WO2006109629A1 - 湿潤原料の乾燥装置及び乾燥方法 - Google Patents
湿潤原料の乾燥装置及び乾燥方法 Download PDFInfo
- Publication number
- WO2006109629A1 WO2006109629A1 PCT/JP2006/307135 JP2006307135W WO2006109629A1 WO 2006109629 A1 WO2006109629 A1 WO 2006109629A1 JP 2006307135 W JP2006307135 W JP 2006307135W WO 2006109629 A1 WO2006109629 A1 WO 2006109629A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- exhaust gas
- coke oven
- raw material
- fluidized bed
- bed dryer
- Prior art date
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
- F26B25/005—Treatment of dryer exhaust gases
- F26B25/007—Dust filtering; Exhaust dust filters
-
- 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
- C10B43/00—Preventing or removing incrustations
- C10B43/14—Preventing incrustations
-
- 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
- C10B45/00—Other details
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
- F26B25/005—Treatment of dryer exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B3/00—Drying solid materials or objects by processes involving the application of heat
- F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
- F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
- F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Definitions
- the present invention relates to a wet raw material drying apparatus and a drying method for drying a wet raw material such as coal charged in a coke oven with a fluidized bed dryer.
- Patent Document 1 discloses that flue exhaust gas from a coke oven is introduced into a fluidized bed dryer as a heat source and fluidized gas. A method for drying coal is disclosed. Most of the coal powder charged in the fluidized bed dryer is discharged from a discharge chute that communicates with the fluidized bed and is transported to a coke oven. In addition, fine powder is generated by drying the coal powder, and this fine powder is discharged together with the exhaust gas from the exhaust gas outlet above the fluidized bed and collected by a dust collector installed in the exhaust gas piping.
- the exhaust gas temperature of the coatus furnace used as the heat source and fluidizing gas of the fluidized bed dryer varies depending on the operation load status, fuel properties, and combustion control status of the coke oven.
- exhaust gas that is significantly hotter than the temperature conditions at the time of dryer design may flow in.
- the amount of fines generated from the coal increases due to the moisture in the coal being dried more than at the time of design, and the amount of fines collected by the dust collector also increases.
- the calorific value of the coke oven fuel is temporarily reduced, exhaust gas that is significantly cooler than the temperature conditions at the time of dryer design may flow in.
- a coke oven usually has two combustion gas systems for each furnace group, and when the usage time in one system reaches a predetermined time, the system is switched to the other system. .
- the system is normally switched once every 15 to 30 minutes.
- the combustion gas flow rate of the system (system A) that has been used so far is gradually decreased, and when the flow rate becomes zero, the system to be used next (system B) )
- the combustion gas flow rate is gradually increased. Therefore, when switching the combustion gas system, the amount of exhaust gas in the coke oven decreases, reaches zero, and increases again.
- the time for fluctuations in gas flow due to switching of the combustion gas system is generally 0.5 to 3 minutes.
- the temperature of the gas flowing into the fluidized bed of the fluidized bed dryer decreases as shown in FIG.
- the dryness of the wet raw material decreases, and the amount of fine powder generated by drying and collected by the dust collector decreases.
- the switching of the combustion gas system is normally performed once every 15 to 30 minutes, and the time for the change of the gas flow rate accompanying the switching is as short as about 0.5 to 3 minutes. It is not realistic to run the hot air generator each time to make up for the amount of heat needed to dry the wet material.
- Patent Document 2 devised a method of granulating by adding heavy oil to fine powder Yes.
- this patent does not take into account fluctuations in the gas flow rate or gas temperature of hot air such as the exhaust gas from the Kotas furnace, and as described in the embodiment, the amount of heavy oil added is about 95 tZhr of fine powder. The amount is constant at about 250kgZhr.
- Patent Document 1 Japanese Patent Laid-Open No. 2001-55582
- Patent Document 2 Japanese Patent Publication No.49-28241
- the problem to be solved by the present invention is that the supply of coke oven exhaust gas, which is a high-temperature gas supplied to a fluidized bed dryer as a heat source and fluidizing gas, is stopped, decreased or increased, or Even if the amount of fine powder discharged and recovered together with the fluidized bed dryer gas is increased or decreased as the temperature changes, dust is scattered by mixing the fine powder at a constant ratio with the binder required for granulation. This is to reliably prevent carbon from adhering to the coke oven wall.
