WO2013125476A1 - Équipement de production de charbon modifié - Google Patents

Équipement de production de charbon modifié Download PDF

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Publication number
WO2013125476A1
WO2013125476A1 PCT/JP2013/053824 JP2013053824W WO2013125476A1 WO 2013125476 A1 WO2013125476 A1 WO 2013125476A1 JP 2013053824 W JP2013053824 W JP 2013053824W WO 2013125476 A1 WO2013125476 A1 WO 2013125476A1
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Prior art keywords
coal
oxygen adsorption
oxygen
adsorption rate
test
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PCT/JP2013/053824
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English (en)
Japanese (ja)
Inventor
飛太 阿部
慶一 中川
大本　節男
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三菱重工業株式会社
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Application filed by 三菱重工業株式会社 filed Critical 三菱重工業株式会社
Priority to AU2013223341A priority Critical patent/AU2013223341B2/en
Priority to US14/373,584 priority patent/US20150027872A1/en
Priority to DE112013001126.3T priority patent/DE112013001126T5/de
Priority to CN201380005660.2A priority patent/CN104053756B/zh
Publication of WO2013125476A1 publication Critical patent/WO2013125476A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means
    • C10L9/06—Treating solid fuels to improve their combustion by chemical means by oxidation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/083—Torrefaction
    • 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
    • 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
    • C10L2290/58—Control or regulation of the fuel preparation of upgrading process
    • 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
    • C10L2290/60—Measuring or analysing fractions, components or impurities or process conditions during preparation or upgrading of a fuel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the present invention relates to a modified coal production facility, and is particularly effective when applied to reforming a low-grade coal having a high moisture content such as lignite or subbituminous coal.
  • Low-grade coal such as lignite and sub-bituminous coal, which has a high water content, has a large reserve, but its calorific value per unit weight is low. The calorific value per weight is increased.
  • the heated low-grade coal is easy to adsorb water, and the surface carboxyl groups and the like are released to generate radicals on the surface, so that the surface activity becomes high and reacts with oxygen in the air. Since it becomes easy, there exists a possibility that it may ignite spontaneously with the reaction heat accompanying the said reaction.
  • the dry-distilled coal obtained by drying and dry-distilling low-grade coal is heated (about 150 to 170 ° C.) in a low-oxygen atmosphere (about 10% oxygen concentration).
  • a part of the surface of the dry-distilled coal is oxidized to perform a deactivation treatment that reduces the activity of the surface of the dry-distilled coal, thereby producing a modified coal that suppresses spontaneous combustion.
  • the composition of the raw material coal varies depending on the sampled mountain, so that it is inactive regardless of the raw material coal of any composition.
  • Various treatment conditions such as the oxygen concentration in the atmosphere of the inactivation treatment, the ambient temperature, and the treatment time are set so that the activation can be sufficiently performed. For this reason, even for raw coal that can be sufficiently deactivated under relatively loose processing conditions, the inactivation is performed under relatively severe processing conditions, resulting in waste of processing costs. It was.
  • the present invention provides a modified coal production facility that can easily produce a modified coal by performing an inactivation treatment under necessary and sufficient conditions even for raw material coal of various compositions.
  • the purpose is to provide.
  • the modified coal production facility according to the first invention for solving the above-mentioned problem is a drying means for making dry coal by removing moisture from raw coal, and dry distillation coal by dry distillation of the dry coal
  • a reformed coal production facility comprising: a dry distillation means; and an inactivation treatment means for heating the dry distillation coal with a treatment gas containing oxygen to inactivate the reformed coal.
  • a part of the dried coal dried by the drying means is fractionated to obtain an oxygen adsorption rate Vd of the dried coal, and the deactivation treatment means is inactivated.
  • a second oxygen adsorption rate measuring means for fractionating a part of the modified coal to determine the oxygen adsorption rate Vr of the modified coal, the following oxygen adsorption rate ratio Oxygen adsorption from the calculation formula
  • the deactivation processing means is controlled so as to maintain the deactivation processing condition, and the oxygen adsorption rate
  • the ratio N is larger than the range of the standard value Ns
  • the increased oxygen concentration value Oa into the processing gas corresponding to the oxygen adsorption rate ratio N is read from the map, and the current oxygen concentration in the processing gas
  • a corrected oxygen concentration value Oc in the processing gas is calculated, and the deactivation processing means is controlled so that the processing gas becomes the corrected oxygen concentration value Oc.
  • a reduced oxygen concentration value Od into the process gas corresponding to the oxygen adsorption rate ratio N is read from the map, and the process gas Current oxygen concentration in Based on Op and the reduced oxygen concentration value Od, a corrected oxygen concentration value Oc in the processing gas is calculated, and the deactivation processing means is controlled so that the processing gas becomes the corrected oxygen concentration value Oc.
  • Computational control means is provided.
  • the main arithmetic control means when the corrected oxygen concentration value Oc exceeds the upper limit value Ou, the oxygen adsorption rate ratio N Is read from the map, and a corrected temperature value Tc is calculated based on the current temperature value Tp in the process gas and the increased temperature value Ta, and the process gas is corrected.
  • the deactivation processing means is controlled so as to have a temperature value Tc.
  • the modified coal production facility is the first or second aspect of the invention, wherein the second oxygen adsorption rate measuring means is inactivated by the inactivation means.
