for the solvent (solvent liquid) after oil-water separation in oil-water separation tank 83 (aftermentioned).Supply to the high temperature side fluid of heat exchanger 77 be the solvent flowing into the 6th circulation road 46, more specifically, for utilizing heat exchanger 63 to carry out after heat exchange and solvent (solvent vapour) before oil-water separation in oil-water separation tank 83.
The steam (comprising the steam of solvent and water as described above) flowing into the 5th circulation road 45 is carried out cooling down (the 5th circulation road refrigerating work procedure) by cooler 81.Cooler 81 uses such as cooling water to be cooled down by steam.Steam is cooled down and makes it condensing by cooler 81.
Oil-water separation tank 83 is from flowing into the 5th fluid separation solvent (oil) circulating road 45 grade and water (oil-water separation operation).Supply the fluid that fluid is inflow the 5th circulation road 45 to oil-water separation tank 83, more specifically, for the liquid after utilizing cooler 81 to cool down.Supply to the fluid of oil-water separation tank 83 be the fluid flowing into the 6th circulation road 46, more specifically, for utilizing the solvent (solvent liquid) after heat exchanger 77 heat exchange.The water separated in oil-water separation tank 83 is as waste water (WW；Wastewater) discharge from oil-water separation tank 83.
Oil heating device 91 utilizes the thermal energy of the solvent (solvent vapour) flowing into the 6th circulation road 46 to make deep fat heat up (oil heating process).Supply is the solvent vapour produced in extraction tank 33 to the solvent of oil heating device 91.The deep fat that oil heating device 91 heats up utilizes as the thermal source of other operations.This deep fat utilizes as the thermal source of such as solvent recovery unit 37.This deep fat is such as described above for the heating of the wall of the membrane distillation groove of solvent recovery unit 37.It is explained, it is possible to the oil heating device 91 heat extraction and recovery device (such as boiler etc.) except the device making deep fat heat up is replaced.
(ashless coal of comparative example manufactures device 101)
In order to carry out the comparison etc. of " comparison of practical amount " described later, the ashless coal manufacture device 101 of the comparative example shown in Fig. 2 is illustrated.Ashless coal manufactures device 101 and manufactures the difference (comparison of practicality amount is had influential difference) of device 1 (with reference to Fig. 1) as shown in following [difference a]～[difference e] with ashless coal.It is explained, ashless coal is manufactured device 101 and manufactures, with ashless coal, the composition labelling same symbol that device 1 (with reference to Fig. 1) is total.
[difference a]
Ashless coal shown in Fig. 1 manufactures device 1 and possesses modulation dehydration groove 21 and modulation intensification machine 23.Replacing, the ashless coal shown in Fig. 2 manufactures device 101 and possesses slurry preparation vessel 121, dehydration groove 122 and intensification groove 123 from upstream side successively.Coal and solvent are mixed by slurry preparation vessel 121 modulates slurry.Coal in the dehydration groove 122 slurry to modulating in slurry preparation vessel 121 carries out dehydration.Intensification groove 123 makes the slurry intensification in dehydration groove 122 after dehydration.
[difference b]
Ashless coal manufacture device 1 shown in Fig. 1 possesses the ashless coal manufacture device 101 shown in steam discharging device 13, Fig. 2 on coal supply pipeline 11 and does not possess steam discharging device 13 (with reference to Fig. 1).Therefore, it is impossible to suppress " blockage problem " (above-mentioned) of coal supply pipeline 11 in steam discharging device 13.Therefore, in order to avoid the evaporation of the moisture in coal at slurry preparation vessel 121, and the solvent being fed to slurry preparation vessel 121 carries out cooling down (such as 107 DEG C).Specifically, utilize the composition of following [difference c]～[difference e] and operation that solvent is cooled down.
[difference c]
Ashless coal manufactures device 101 and possesses the first circulation road 141.First circulation road 141 for manufacturing the first circulation road 41 of device 1 and the stream that the second circulation road 42 is corresponding with the ashless coal shown in Fig. 1.The first circulation road 141 shown in Fig. 2 is for for supplying the solvent vapour of institute's evaporation separation in the first solvent recovery unit 37a to the stream of slurry preparation vessel 121.Circulate first and road 141 configures successively dehydration groove 122 and intensification groove 123 from upstream side.First circulation road 141 makes to be evaporated the solvent (solvent vapour) separated in the first solvent recovery unit 37a and flows into dehydration groove 122 and intensification groove 123.Thus, flow into the slurry in the first solvent circulating road 141 and dehydration groove 122 and in intensification groove 123 and indirectly carry out heat exchange.That is, as the heating source of the dehydration of the slurry in dehydration groove 122 and intensification groove 123 and intensification, it is used in the first solvent recovery unit 37a being evaporated the thermal energy of the solvent vapour separated.