- coke oven exhaust gas which is a high-temperature gas supplied to a fluidized bed dryer as a heat source and fluidizing gas
- the present invention includes a fluidized bed dryer for drying a wet raw material, a gas supply pipe (duct and blower) for supplying the exhaust gas from the coatus furnace as a heat source and fluidizing gas to the fluidized bed dryer.
- Fluidized bed dryer power In a wet raw material drying device having a dust collector that collects fine powder discharged together with gas, the dust collector is affected by fluctuations in the dryness of the wet raw material accompanying fluctuations in the temperature or flow rate of the coke oven exhaust gas supplied. It is characterized in that it has a binder addition device equipped with a mechanism that can be adjusted automatically or manually so that the amount of binder added is a fixed ratio to the fine powder with respect to the fine powder whose recovery amount also fluctuates.
- the present invention provides a binder addition for detecting a change in the amount of exhaust gas supplied from a coke oven or a change in the temperature of the exhaust gas in the drying apparatus, and adjusting a binder addition amount in response to the detection signal.
- a quantity control device is provided.
- the drying device the fluctuation of the exhaust gas temperature / flow rate accompanying the fluctuation of the production amount in the coke oven is detected, and the amount of binder added to the fine dust collected according to the fluctuation amount is automatically detected.
- a binder addition control device having a mechanism that can be manually adjusted is provided.
- the present invention provides a binder for fine powder collected in the drying device by detecting a change in exhaust gas temperature / flow rate associated with a change in the calorific value of the coke oven fuel. It is characterized by a binder addition control device equipped with a mechanism that can adjust the addition amount automatically or manually.
- the present invention in the above drying apparatus, it is detected that the supply of exhaust gas from the coke oven is stopped or reduced, and the amount of binder added to the fine powder collected in accordance with the detection signal is automatically set.
- a binder addition control device equipped with a mechanism that can be manually adjusted is provided.
- the amount of collected dust collected by the dryness of the wet raw material accompanying a change in the temperature or flow rate of the supplied coal furnace exhaust gas is also reduced. It is characterized in that the added amount of the binder is adjusted by a binder adding device equipped with a mechanism capable of being automatically or manually adjusted so that the added amount of the binder becomes a constant ratio with respect to the changing fine powder.
- the fluctuation of the exhaust gas temperature / flow rate accompanying the fluctuation of the production amount in the coke oven is detected, and the fine powder collected according to the fluctuation amount is detected.
- the amount of binder added is adjusted.
- the present invention provides a method for drying a wet raw material by the drying device, wherein the fluctuation of the exhaust gas temperature and the flow rate accompanying the fluctuation of the calorific value of the coke oven fuel is detected, and the fine powder collected according to the fluctuation amount. It is characterized in that the amount of the binder added to is adjusted.
- the drying apparatus in the method for drying a wet raw material by the drying apparatus, it is detected that the supply of the high-temperature gas from the coke oven is stopped or reduced, and the fine powder collected according to the detection signal is detected. The amount of the binder added is adjusted.
- the gas discharged from the fluidized bed dryer is circulated and reused as the fluidized gas of the fluidized bed dryer. it can. In addition, it can be detected from the prediction signal or the start signal of the combustion system switching of the coke oven that the supply of the exhaust gas from the coatus furnace is stopped or decreased.
- the coke oven exhaust supplied to the fluidized bed dryer as a heat source and fluidizing gas is provided. Even if the gas supply stops, decreases or increases, or the temperature of the coke oven exhaust gas fluctuates, even if the amount of fine powder discharged and recovered together with the fluidized bed dryer power gas fluctuates, the coke oven exhaust gas supply stops or decreases Or the increase or the change in the coke oven exhaust gas temperature is detected or predicted, and the amount of fine powder recovered by the dust collector is adjusted to adjust the amount of binder added, so the mixing ratio of fine powder and binder is always optimal. The ratio can be maintained. Therefore, by adding a sufficient amount of binder to the fine powder, if dust is scattered, carbon adhesion to the coke oven wall can be prevented, and problems such as contamination of the conveying path and waste of binder due to excessive binder can be solved.