  • a portion of the reformed coal is sampled and every time the specified time Ts elapses, a portion of the new reformed coal that has been deactivated by the deactivation processing means is again sorted and the modified coal is separated.
  • the oxygen adsorption rate Vr n-1 that this is newly sought immediately before the oxygen adsorption rate Vr n and time determined based on, it calculates the stability S from stability calculation formula, when the stability S is in the range of standard value Ss, the oxygen adsorption rate Vd, on the basis of Vr n, oxygen adsorption rate below
  • the oxygen adsorption rate ratio N is recalculated from the ratio recalculation formula, and the standard value Ns The comparison is performed again.
  • the reformed coal production facility is the modified coal production facility according to any one of the first to third aspects, wherein the first oxygen adsorption rate measuring means is the dry coal dried by the drying means.
  • first sub-operation control means for calculating the oxygen adsorption rate Vd of the dry coal from the following dry coal oxygen adsorption rate calculation formula based on the weights Wd1 and Wd2 weighed by the first weighing unit. And comprising A second fractionation means, wherein the second oxygen adsorption rate measuring means fractionates a part of the modified coal deactivated by the inactivation treatment means as a sample; and the second fractionation means A second test means for performing an oxygen adsorption test by exposing the sample fractionated in step (b) to an oxygen-containing gas at a test temperature for a test time Tr; and before the oxygen adsorption test fractionated by the second fractionation means.
  • a second sub-operation control means for calculating the oxygen adsorption rate Vr of the modified coal from a modified coal oxygen adsorption rate calculation formula.
  • Vd (Wd2 ⁇ Wd1) / (Wd1 ⁇ Td) ⁇ 100
  • Modified coal oxygen adsorption rate calculation formula: Vr (Wr2 ⁇ Wr1) / (Wr1 ⁇ Tr) ⁇ 100
  • the reformed coal production facility is the modified coal production facility according to any one of the first to third aspects, wherein the first oxygen adsorption rate measuring means is the dry coal dried by the drying means.
  • First sorting means for sorting a part as a sample, first weighing means for weighing the weight Wd1 of the sample sorted by the first sorting means, and the first sorting means Measuring the pressure inside the first test means, and a first test means for performing an oxygen adsorption test by keeping the sample separated in step 2 in an oxygen-containing atmosphere at a constant temperature in a test temperature Td.
  • a first pressure measuring means an internal pressure Pd1 before the oxygen adsorption test of the first testing means measured by the first pressure measuring means that is hermetically maintained in a constant temperature state in the oxygen-containing atmosphere, and Internal pressure Pd2 immediately after the oxygen adsorption test and before First sub-operation control means for calculating the oxygen adsorption rate Vd of the dry coal from the following dry coal oxygen adsorption rate calculation formula based on the weight Wd1 weighed by the first weighing unit, A second oxygen adsorption rate measuring means, a second fractionation means for fractionating a part of the modified coal deactivated by the inactivation treatment means as a sample; and the second fractionation A second weighing means for weighing a weight Wr1 of the sample separated by the means, and the sample separated by the second sorting means is hermetically sealed in a constant temperature state of an oxygen-containing atmosphere at a test time Tr.
  • a second test means for holding and performing an oxygen adsorption test a second pressure measuring means for measuring the pressure inside the second test means, and the inside being kept airtight in a constant temperature state in the oxygen-containing atmosphere.
  • the second pressure measuring means Based on the internal pressure Pr1 before the oxygen adsorption test of the second test means, the internal pressure Pr2 immediately after the oxygen adsorption test, and the weight Wr1 weighed by the second weighing means, the following modified coal oxygen adsorption rate calculation And a second sub-operation control means for calculating the oxygen adsorption rate Vr of the modified coal from the equation.
  • Vd Qd / (Wd1 ⁇ Td) ⁇ 100
  • Modified coal oxygen adsorption rate calculation formula: Vr Qr / (Wr1 ⁇ Tr) ⁇ 100
  • Qd is the oxygen adsorption amount of dry coal
  • Qr is the oxygen adsorption amount of the modified coal, and is a value obtained from the following formula.
  • Qd [ ⁇ (Pd1-Pd2) / 1013 ⁇ ⁇ ⁇ Cd ⁇ (Wd1 / D) ⁇ ] / (22.4 ⁇ Wd1)
  • Qr [ ⁇ (Pr1-Pr2) / 1013 ⁇ ⁇ ⁇ Cr- (Wr1 / D) ⁇ ] / (22.4 ⁇ Wr1)
  • Cd is the internal volume of the first test means
  • Cr is the internal volume of the second test means
  • D is the true density of the raw material coal.
  • the modified coal production facility according to the sixth invention is characterized in that, in any of the first to fifth inventions, the raw coal is lignite or subbituminous coal.
  • the modified coal production facility it is possible to easily produce a modified coal by performing an inactivation treatment under necessary and sufficient conditions even for raw material coal of various compositions.
  • FIG. 3 is a control flow diagram following FIG. 2.
  • FIG. 4 is a control flow diagram following FIG. 3.
  • FIG. 7 is a control flow diagram following FIG. 6.
  • FIG. 8 is a control flow diagram following FIG. 7.
  • the outlet of a mill-type pulverizer 111 that pulverizes low-grade coal 1 that is raw coal such as subbituminous coal and lignite coal is a steam tube dryer that evaporates moisture 2 in the low-grade coal 1.