[difference d]
Ashless coal manufactures device 101 and possesses heat extraction recovery boiler 153 and cooler 155.Heat extraction recovery boiler 153 and cooler 155 are configured at the first circulation road 141.Heat extraction recovery boiler 153 utilizes the thermal energy of the solvent (solvent liquid) in intensification groove 123 after heat exchange to manufacture saturated vapor.Heat extraction recovery boiler 153 manufactures the saturated vapor of 0.50MPaG with the speed of 8.18t/h.Solvent (solvent liquid) after recuperation of heat in heat extraction recovery boiler 153 is used cooling water to cool down by cooler 155.
[difference e]
Ashless coal manufactures device 101 and possesses heat extraction recovery boiler 193 and cooler 195.Heat extraction recovery boiler 193 and cooler 195 are configured on the 6th circulation road 46.Manufacturing in device 101 at ashless coal, the 6th circulation road 46 makes the steam produced in extraction tank 33 be circulated in slurry preparation vessel 121.Heat extraction recovery boiler 193 utilizes the thermal energy of the solvent (solvent vapour) after making deep fat heat up in oil heating device 91 to manufacture saturated vapor.Heat extraction recovery boiler 193 manufactures the saturated vapor of 0.5MPaG with the speed of 1.72t/h.Solvent (solvent liquid) after recuperation of heat in heat extraction recovery boiler 193 is used cooling water to cool down by cooler 195.Being explained, ashless coal manufactures the heat extraction recovery boiler 73 of device 101 and manufactures the saturated vapor of 0.50MPaG with the speed of 6.88t/h.
(comparison of practical amount)
The manufacture method (using the ashless coal shown in Fig. 1 to manufacture the situation of device 1) of the ashless coal of present embodiment is as follows relative to the practicality amount of the manufacture method of the ashless coal of comparative example (using ashless coal to manufacture the situation of device 101).
Saturated vapor generating capacity: increase about 50%
Cooling water makes consumption: cut down about 30wt%
(saturated vapor generating capacity)
Ashless coal shown in Fig. 1 manufactures the total amount that saturated vapor generation amount is the saturated vapor manufactured by heat extraction recovery boiler 61 and heat extraction recovery boiler 73 in device 1.Ashless coal shown in Fig. 2 manufactures the total amount that saturated vapor generation amount is the saturated vapor manufactured by heat extraction recovery boiler 153, heat extraction recovery boiler 193 and heat extraction recovery boiler 73 in device 101.From above-mentioned comparative result: when using the ashless coal shown in Fig. 1 to manufacture device 1, compared with comparative example, it is possible to make the vapor volume that can reclaim in heat extraction recovery boiler increase.
(cooling water makes consumption)
Ashless coal manufactures the cooling water in device 1 makes consumption be the total amount that the cooling water in cooler 75 and cooler 81 makes consumption.Ashless coal shown in Fig. 2 manufactures the cooling water in device 101 makes consumption be the total amount that the cooling water in cooler 155, cooler 195 and cooler 75 makes consumption.From above-mentioned comparative result: when using the ashless coal shown in Fig. 1 to manufacture device 1, compared with comparative example, it is possible to that cuts down the cooling water that uses in cooler makes consumption.Result: compared with comparative example, it is possible to cut down ashless coal and manufacture the operating cost of device 1.
(effect)
Then, the effect of the manufacture method of the ashless coal adopting present embodiment is illustrated.Hereinafter, machine (machine corresponding with each operation) the labelling parantheses after the title of operation that will use to carry out each operation.