- FIG. 1 is a schematic configuration diagram showing an embodiment of a drying apparatus of the present invention.
- FIG. 2 is a schematic configuration diagram showing another embodiment of the drying apparatus of the present invention.
- FIG. 3 is a diagram showing a switching state of a combustion exhaust gas system of a coke oven in the present invention.
- FIG. 4 is a diagram showing a switching state of a combustion exhaust gas system of a coke oven in the prior art.
- coal powder for coke ovens
- FIG. 1 is a schematic configuration diagram showing an embodiment of a drying apparatus of the present invention.
- the coke oven combustion exhaust gas generated in the coke oven 1 passes through the flue 2 and is emitted from the coke oven chimney 3 to the atmosphere.
- the temperature of flue exhaust gas (coatus furnace exhaust gas) 4 passing through the flue 2 is about 150-250 ° C.
- the coke oven exhaust gas 4 flows through the gas supply pipe 5 branched from the coke oven flue 2, is pressurized by the blower 6, and is then supplied from the lower part of the fluidized bed dryer 8 as the heat source / fluidized gas 7.
- the exhaust gas 9 discharged from the fluidized bed dryer 8 is diffused into the atmosphere from the chimney 13 via the dust collector 11 and the professional tank 12 by the exhaust gas pipe 10.
- Coal powder as a wet raw material is charged into the fluidized bed dryer 8 by the charging chute 15, and is fluidized by the upward flow of the heat source / fluidizing gas 7 introduced from the lower part of the fluidized bed dryer 8.
- Form 16 In the fluidized bed 16, the coal powder is dried, and the coal powder is adjusted to a predetermined temperature and moisture content, most of which is discharged by the discharge chute 17.
- the coal powder discharged from the discharge chute 17 is transported to the coatus furnace by a transport path (not shown).
- fine powder is generated by drying the coal powder in the fluidized bed 16, and this fine powder is discharged together with the gas from the upper force of the fluidized bed dryer 8, and is collected by the dust collector 11 provided in the exhaust gas pipe 10.
- a binder such as heavy oil is added to the collected fine powder by a binder addition device 18, and after being kneaded and granulated by a kneading granulator 19, it is conveyed to a coke oven by a conveying path (not shown).
- the amount of noda added by the binder addition device 18 is adjusted by the binder addition control device 20.
- the noinder addition control device 20 can be incorporated in the binder addition device 18.
- the binder addition control apparatus 20 is unnecessary.
- the above-described coke oven flue 2 is provided with an exhaust gas flow meter 21, the gas supply pipe 5 is provided with a flow meter 23 and a first control valve 24, and the exhaust gas pipe 10 is provided with a second control valve 25.
- a third control valve 26 is provided in the gas circulation pipe 14.
- the exhaust gas flow meter 21 can estimate the exhaust gas flow rate by calculating the combustion of the coke oven, which is not essential.
- the opening degree or flow rate of the first to third control valves 24 to 26 can be adjusted by the control valve control devices 27 to 29, respectively.
- the mixing ratio of the fine powder recovered by the dust collector 11 and the binder is always set to an optimum ratio by adjusting the binder adding device 18 in accordance with the change in the exhaust gas temperature or flow rate of the coater furnace. To do. A specific description will be given with reference to FIG.
- the amount of fine powder collected by the dust collector 11 also changes.
- a binder necessary for kneading and granulation is added to the collected fine powder.
- the change in the flow rate or temperature of the coke oven exhaust gas is obtained by grasping the amount of fine powder collected by the dust collector 11 that changes with the change in the flow rate or temperature of the coke oven exhaust gas.
- the Noinder adder 18 can be adjusted manually or automatically to keep the mixing ratio of the fine powder discharged from the dust collector 11 and the binder constant. This can prevent problems such as contamination of the conveyance path due to excessive binder, dust generation on the conveyance path due to insufficient binder, or carbon adhesion in the coke oven.
- the coke oven exhaust gas property change can be manually detected and predicted, but the coke oven exhaust gas is also sent to the coke oven exhaust gas property. Is detected by the binder addition control device 20 shown in the figure, such as a signal indicating the increase or decrease in coke oven production, a signal indicating the increase or decrease in calorific value of coke oven fuel, etc. It is also possible to automatically adjust the amount.