  • the drying device 112 of the type is connected to the inlet of the low-grade coal 1 via a rotary valve 121, and the drying device 112 is a heating medium inside a coiled heating tube disposed in the central portion.
  • the low-grade coal 1 can be heated (about 100 ° C.) to remove the moisture 2 from the low-grade coal 1 to obtain dry coal 3.
  • the discharge port of the dry coal 3 of the drying device 112 is connected to the upstream side of the conveyor 113 in the transport direction via a rotary valve 122.
  • the downstream side in the transport direction of the conveyor 113 is connected to the dry coal 3 receiving port of the rotary kiln type dry distillation apparatus 114 for carbonizing the dry coal 3 via a rotary valve 123, and the dry distillation apparatus 114 is By supplying combustion gas 102 as a heating medium to the outer jacket fixedly supported, the dry coal 3 is heated and distilled (400 to 600 ° C.) to remove the volatile component 4 from the dry coal 3.
  • combustion gas 102 as a heating medium
  • the discharge port of the dry distillation coal 6 of the dry distillation device 114 is connected to the upstream side of the conveyor 115 in the transport direction via a rotary valve 124.
  • a downstream side of the conveyor 124 in the conveying direction is connected to a receiving port of the dry distillation coal 6 of a steam tube dryer type cooling device 116 for cooling the dry distillation coal 6 via a rotary valve 125.
  • the dry-distilled coal 6 can be cooled (100 ° C. or lower) by supplying the cooling water 103 as a cooling medium to the inside of the coiled cooling pipe disposed in the central portion. .
  • the discharge port of the dry distillation coal 6 of the cooling device 116 is a continuous processing type inactivation processing device such as a circular grade type or a sintering machine type (mesh conveyor type) for inactivating the dry distillation coal 6.
  • the apparatus main body 131 is connected to the inlet of the dry-distilled coal 6 via a rotary valve 126.
  • a nitrogen gas supply source 132 is connected to the lower portion of the apparatus main body 131 via a blower 133 and a heater 134.
  • a blower 135 for feeding air 104 is connected between the blower 133 and the heater 134.
  • the nitrogen gas 105 which is an inert gas from the nitrogen gas supply source 132, and the external air 104 are mixed to form the processing gas 106 containing oxygen as the heating gas 106.
  • the vessel 134 By operating the vessel 134, the processing gas 106 can be heated, and the dry-distilled coal 6 inside the apparatus main body 131 is heated with the processing gas 106 to be inactivated, and the modified coal 7 It can be done.
  • the oxygen gas concentration in the processing gas 106 can be adjusted, and the heater 134 is adjusted. By doing so, the temperature of the processing gas 106 can be adjusted.
  • the outlet of the reformed coal 7 of the apparatus main body 131 is connected to the upstream side of the conveyor 117 in the transport direction via a rotary valve 127.
  • a downstream side of the conveyor 117 in the transport direction is connected to a receiving port of the modified coal 7 of the storage tank 118 that stores the modified coal 7 via a rotary valve 128.
  • the pulverizing device 111, the drying device 112, the conveyor 113, the rotary valves 121, 122, and the like constitute drying means, and the dry distillation device 114, the conveyor 115, and the cooling device 116.
  • the rotary valves 123 to 125 constitute dry distillation means, the apparatus main body 131, the nitrogen gas supply source 132, the blowers 133 and 135, the deactivation processing device 130 such as the heater 134, the conveyor 117,
  • the rotary valves 126, 127, etc. constitute deactivation processing means, and the storage tank 118, the rotary valve 128, etc. constitute storage means.
  • the conveyor 113 is provided with a first sorting device 141 for sorting a part of the dry coal 3 dried by the drying device 112 as a sample 3a.
  • a first sample moving device 142 that receives and moves the sample 3 a from the first sorting device 141 is in communication with the first sorting device 141.
  • the first sample moving device 142 includes a first test device 143 that performs an oxygen adsorption test of the sample 3a sorted by the first sorting device 141, and the first sorting device 141 that sorts the sample 3a.
  • a first weighing device 144 that weighs the weight of the sample 3a before the oxygen adsorption test and the weight of the sample 3b after the oxygen adsorption test can be communicated with each other.
  • the first test apparatus 143 is connected to a blower 149a and a heater 149b for supplying air 104 which is an oxygen-containing gas heated in the test apparatus 143.
  • the conveyor 117 is attached with a second sorting device 145 for sorting a part of the modified coal 7 deactivated by the deactivation processing device 130 as a sample 7a.
  • a second sample moving device 146 that receives and moves the sample 7a from the second sorting device 145 communicates with the second sorting device 145.
  • the second sample moving device 146 includes a second test device 147 that performs an oxygen adsorption test on the sample 7 a that has been collected by the second sorting device 145 and the second sorting device 145 that has sorted the sample 7 a.
  • a second weighing device 148 that weighs the weight of the sample 7a before the oxygen adsorption test and the weight of the sample 7b after the oxygen adsorption test can be communicated with each other.
  • the second test apparatus 147 is connected to the blower 149a and the heater 149b for feeding the heated air 104 into the test apparatus 147.
  • the weighing devices 144 and 148 are electrically connected to the input unit of the arithmetic control device 150 having a built-in timer.
  • the output unit of the arithmetic and control unit 150 includes the blowers 133 and 135, the heater 134, the sorting devices 141 and 145, the sample moving devices 142 and 146, the test devices 143 and 147, the blower 149a, and the heating.