(effect 1)
The manufacture method (ashless coal manufactures device 1) of ashless coal has slurry modulating process (slurry modulation machine 20), extraction process (extraction tank 33), separation circuit (segregation apparatus 35), ashless coal acquirement operation (the first solvent recovery unit 37a) and circulating process (the first circulation road 41, the second circulation road 42).Slurry modulating process (slurry modulation machine 20) is for mixing coal and solvent and modulate slurry, and carries out the dehydration of slurry and the operation of intensification.Extraction process (extraction tank 33) extracts the operation of the coal composition dissolving in solvent for the slurry of gained in slurry modulating process (slurry modulation machine 20) is heated.Separation circuit (segregation apparatus 35) is by the operation of solution that the pulp separation of gained in extraction process (extraction tank 33) is the coal composition comprising and dissolving in solvent and the solid constituent concentrated solution of the concentration of the coal composition insoluble in solvent.Ashless coal obtains the operation that operation (the first solvent recovery unit 37a) obtains ashless coal for the solution evaporation separation solvent that separates from separation circuit (segregation apparatus 35).Circulating process (the first circulation road 41, the second circulation road 42) for make ashless coal obtain in operation (the first solvent recovery unit 37a) the operation that is circulated of the solvent of evaporation separation.Slurry modulating process (slurry modulation machine 20) has modulation dehydration procedure (modulation dehydration groove 21) and modulation heating process (modulation intensification machine 23).
[constituting 1-1]
Modulation dehydration procedure (modulation dehydration groove 21) is for by carrying out the modulation of slurry and the operation of the dehydration of coal by the solvent liquid circulated in circulating process (the first circulation road 41) and coal mixing.
[constituting 1-2]
Modulation heating process (modulation intensification machine 23) is for by carrying out the modulation of slurry and the operation of intensification by the solvent vapour circulated in circulating process (the second circulation road 42) and slurry mixing.
The modulation dehydration procedure (modulation dehydration groove 21) of above-mentioned [constituting 1-1] carries out the mixing of solvent and coal.Owing to utilizing this mixing to make solvent directly contact with coal, therefore solvent and coal are made directly heat exchange.It addition, carry out the mixing of solvent and slurry in the modulation heating process (modulation intensification machine 23) of above-mentioned [constituting 1-2].Owing to utilizing this mixing to make solvent directly contact with slurry, therefore solvent and slurry are made directly heat exchange.Compared with the heat exchange of indirect (such as using the heat exchange of heat exchanger), the efficiency of the heat exchange of these substantivities is better.Specifically, such as, in the heat exchange using heat exchanger, it is necessary between the heat exchanger entrance temperature and the heat exchanger outlet temperature of low temperature side fluid (fluid of the side being warmed) of high temperature side fluid (fluid of the side being warmed), temperature difference is set.On the other hand, in the direct heat exchange that above-mentioned [constituting 1-1] and [constituting 1-2] carry out, it is possible to above-mentioned temperature difference is considered as zero.Therefore, it can be effectively taking place the heat exchange (this effect is set to [effect 1-1]) of the coal heat exchange with solvent and slurry and solvent.
And then, in the modulation dehydration procedure (modulation dehydration groove 21) of above-mentioned [constituting 1-1], solvent liquid (liquid) and coal (solid) are mixed.The same solvent vapour of the heat exchange (gas) of solvent liquid (liquid) and coal (solid) is with the heat exchange phase specific efficiency of coal (solid) more preferably.It addition, in the modulation heating process (modulation intensification machine 23) of above-mentioned [constitute 1-2], solvent vapour (gas) and the slurry mixture of liquid (solid with) are mixed.The same solvent vapour of the heat exchange (gas) of solvent vapour (gas) and the slurry mixture of liquid (solid with) is with the heat exchange phase specific efficiency of coal (solid) more preferably.Therefore, by above-mentioned [constituting 1-1] and [constituting 1-2], it is possible to be effectively taking place the heat exchange (this effect is set to [effect 1-2]) of the coal heat exchange with solvent and slurry and solvent.By above-mentioned [effect 1-1] and [effect 1-2], it is possible to effectively utilize the thermal energy produced in the manufacture process of ashless coal.
(effect 2)
[constituting 2]
According to the entrance concentration as extraction process (extraction tank 33), entrance concentration set in advance regulates the concentration of slurry to modulation heating process (modulation intensification machine 23).
By above-mentioned [constituting 2], it is not necessary to the concentration of adjustment slurry (between modulation intensification machine 23 and extraction tank 33) after modulation heating process and before extraction process.Therefore, compared with the situation needing to be arranged to regulate after extraction process and before extraction process the machine of the concentration of slurry, it is possible to cut down number of machines.Result can cut down the equipment cost of the equipment (ashless coal manufactures device 1) of the manufacture method carrying out ashless coal.