- Fig. 2 is a schematic configuration diagram showing another embodiment of the drying apparatus of the present invention.
- the coke oven combustion exhaust gas generated in the coke oven 1 passes through the flue 2 and is emitted from the coke oven chimney 3 to the atmosphere.
- the temperature of the coke oven exhaust gas 4 passing through the flue 2 is about 150 to 250 ° C.
- the coke oven exhaust gas 4 flows through the gas supply pipe 5 branched from the coke oven flue 2, is pressurized by the blower 6, and is then supplied from the lower part of the fluidized bed dryer 8 as the heat source / fluidizing gas 7.
- the exhaust gas 9 discharged from the fluidized bed dryer 8 is dissipated into the atmosphere from the chimney 13 via the dust collector 11 and the professional tank 12 through the exhaust gas pipe 10.
- the gas circulation pipe 14 is branched from the exhaust gas pipe 10, and the tip thereof is connected to the gas supply pipe 5, so that the exhaust gas 9 of the fluidized bed dryer 8 is circulated, and again the fluidized bed dryer 8 It can be used as a fluidizing gas!
- Coal powder as a wet raw material is charged into the fluidized bed dryer 8 by the charging chute 15, and is fluidized by the upward flow of the heat source / fluidizing gas 7 introduced from the lower part of the fluidized bed dryer 8.
- Form 16 In the fluidized bed 16, the coal powder is dried, and the coal powder is adjusted to a predetermined temperature and moisture content, most of which is discharged by the discharge chute 17.
- the coal powder discharged from the discharge chute 17 is transported to the coatus furnace by a transport path (not shown).
- the upper powder of the fluidized bed dryer 8 is discharged together with the gas and is collected by the dust collector 11 provided in the exhaust gas pipe 10.
- the recovered fine powder is calcined with a binder such as heavy oil by a binder addition device 18, and after being kneaded and granulated by a kneading granulator 19, it is conveyed to a coke oven by a conveyance path (not shown).
- the amount of noda added by the binder addition device 18 is adjusted by the binder addition control device 20.
- the noinder addition control device 20 can be incorporated in the binder addition device 18.
- the flue 2 of the coke oven described above is provided with an exhaust gas flow meter 21, the gas supply pipe 5 is provided with a flow meter 23 and a first control valve 24, and the exhaust gas pipe 10 is provided with a second control valve 25.
- a third control valve 26 is provided in the gas circulation pipe 14.
- the exhaust gas flow meter 21 can estimate the exhaust gas flow rate by calculating the combustion of the coke oven, which is not essential.
- the opening degree or flow rate of the first to third control valves 24 to 26 can be adjusted by the control valve control devices 27 to 29, respectively.
- a gas circulation system control device 30 is provided, and the control devices 27 to 29 of the first to third control valves 24 to 26 are given control commands to control the circulating gas amount.
- the coke oven 1 usually has two combustion gas systems for each furnace group, and the usage time in one system reaches a predetermined time. Then, the system is switched to the other system. The system is normally switched once every 15 to 30 minutes.
- the third control valve 26 disposed in the gas circulation pipe 14 is fully closed or slightly opened during steady operation. In other words, if the exhaust gas temperature of the coatus furnace is too high during steady operation, it is effective to lower the gas temperature by mixing the low-temperature circulating gas slightly, and the water content of the supplied coal powder varies. Circulating gas can also be used to adjust the drying capacity.
- the third control valve 26 is fully closed or slightly opened to a certain degree of opening.
- the circulation gas 31 flows through the gas circulation pipe 14 by the action of the blower 6 and the blower 12, and a recycle flow is generated.
- the opening of the first control valve 24 is gradually reduced at a timing when a constant amount of the circulating gas 31 is secured.
- the coke oven exhaust gas 4 that has been supplied to the fluidized bed dryer 8 gradually decreases, and conversely, the flow rate to the coke oven chimney 3 increases.
- the operating speed of the coke oven 1 does not necessarily remain constant.
- the operating status of the coke oven 1 varies depending on the operating condition of the coke oven 1 and the combustion state of the coke oven 1. It is necessary to decide on an individual basis.
- the first to third control valves 24 to 26 are controlled by the control valve control devices 27 to 29 controlling the control valves based on commands from the gas circulation system control device 30.