  • the calculation control device 150 is electrically connected to each of the devices 149b, and the calculation control device 150 is based on the information from the timer or the like, and the sorting devices 141 and 145, the sample moving devices 142 and 146, the testing device 143 and the like. 147, the blower 149a, the heater 149b, etc. can be operated and controlled, and the blowers 133, 135, the heater 134, etc. are controlled based on information from the weighing devices 144, 148, etc. (Details will be described later).
  • the first sorting device 141 and the like constitute a first sorting means
  • the first sample moving device 142 and the like constitute a first sample moving means
  • the first sorting device and the like constitute a first sorting device
  • the test device 143, the blower 149a, the heater 149b, etc. constitute a first test means
  • the first weighing device 144, etc. constitute a first weighing means
  • the second sample moving device 146 etc. constitutes a second sample moving device
  • the second test device 147, the blower 149a, the heater 149b etc. constitute a second test means.
  • the second weighing device 148 and the like constitute second weighing means
  • the arithmetic and control device 150 and the like constitute main arithmetic control means, first sub-arithmetic control means, and second sub-arithmetic control means.
  • the second oxygen adsorption rate measuring means is configured.
  • the pulverizer 111 When the low-grade coal 1 is supplied to the hopper 111a of the pulverizer 111, the pulverizer 111 pulverizes the low-grade coal 1 to a predetermined particle size, and the drying device 112 via the rotary valve 121. To supply. The drying device 112 heats and dries the low-grade coal 1 with the heat of the water vapor 101 (about 100 ° C.) to remove moisture 2 to form the dry coal 3, and then passes the rotary valve 122 through the rotary valve 122. Feed to the conveyor 113. The conveyor 113 feeds the dry coal 3 to the dry distillation apparatus 114 via the rotary valve 123.
  • the dry distillation device 114 heats and dry-distills the dry coal 3 (400 to 600 ° C.) to remove the volatile component 4 to make the dry-distilled coal 6 by the heat of the combustion gas 102, and then turns the rotary valve 124.
  • the conveyor 115 supplies the dry-distilled coal 6 to the cooling device 116 via the rotary valve 125.
  • the cooling device 116 cools the dry-distilled coal 6 with the cooling water 103 (100 ° C. or less), and then feeds it into the device main body 131 of the deactivation processing device 130 via the rotary valve 126. .
  • the deactivation processing device 130 is a processing gas 106 in which the nitrogen gas 105 from the nitrogen gas supply source 132 and the external air 104 are mixed by the blowers 133 and 135 and the heater 134 (oxygen concentration: 1.. 5%) is heated (50 ° C.) and fed to the inside of the apparatus main body 131, and the dry-distilled coal 6 in the apparatus main body 131 is heated and deactivated to obtain the modified coal 7. , And fed to the conveyor 117 via the rotary valve 127. The conveyor 117 supplies and stores the modified coal 7 to the storage tank 118 through the rotary valve 128.
  • the arithmetic and control unit 150 uses a part of the dry coal 3 dried by the drying unit 112 as the sample 3a from the conveyor 113.
  • the first sample moving device After controlling the operation of the first sorting device 141 so as to sort (S101 in FIG. 2), the first sample moving device so as to receive the sorted sample 3a from the first sorting device 141. 142 controls the operation.
  • the arithmetic and control unit 150 controls the operation of the first sample moving unit 142 so that the weight Wd1 (g) of the sample 3a is measured by the first weighing unit 144 (S102 in FIG. 2).
  • the first sample moving device 142 is controlled to move the weighed sample 3a into the first test device 143.
  • the arithmetic and control unit 150 operates the blower 149a and the heater 149b so as to supply the air 104 heated to a predetermined test temperature (for example, 95 ° C.) into the first test unit 143.
  • a predetermined test temperature for example, 95 ° C.
  • the sample 3a is exposed to the air 104 at the test temperature to perform an oxygen adsorption test (S103 in FIG. 2).
  • the arithmetic and control unit 150 adds the sample 3b that has been subjected to the oxygen adsorption test to the first sample based on information from the timer.
  • Td predetermined test time
  • the arithmetic and control unit 150 adds the sample 3b that has been subjected to the oxygen adsorption test to the first sample based on information from the timer.
  • the weight Wd2 (g) of the sample 3b is weighed by the first weighing device 144 ( In FIG. 2, the operation of the first sample moving device 142 is controlled so that the sample 3b is discharged out of the system (S104).
  • the arithmetic and control unit 150 calculates the drying from the dry coal oxygen adsorption rate calculation formula (11) below based on the weights Wd1 and Wd2.
  • the oxygen adsorption rate Vd (wt% / min.) Of the coal 4 is calculated (S105 in FIG. 2).
  • Vd (Wd2-Wd1) / (Wd1 ⁇ Td) ⁇ 100 (11)
  • the arithmetic and control unit 150 sorts the part of the reformed coal 7 deactivated by the apparatus main body 131 of the deactivation processing unit 130 as the sample 7a from the conveyor 117. After the operation of the second sorting device 145 is controlled (S106 in FIG. 2), the second sample moving device 146 is controlled to receive the sample 7a that has been sorted from the second sorting device 145.
  • the arithmetic and control unit 150 controls the operation of the second sample moving unit 146 so that the weight Wr1 (g) of the sample 7a is measured by the second weighing unit 148 (S107 in FIG. 2).
  • the second sample moving device 146 is controlled to operate so that the weighed sample 7 a is positioned in the second test device 147.