(effect 3)
[constituting 3]
Till modulation heating process (modulation intensification machine 23) makes slurry be warming up to inlet temperature and the inlet temperature set in advance of the then operation (such as preheater 31) that slurry modulating process (slurry modulation machine 20) carries out.
By above-mentioned [constitute 3], it is not necessary to after modulation heating process and before the operation that then slurry modulating process carries out, (modulation intensification machine 23 and such as between preheater 31) regulates the temperature of slurry.Therefore, compared with the situation of the machine of the temperature regulating slurry before the operation that needs are arranged to after modulating heating process and then slurry modulating process carries out, it is possible to cut down number of machines.Result can cut down the equipment cost of the equipment (ashless coal manufactures device 1) of the manufacture method carrying out ashless coal.
(effect 4)
[constituting 4]
Solvent vapour and the mixing of slurry in modulation heating process (modulation intensification machine 23) utilize Venturi scrubber 23a to carry out.
The Venturi scrubber 23a of above-mentioned [constituting 4] reliably carries out the mixing of solvent vapour (gas) and slurry (mixture of solid and liquid).Therefore, it can the heat exchange being more effectively carried out solvent vapour with slurry.
(effect 5)
The manufacture method (ashless coal manufactures device 1) of ashless coal has coal supply step (coal supply pipeline 11) and steam discharges operation (steam discharging device 13).The coal supply step (the coal supply pipeline 11) operation for being undertaken by coal supply pipeline 11 supplying by (the supplying to slurry modulation machine 20) that use in slurry modulating process coal.
[constituting 5]
Steam discharge operation (steam discharging device 13) is for modulating dehydration procedure (modulating dehydration groove 21) the middle steam the produced operation from the interior discharge of coal supply pipeline 11 by flowing into purging gas in coal supply pipeline 11.
By above-mentioned [constituting 5], it is possible to suppress the steam in coal supply pipeline 11 to become condensed liquid.Therefore, coal is attached to this condensed liquid, such that it is able to suppress the blocking of coal supply pipeline 11.It addition, by above-mentioned [constituting 5], it is possible to suppress the steam in coal supply pipeline 11 to become condensed liquid, therefore without preventing the generation of steam in modulation dehydration procedure (modulation dehydration groove 21).It is therefore not necessary to the solvent being fed to modulation dehydration procedure (modulation dehydration groove 21) is cooled to the degree not producing steam in modulation dehydration procedure (modulation dehydration groove 21).Therefore, compared with the situation needing to be arranged to carry out the cooler (cooler 155 of such as Fig. 2) of this cooling, it is possible to cut down number of machines (or scale of machine).Result can cut down the equipment cost of the equipment (ashless coal manufactures device 1) of the manufacture method carrying out ashless coal.
(variation)
Above-mentioned embodiment can carry out various deformation.Such as, Fig. 1 exemplifies the temperature of solvent, slurry.However, it is possible to the temperature of solvent, slurry to be set to the temperature different from the temperature that Fig. 1 illustrates.
It addition, such as, Fig. 1 distinguishes the state (solvent liquid, solvent vapour) representing solvent with the arrow of solid line and the arrow of dotted line.But it is also possible to the state of solvent is set to the state different from the state shown in Fig. 1.Wherein, supply is solvent liquid to the solvent of modulation dehydration groove 21, and supply is solvent vapour to the solvent of Venturi scrubber 23a.
It addition, for example, it is possible to suitably change the presence or absence of the order (order of connection of each machine) of each operation, each operation (each machine).[example 1] can not have the 3rd circulation road the 43, the 4th to circulate road the 44, the 5th to circulate road the 45, the 6th and circulate road 46 and be configured at all or part of of machine on these circulation roads.[example 2] flows into the solvent on the 6th circulation road 46 and supplies to oil-water separation tank 83 after by heat exchanger 77 heat exchange.But, the solvent flowing into the 6th circulation road 46 can supply to cooler 81 after by heat exchanger 77 heat exchange.