- the control valve control devices 27 to 29 controlling the control valves based on commands from the gas circulation system control device 30.
- part or all of the gas circulation system control device 30 and the control valve control devices 27 to 29 can be integrated into a single control device.
- Each control valve control device can also be incorporated in each control valve.
- Changing the supply gas to the fluidized bed dryer 8 when the combustion gas system of the coke oven is switched The control is started by receiving a start signal for switching the combustion gas system from the coke oven 1 and the flue 2 It is possible to use a method that starts based on the change in the flow rate of the exhaust gas flow meter 21. Further, as shown in FIG. 3, a prediction signal is received from the coke oven 1 for a predetermined time before the combustion gas system switching is started, and the supply gas change control to the fluidized bed dryer 8 is controlled based on this prediction signal. You can also start. For example, a prediction signal is received one minute before the exhaust gas flow rate becomes zero, and waste recycling via the gas circulation pipe 14 is started. As a result, it is possible to avoid a situation in which the amount of gas supplied to the fluidized bed dryer 8 (heat source / fluidized gas amount) is insufficient due to the dead cycle not being in time.
- the circulating gas 31 used when switching the combustion gas system of the coke oven is the gas after being used for drying the coal powder in the fluidized bed dryer 8, the temperature of the gas naturally depends on the coke oven exhaust gas 4. Low. Therefore, when the combustion gas system of the coke oven is switched, the temperature of the gas flowing into the fluidized bed of the fluidized bed dryer is lowered as shown in FIG. As a result, the dryness of the wet raw material is lowered, and the amount of fine powder generated by drying and collected by the dust collector is reduced.
- the recovered fine powder is added with a binder necessary for kneading and granulation.
- the amount of fine powder decreases when the combustion gas system of the coke oven is switched, the same amount as during steady operation is used.
- the binder becomes excessive.
- the switching of the combustion gas system of the coke oven is detected, and the amount of binder added is reduced after anticipating the reduction in the amount of fine powder (see the bottom row in FIG. 3).
- detection of combustion gas system switching can be performed by receiving a prediction signal from the coke oven a certain time before starting combustion gas system switching.
- the binder addition control device 20 When the binder addition control device 20 receives this prediction signal, it predicts that the amount of fine powder will decrease in t seconds, and the binder addition device 18 uses the binder addition device 18 so that the ratio of fine powder to binder is the same as in steady operation. Decrease the amount of Noinder added. As a result, the fine powder and the binder can always be mixed at a constant rate, and problems such as contamination of the conveyance path due to excessive binder do not occur.
- the detection of switching of the combustion gas system can also be performed by receiving a start signal for switching of the combustion gas system from the coke oven 1. In this case, it takes less time to start adjusting the amount of noinder added compared to detection using a prediction signal, but it can be adequately handled in actual operation.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
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- Drying Of Solid Materials (AREA)
- Coke Industry (AREA)
Abstract
Description
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Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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UAA200712399A UA83979C2 (ru) | 2005-04-08 | 2006-04-04 | Сушилка для влажного сырья и способ сушки влажного сырья (варианты) |