  • the arithmetic and control unit 150 operates the blower 149a and the heater 149b so as to supply the air 104 heated to a predetermined test temperature (for example, 95 ° C.) into the second test unit 147.
  • a predetermined test temperature for example, 95 ° C.
  • the sample 7a is exposed to the air 104 at the test temperature to perform an oxygen adsorption test (S108 in FIG. 2).
  • the arithmetic and control unit 150 determines the sample 7b on which the adsorption test has been performed on the second test based on information from the timer.
  • the second sample moving device 146 is controlled to move from the device 147 to the second weighing device 148, and the weight Wr2 (g) of the sample 3b is weighed by the second weighing device 148 (see FIG. 2, the operation of the second sample moving device 146 is controlled so that the sample 7 b is discharged out of the system.
  • the arithmetic and control unit 150 calculates the above-described modified coal oxygen adsorption rate calculation formula (12) based on the weights Wr1 and Wr2.
  • the oxygen adsorption rate Vr (wt% / min.) Of the modified coal 7 is calculated (S110 in FIG. 2).
  • Vr (Wr2-Wr1) / (Wr1 ⁇ Tr) ⁇ 100 (12)
  • the arithmetic and control unit 150 calculates the following based on the oxygen adsorption rates Vd and Vr.
  • the oxygen adsorption rate ratio N is calculated from the oxygen adsorption rate ratio calculation formula (13) (S111 in FIG. 2).
  • the arithmetic and control unit 150 determines whether or not the oxygen adsorption rate ratio N is within a range of a standard value Ns (for example, 0 to 0.05) (S112 in FIG. 2), and the standard value Ns. If it is within the range, it is determined that the inactivation process is properly performed, and the blowers 133, 135 and Operation of the heater 134 is controlled (S113 in FIG. 2).
  • Ns for example, 0 to 0.05
  • the arithmetic and control unit 150 determines whether or not the oxygen adsorption rate ratio N is larger than the range of the standard value Ns ( In FIG. 3, when S114) is larger than the range of the standard value Ns (N> Ns), it is determined that the inactivation process is insufficient, and is set corresponding to the oxygen adsorption rate ratio N.
  • the increased oxygen concentration value Oa into the processing gas 106 is read out from a previously input map (S115 in FIG. 3), and the current oxygen concentration value Op in the processing gas 106 and the increased oxygen concentration value Oa are read out. Based on the above, a corrected oxygen concentration value Oc in the processing gas 106 is calculated (S116 in FIG. 3).
  • the arithmetic and control unit 150 determines whether or not the corrected oxygen concentration value Oc is equal to or lower than an upper limit value Ou (for example, 10%) (S117 in FIG. 3).
  • an upper limit value Ou for example, 10%
  • the blowers 133 and 135 of the deactivation processing apparatus 130 are controlled to operate so that the processing gas 106 becomes the corrected oxygen concentration value Oc (S118 in FIG. 3).
  • the arithmetic and control unit 150 determines that the response due to the increase in the oxygen concentration of the processing gas 106 is inappropriate, An increased temperature value Ta of the processing gas 106 set corresponding to the oxygen adsorption rate ratio N is read from a previously input map (S119 in FIG. 3), and the current temperature value in the processing gas 106 is read. A corrected temperature value Tc of the processing gas 106 is calculated based on Tp and the increased temperature value Ta (S120 in FIG. 3).
  • the arithmetic and control unit 150 determines whether or not the corrected temperature value Tc is equal to or lower than an upper limit value Tu (for example, 95 ° C.) (S121 in FIG. 3).
  • an upper limit value Tu for example, 95 ° C.
  • the heater 134 of the deactivation processing apparatus 130 is controlled to operate so that the processing gas 106 becomes the corrected temperature value Tc (S122 in FIG. 3).
  • the arithmetic and control unit 150 determines that the deactivation process cannot be appropriately performed for some reason, and the modified coal 7 A command necessary for interrupting the manufacturing of the device is transmitted (S123 in FIG. 3).
  • step S114 when the oxygen adsorption rate ratio N is smaller than the range of the standard value Ns (N ⁇ Ns), it is determined that the arithmetic and control unit 150 is excessively inactivated. Then, a reduced oxygen concentration value Od from the processing gas 106 set corresponding to the oxygen adsorption rate ratio N is read from a previously input map (S124 in FIG. 3), and the processing gas 106 is read out.
  • the corrected oxygen concentration value Oc in the processing gas 106 is calculated on the basis of the current oxygen concentration value Op and the reduced oxygen concentration value Od in the processing gas (S125 in FIG. 3), and the processing gas is subjected to the corrected oxygen concentration value.
  • the blowers 133 and 135 of the deactivation processing apparatus 130 are controlled to be Oc (S118 in FIG. 3).
  • the blowers 133 and 135 and the heater 134 of the deactivation processing apparatus 130 are operated and controlled so as to appropriately perform the deactivation processing, and the specified time Ts ( For example, when 1 hour elapses (S126 in FIG. 4), the arithmetic and control unit 150 performs the new modification that has been deactivated by the deactivation processing unit 130 in the same manner as in steps S106 to S110. was collected again divided part quality coal 7 as a sample 7a n (in FIG. 4, S127), after weighing the weight Wr1 n (g) of the sample 7a n before the oxygen adsorption test (in FIG.