It addition, for example, it is possible to the some or all of composition that the ashless coal of the comparative example shown in Fig. 2 manufactures device 101 manufactures the some or all of of device 1 with the ashless coal shown in Fig. 1 and constitutes combination or displacement.Specifically, for instance, it is possible to the heat extraction recovery boiler 193 on the 6th circulation road 46 shown in Fig. 2 is configured to the ashless coal shown in Fig. 1 and manufactures on the 6th circulation road 46 of device 1.
Describe the present invention with reference to detailed and specific embodiment, but those skilled in the art are clear that: without departing from the spirit and scope of the present invention, the present invention can be made various changes and modifications.The application proposes based on the Japanese patent application (Japanese Patent Application 2013-267439) of December in 2013 application on the 25th, and its content is as with reference to being incorporated herein.
Industrial applicability
According to the present invention, by being effectively taking place the heat exchange of the coal heat exchange with solvent and slurry and solvent, such that it is able to effectively utilize the thermal energy produced in the manufacture process of ashless coal, and ashless coal can be manufactured inexpensively.
The explanation of symbol
1 ashless coal manufactures device
11 coal supply pipelines
13 steam discharging devices
20 slurry modulation machines
21 modulation dehydration grooves
23 modulation intensification machines
23a Venturi scrubber
33 extraction tanks
35 segregation apparatuss
37 solvent recovery units
41～46 circulation roads
Claims (5)
1. a manufacture method for ashless coal, it possesses following operation:
Slurry modulating process, mixes coal and solvent and modulates slurry, and carries out the dehydration of coal contained in described slurry and the intensification of described slurry；
Extraction process, is heated the described slurry of gained in described slurry modulating process and extracts the coal composition that dissolves in described solvent；
Separation circuit, is, by the described pulp separation obtained in described extraction process, the solution comprising the described coal composition dissolving in described solvent and solid constituent concentrated solution that the described coal composition insoluble in described solvent concentrates；
Ashless coal obtains operation, and from described separation circuit, in isolated solution, evaporation separates described solvent and obtains ashless coal；With
Circulating process, makes described ashless coal obtain and evaporates the circulation of isolated described solvent in operation,
Described slurry modulating process has:
Modulation dehydration procedure, by mixing the solvent circulated in described circulating process liquid and described coal and carry out the modulation of described slurry and the dehydration of described coal；With
Modulation heating process, carries out modulation and the intensification of described slurry by the solvent vapour circulated in described circulating process and described slurry being mixed.
2. the manufacture method of ashless coal according to claim 1, wherein, described modulation heating process regulates the concentration of described slurry in the way of the entrance concentration becoming described extraction process and described entrance concentration set in advance.
3. the manufacture method of ashless coal according to claim 1 and 2, wherein, till described modulation heating process makes described slurry be warming up to inlet temperature and the described inlet temperature set in advance of the then operation that described slurry modulating process carries out.
4. the manufacture method of ashless coal according to claim 1, wherein, the mixing of the described solvent vapour in described modulation heating process and described slurry utilizes Venturi scrubber to carry out.
5. the manufacture method of ashless coal according to claim 1, it has:
Coal supply step, utilizes coal supply pipeline to supply the described coal used in described slurry modulating process；With
Steam discharges operation, purges gas by flowing in described coal supply pipeline, thus being discharged in described coal supply pipeline by the steam produced in described modulation dehydration procedure.
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 |
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| Publication Number | Publication Date |
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| CN105793399A true CN105793399A (en) | 2016-07-20 |
| CN105793399B CN105793399B (en) | 2018-06-08 |
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| CN201480066265.XA Active CN105793399B (en) | 2013-12-25 | 2014-12-09 | The manufacturing method of ashless coal |
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| US (1) | US20160272910A1 (en) |
| JP (1) | JP5982666B2 (en) |
| KR (1) | KR101822772B1 (en) |
| CN (1) | CN105793399B (en) |
| AU (1) | AU2014371509B2 (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 |
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| 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 |
| CN105793399B (en) | 2018-06-08 |
| AU2014371509B2 (en) | 2016-12-22 |
| AU2014371509A1 (en) | 2016-06-23 |
| KR101822772B1 (en) | 2018-01-26 |
| WO2015098505A1 (en) | 2015-07-02 |
| JP2015124237A (en) | 2015-07-06 |
| KR20160089438A (en) | 2016-07-27 |
| US20160272910A1 (en) | 2016-09-22 |
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