CN2006800114453A CN101155898B (zh) | 2005-04-08 | 2006-04-04 | 湿润原料的干燥装置及干燥方法 |
BRPI0608619-5A BRPI0608619A2 (pt) | 2005-04-08 | 2006-04-04 | secador de matÉria-prima émida e mÉtodo de secagem de matÉria-prima émida |
Applications Claiming Priority (2)
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JP2005112596A JP4787528B2 (ja) | 2005-04-08 | 2005-04-08 | 湿潤原料の乾燥装置及び乾燥方法 |
JP2005-112596 | 2005-04-08 |
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WO2006109629A1 true WO2006109629A1 (ja) | 2006-10-19 |
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JP (1) | JP4787528B2 (ja) |
KR (1) | KR100972707B1 (ja) |
CN (1) | CN101155898B (ja) |
BR (1) | BRPI0608619A2 (ja) |
RU (1) | RU2373256C2 (ja) |
TW (1) | TW200643161A (ja) |
UA (1) | UA83979C2 (ja) |
WO (1) | WO2006109629A1 (ja) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102730252A (zh) * | 2012-06-11 | 2012-10-17 | 张家港市新盛新材料有限公司 | 聚苯硫醚的干燥包装装置 |
CN103663592A (zh) * | 2012-09-13 | 2014-03-26 | 中国辐射防护研究院 | 高含盐无机废水流化处理工艺及系统 |
WO2018152471A1 (en) * | 2017-02-20 | 2018-08-23 | Nous, Llc | Fluidized bed system |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
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KR101116832B1 (ko) * | 2010-06-30 | 2012-02-29 | 한국전력공사 | 석탄 건조 장치 및 이를 포함하는 석탄 고품위화 시스템 |
JP5683380B2 (ja) * | 2011-05-20 | 2015-03-11 | 三菱重工業株式会社 | 流動層乾燥装置 |
JP5410633B1 (ja) * | 2013-06-13 | 2014-02-05 | 新日鉄住金エンジニアリング株式会社 | 乾燥装置及び当該乾燥装置を用いる乾燥方法 |
CN110436464B (zh) * | 2019-06-14 | 2023-06-16 | 阳城县绿色科技研发中心 | 焦炭法二硫化碳生产半自动化烤焦装置 |
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JP2001055582A (ja) * | 1999-08-18 | 2001-02-27 | Nippon Steel Corp | 石炭の乾燥方法及び乾燥装置 |
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CN1020860C (zh) * | 1989-06-20 | 1993-05-26 | 中国科学院化工冶金研究所 | 粉料快速流态化干燥热解制粒的方法和装置 |
CN1104236A (zh) * | 1994-07-17 | 1995-06-28 | 邯郸市煤炭经济技术开发公司 | 型煤(型焦)及其生产方法 |
JP2006232938A (ja) * | 2005-02-23 | 2006-09-07 | Nippon Steel Corp | 湿潤原料の乾燥装置 |
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2005
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2006
- 2006-04-04 BR BRPI0608619-5A patent/BRPI0608619A2/pt not_active IP Right Cessation
- 2006-04-04 RU RU2007141399/15A patent/RU2373256C2/ru not_active IP Right Cessation
- 2006-04-04 WO PCT/JP2006/307135 patent/WO2006109629A1/ja active Application Filing
- 2006-04-04 CN CN2006800114453A patent/CN101155898B/zh active Active
- 2006-04-04 UA UAA200712399A patent/UA83979C2/ru unknown
- 2006-04-04 KR KR1020077025796A patent/KR100972707B1/ko active IP Right Grant
- 2006-04-07 TW TW095112441A patent/TW200643161A/zh not_active IP Right Cessation
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JPS58120690A (ja) * | 1982-01-13 | 1983-07-18 | Nippon Steel Chem Co Ltd | コ−クスの製造法 |
JP2001055582A (ja) * | 1999-08-18 | 2001-02-27 | Nippon Steel Corp | 石炭の乾燥方法及び乾燥装置 |
Cited By (5)
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CN102730252A (zh) * | 2012-06-11 | 2012-10-17 | 张家港市新盛新材料有限公司 | 聚苯硫醚的干燥包装装置 |
CN103663592A (zh) * | 2012-09-13 | 2014-03-26 | 中国辐射防护研究院 | 高含盐无机废水流化处理工艺及系统 |
WO2018152471A1 (en) * | 2017-02-20 | 2018-08-23 | Nous, Llc | Fluidized bed system |
US10690412B2 (en) | 2017-02-20 | 2020-06-23 | Nous, Llc | Fluidized bed system |
US11262128B2 (en) | 2017-02-20 | 2022-03-01 | Nous, Llc | Fluidized bed system |
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JP2006291010A (ja) | 2006-10-26 |
RU2373256C2 (ru) | 2009-11-20 |
BRPI0608619A2 (pt) | 2010-01-19 |
JP4787528B2 (ja) | 2011-10-05 |
TW200643161A (en) | 2006-12-16 |
TWI313295B (ja) | 2009-08-11 |
UA83979C2 (ru) | 2008-08-26 |
RU2007141399A (ru) | 2009-05-20 |
KR100972707B1 (ko) | 2010-07-27 |
KR20070120578A (ko) | 2007-12-24 |
CN101155898B (zh) | 2011-03-23 |
CN101155898A (zh) | 2008-04-02 |
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