  • Vr n (Wr2 n ⁇ Wr1 n ) / (Wr1 n ⁇ Tr) ⁇ 100 (14)
  • the arithmetic and control unit 150 performs the following based on the oxygen adsorption rate Vr n newly obtained this time and the oxygen adsorption rate Vr n-1 (Vr in this case) obtained immediately before this time.
  • the stability S of the inactivation processing is calculated from the stability calculation formula (15) (S132 in FIG. 4).
  • the arithmetic and control unit 150 determines whether or not the stability S is within a standard value Ss (for example, 0 to 0.01) (S133 in FIG. 4), and the range of the standard value Ss. If it is within the range, it is determined that the inactivation process has been stably performed, and the oxygen adsorption rate Vd obtained from the samples 3a and 3b of the dry coal 3 and the current time are determined.
  • a standard value Ss for example, 0 to 0.01
  • the arithmetic and control unit 150 determines that the inactivation process is in an unstable state and cannot be determined appropriately. Then, returning to the step S126, the steps S127 to S133 are performed again.
  • the modified coal production facility 100 even if the low-grade coal 1 has various compositions, the modified coal can be easily produced at low cost.
  • the first sample moving device 142 that receives and moves the sample 3 a from the first sorting device 141 includes the oxygen contained in the sample 3 a sorted by the first sorting device 141.
  • a first test device 243 which is a first test means for performing an oxygen adsorption test while keeping the inside of a constant temperature state (for example, 20 ° C.) of an air atmosphere which is an atmosphere, and the first sorting device 141 for sorting. It is possible to communicate with the first weighing device 144 for weighing the sample 3a.
  • the first test apparatus 243 is provided with a pressure sensor 243a that is a first pressure measuring unit that measures the pressure inside the test apparatus 243.
  • the second sample moving device 146 that receives and moves the sample 7a from the second sorting device 145 is an air atmosphere in which the sample 7a sorted by the second sorting device 145 is an oxygen-containing atmosphere.
  • a second test device 247 which is a second test means for performing an oxygen adsorption test while maintaining airtightness in a constant temperature state (for example, 20 ° C.), and the sample 7a sorted by the second fractionation device 145 It is possible to communicate with a second weighing device 148 for weighing each of the two.
  • the second test apparatus 247 is provided with a pressure sensor 247a which is a second pressure measuring means for measuring the pressure inside the test apparatus 247.
  • the pressure sensors 243a and 247a are electrically connected together with the weighing devices 144 and 148 to the input unit of the arithmetic control device 250 having a built-in timer or the like.
  • the output unit of the arithmetic control device 250 is electrically connected to the blowers 133 and 135, the heater 134, the sorting devices 141 and 145, and the sample moving devices 142 and 146, together with the test devices 243 and 247, respectively.
  • the arithmetic and control unit 250 controls the operations of the sorting devices 141 and 145, the sample moving devices 142 and 146, the test devices 243 and 247, etc., based on information from the timer and the like.
  • the blowers 133 and 135, the heater 134 and the like can be controlled based on information from the weighing devices 144 and 148 and the pressure sensors 243a and 247a (details). Will be described later).
  • the arithmetic control device 250 or the like is configured to serve as the main arithmetic control means, the first sub arithmetic control means, and the second sub arithmetic control means.
  • the modified coal production facility 200 is similar to the modified coal production facility 100 according to the embodiment described above.
  • the dry coal 3 is obtained by removing moisture 2 from the low-grade coal 1, the dry coal 3 is dry-distilled to form the dry-distilled coal 6, and the dry-distilled coal 6 is heated with the processing gas 106 to be inactivated.
  • the modified coal 7 is stored in the storage tank 118.
  • the arithmetic and control unit 250 is configured to sort a part of the dry coal 3 dried by the drying device 112 as the sample 3a from the conveyor 113.
  • the first sample moving device 142 is controlled to receive the sample 3a thus sorted from the first sorting device 141.
  • the arithmetic and control unit 250 operates the first sample moving device 142 so that the weight Wd1 (g) of the sample 3a is weighed by the first weighing device 144 as in the case of the above-described embodiment.
  • the first sample moving device 142 is controlled to seal the weighed sample 3a inside the first test device 243, information from the pressure sensor 243a is obtained.
  • the internal pressure Pd1 (hPa) before the oxygen adsorption test of the first test apparatus 243 is measured (S203 in FIG. 6).
  • the arithmetic and control unit 250 sets the sample 3a to a predetermined test time Td (min.) (For example, in a constant temperature air atmosphere inside the first test unit 243). 10 minutes)
  • Td predetermined test time
  • the arithmetic and control unit 250 sets the sample 3a to a predetermined test time Td (min.) (For example, in a constant temperature air atmosphere inside the first test unit 243). 10 minutes)
  • the arithmetic and control unit 250 sets the sample 3a to a predetermined test time Td (min.) (For example, in a constant temperature air atmosphere inside the first test unit 243). 10 minutes)
  • Td predetermined test time
  • the internal pressure Pd2 (hPa) after the oxygen adsorption test of the first test device 243 S205 in FIG. 6
  • the operation of the first sample moving device 142 is controlled so that the sample 3b after the oxygen adsorption test is discharged out of the system from the first test device 243.
  • the arithmetic and control unit 250 determines the weight Wd1 and the internal pressures Pd1 and Pd2. Based on the dry coal oxygen adsorption rate calculation formulas (21) and (22) below, the oxygen adsorption rate Vd (wt% / min.) Of the dry coal 3 is calculated (S206 in FIG. 6).
  • Vd Qd / (Wd1 ⁇ Td) ⁇ 100 (21)
  • Qd is the oxygen adsorption amount (mmol-O 2 / g-coal) of the dry coal 3, and is a value obtained from the following formula (22).
  • Cd is the internal volume (cm 3 ) of the first test apparatus 243
  • D is the true density (g / cm 3 ) of the low-grade coal 1, each of which is obtained in advance.
  • the arithmetic and control unit 250 separates a part of the modified coal 7 deactivated by the deactivation processing unit 130 from the conveyor 117 as a sample 7a.
  • the second sample moving device 146 is received so as to receive the sorted sample 7a from the second sorting device 145. To control the operation.
  • the arithmetic and control unit 250 operates the second sample moving unit 146 so that the weight Wr1 (g) of the sample 7a is weighed by the second weighing unit 148 as in the case of the above-described embodiment.
  • the control S208 in FIG. 6
  • the second sample moving device 146 is controlled to seal the weighed sample 7a inside the second test device 247
  • information from the pressure sensor 247a is obtained.
  • the internal pressure Pr1 (hPa) before the oxygen adsorption test of the second test apparatus 247 is measured (S209 in FIG. 6).
  • the arithmetic and control unit 250 sets the sample 7a to a predetermined test time Tr (min.) (For example, in a constant temperature air atmosphere inside the second test unit 247). 10 minutes) After the oxygen adsorption test by holding the gas tightly (S210 in FIG. 6), based on the information from the pressure sensor 247a, the internal pressure Pr2 (hPa) after the oxygen adsorption test of the second test device 247 (S211 in FIG. 6), the second sample moving device 146 is controlled to discharge the sample 7b after the oxygen adsorption test from the second test device 247 to the outside of the system.
  • Tr predetermined test time Tr
  • the arithmetic and control unit 250 calculates the weight Wr1 and the internal pressures Pr1 and Pr2. Based on the following modified coal oxygen adsorption rate calculation formula (23), the oxygen adsorption rate Vr (wt% / min.) Of the modified coal 7 is calculated (S212 in FIG. 6).
  • Vr Qr / (Wr1 ⁇ Tr) ⁇ 100 (23)
  • Qr is the oxygen adsorption amount (mmol-O 2 / g-coal) of the modified coal 7, and is a value obtained from the following equation (24).
  • Cr is the internal volume (cm 3 ) of the second test apparatus 247 and is a value obtained in advance.
  • the oxygen adsorption rate ratio N is calculated from the oxygen adsorption rate ratio calculation formula (13) (S111 in FIG. 6).
  • the arithmetic and control unit 250 performs the steps S112 to S126 as in the above-described embodiment (see FIGS. 6 to 8).
  • the blower 133, 135 and the heater 134 of the deactivation processing apparatus 130 are operated and controlled so as to appropriately perform the deactivation processing, and the modified coal
  • Ts for example, 1 hour
  • the arithmetic and control unit 250 causes the deactivation processing unit 130 to perform the inactivation in the same manner as in steps S207 to S212.
  • Vr n Qr n / (Wr1 n ⁇ Tr) ⁇ 100 (25)
  • Qr n is the oxygen adsorption amount (mmol-O 2 / g-coal) of newly reformed coal 7 that has been newly separated, and is obtained from the following equation (26) similar to the equation (24). Value.
  • the arithmetic and control unit 250 described above based on the oxygen adsorption rate Vr n newly obtained this time and the oxygen adsorption rate Vr n-1 (Vr in this case) obtained immediately before this time.
  • the stability S is calculated from the equation (15) (S132 in FIG. 8).
  • the said arithmetic and control unit 250 performs said step S133, S134 similarly to the case of embodiment mentioned above (refer FIG. 8). Thereafter, the arithmetic and control unit 250 performs operation control in the same manner as in the above-described embodiment (see FIGS. 6 to 8).
  • the composition of the low-grade coal 1 has variations, as in the case of the modified coal manufacturing facility 100 according to the above-described embodiment.
  • inactivation treatment can be easily performed under necessary and sufficient conditions corresponding to the composition of the low-grade coal 1.
  • the reformed coal production facility 100 according to the present embodiment as in the case of the reformed coal production facility 100 according to the above-described embodiment, even with the low-grade coal 1 having various compositions, the cost is low.
  • the modified coal can be easily produced.
  • the arithmetic control devices 150 and 250 are configured to serve as the main arithmetic control means, the first sub arithmetic control means, and the second sub arithmetic means.
  • the main calculation control means, the first sub calculation control means, and the second sub calculation means independently of each other.
  • the sample 3a sorted by the first sorting device 141 is moved to the first weighing device 144 and the first testing devices 143 and 243 by the first sample moving device 142.
  • the sample 7a sorted by the second sorting device 145 is moved to the second weighing device 148 and the second testing devices 147 and 247 by the second sample moving device 146.
  • the sample 3a sorted by the first sorting means and the sample 7a sorted by the second sorting means are moved by the same sample moving means.
  • the first weighing means and the second weighing means can be configured to serve as the same weighing means, or the first testing means and the second testing means can be used as the same testing means. It is also possible to configure the.
  • the processing gas 106 having a desired oxygen concentration is generated by mixing the nitrogen gas 105 and the air 104.
  • the nitrogen gas 105 is used. It is also possible to generate the processing gas 106 having a desired oxygen concentration by mixing the oxygen gas and the oxygen gas. However, if the processing gas 106 having a desired oxygen concentration is generated by mixing the nitrogen gas 105 and the air 104 as in the above-described embodiment, it is not necessary to prepare the oxygen gas. So very preferable.
  • a nitrogen gas cylinder prepared only for generating the processing gas 106 can be applied, and in addition, for example, nitrogen gas supplied to the dry distillation apparatus, for example. It is also possible to apply dry distillation gas (main component: nitrogen gas) from which volatile components and dust, etc. have been separated after carbonizing low-grade coal and sending it from the carbonization device. It is possible to reduce the heat energy newly added to the processing gas 106 when performing.
  • main component nitrogen gas
  • the modified coal 7 is not limited to this, Drying
  • the reformed coal production facility according to the present invention can be used for industrially extremely beneficial because it can produce a reformed coal by simply inactivating at low cost even if it is a raw material coal of various compositions. can do.

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  • General Chemical & Material Sciences (AREA)
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Abstract

La présente invention concerne un équipement de production de charbon modifié comprenant : un premier moyen de mesure de vitesse d'adsorption d'oxygène (141 à 144, 149a, 149b), etc., qui trie le charbon séché (3) séché dans un dispositif de séchage (112), et détermine la vitesse d'adsorption d'oxygène (Vd) du charbon séché (3) ; un second moyen de mesure de vitesse d'adsorption d'oxygène (145 à 148, 149a, 149b) qui trie le charbon modifié (7) désactivé par un dispositif de traitement de désactivation (130), et détermine la vitesse d'adsorption d'oxygène (Vr) du charbon modifié (7) ; et un dispositif de commande arithmétique (150) qui calcule le rapport de vitesse d'adsorption d'oxygène (N) à partir de la formule (Vr-Vd)/Vd = N, sur la base de Vd et de Vr et, si N>Ns (une valeur standard), lit depuis une carte la valeur de concentration d'oxygène augmentée (Oa) d'un gaz de traitement (106) correspondant à N, calcule une valeur de concentration d'oxygène révisée (Oc) sur la base de la valeur de concentration d'oxygène courant (Op) et Oa, et commande des soufflantes (133, 135) de façon à atteindre Oc.
PCT/JP2013/053824 2012-02-24 2013-02-18 Équipement de production de charbon modifié WO2013125476A1 (fr)

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AU2013223341A AU2013223341B2 (en) 2012-02-24 2013-02-18 Modified coal production equipment
US14/373,584 US20150027872A1 (en) 2012-02-24 2013-02-18 Modified coal production equipment
DE112013001126.3T DE112013001126T5 (de) 2012-02-24 2013-02-18 Produktionsanlage für modifizierte Kohle
CN201380005660.2A CN104053756B (zh) 2012-02-24 2013-02-18 改性煤制造设备

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WO2016143431A1 (fr) * 2015-03-09 2016-09-15 三菱重工業株式会社 Dispositif d'inactivation de charbon distillé à sec, usine de valorisation de charbon, et procédé de production de charbon inactivé distillé à sec
US10151530B2 (en) 2015-03-09 2018-12-11 Mitsubishi Heavy Industries Engineering, Ltd. Coal upgrade plant and method for manufacturing upgraded coal
US10188980B2 (en) 2015-03-09 2019-01-29 Mitsubishi Heavy Industries Engineering, Ltd. Coal upgrade plant and method for manufacturing upgraded coal
US10221070B2 (en) 2015-03-09 2019-03-05 Mitsubishi Heavy Industries Engineering, Ltd. Coal upgrade plant and method for manufacturing upgraded coal
US10703976B2 (en) 2015-03-09 2020-07-07 Mitsubishi Heavy Industries Engineering, Ltd. Pyrolyzed coal quencher, coal upgrade plant, and method for cooling pyrolyzed coal

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CN103983545A (zh) * 2014-06-05 2014-08-13 北京国电清新环保技术股份有限公司 一种活性焦二氧化硫吸附速率测试装置和方法
CN108759313B (zh) * 2018-06-14 2019-10-29 中国矿业大学 一种褐煤干燥-干法分选协同优化提质方法及工艺

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WO2016143431A1 (fr) * 2015-03-09 2016-09-15 三菱重工業株式会社 Dispositif d'inactivation de charbon distillé à sec, usine de valorisation de charbon, et procédé de production de charbon inactivé distillé à sec
US10151530B2 (en) 2015-03-09 2018-12-11 Mitsubishi Heavy Industries Engineering, Ltd. Coal upgrade plant and method for manufacturing upgraded coal
US10188980B2 (en) 2015-03-09 2019-01-29 Mitsubishi Heavy Industries Engineering, Ltd. Coal upgrade plant and method for manufacturing upgraded coal
US10221070B2 (en) 2015-03-09 2019-03-05 Mitsubishi Heavy Industries Engineering, Ltd. Coal upgrade plant and method for manufacturing upgraded coal
US10703976B2 (en) 2015-03-09 2020-07-07 Mitsubishi Heavy Industries Engineering, Ltd. Pyrolyzed coal quencher, coal upgrade plant, and method for cooling pyrolyzed coal

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AU2013223341A1 (en) 2014-08-14
AU2013223341B2 (en) 2015-07-16
DE112013001126T5 (de) 2014-11-06

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