WO2013174828A1 - Verfahren zur aufbereitung von grubenfeuchter rohbraunkohle - Google Patents
Verfahren zur aufbereitung von grubenfeuchter rohbraunkohle Download PDFInfo
- Publication number
- WO2013174828A1 WO2013174828A1 PCT/EP2013/060437 EP2013060437W WO2013174828A1 WO 2013174828 A1 WO2013174828 A1 WO 2013174828A1 EP 2013060437 W EP2013060437 W EP 2013060437W WO 2013174828 A1 WO2013174828 A1 WO 2013174828A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- lignite
- fluidized bed
- dry
- coal
- raw
- Prior art date
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B1/00—Preliminary treatment of solid materials or objects to facilitate drying, e.g. mixing or backmixing the materials to be dried with predominantly dry solids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23K—FEEDING FUEL TO COMBUSTION APPARATUS
- F23K2201/00—Pretreatment of solid fuel
- F23K2201/20—Drying
-
- 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
- F26B3/084—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 with heat exchange taking place in the fluidised bed, e.g. combined direct and indirect heat exchange
Definitions
- the invention relates to a method for the treatment of porridge wet
- Fluidized bed dryer is performed, which with steam as
- Fluidizing medium is operated.
- Fluidized bed is known for example from DE 29 01 723 C2. In the fluidized-bed drying process described therein, it is provided to feed the feed coal to the fluidized-bed dryer by means of a screw conveyor
- the method known from the aforementioned publication is intended to be suitable for drying lumpy materials whose size is in the range of, for example, 0.3 cm to 10 cm.
- the material to be dried for example lignite
- a denser material such as quartz sand.
- the process requires that the dried solid material be in association with a portion of the particulate matter
- the fluid mechanical processes within a stationary fluidized bed are extremely complex and only limitedly simulatable.
- a pilot plant operated by the applicant depending on
- Raw lignite is preferred on the heat exchangers of the fluidized bed dryer. As a result, the heat transfer deteriorates, the performance of the dryer is significantly reduced, in the worst case, the fluidized bed collapses.
- Composition of the raw lignite is dependent.
- the invention is therefore an object of the invention to provide a method for the treatment of gruel wet lignite using at least one indirectly heated fluidized bed dryer, which is a substantially stable and trouble-free fluidized bed operation even at high
- the problem underlying the invention is achieved by a process for the treatment of crude brown lignite, particularly for thermal utilization in a power plant boiler, wherein the raw lignite is first pre-broken and then comminuted in at least one grinder and fed to a subsequent drying, wherein the drying in a fluidized bed is carried out using at least one indirectly heated fluidized bed dryer, which with steam as
- Fluidized medium is operated, wherein the raw lignite is discharged as bulk material having a mean grain diameter d 50 of a maximum of 2 mm in the fluidized bed and wherein the dried lignite behind the
- Fluidized bed dryer a partial flow diverted and the raw lignite is added before drying.
- Ensuring the particle size distribution can be effected, for example, by influencing the rotational speed of one or more mills upstream of the fluidized-bed dryer. For example, as mills
- the particle size distribution is checked by sieving and this can be done daily or batchwise
- the particle size distribution can also be measured volumetrically via an online method.
- the grain size distribution can alternatively be ensured by following the sieving of the dried lignite with a sieve classification, wherein the oversize fraction is screened off and subjected to subsequent grinding.
- the invention is based on the finding that pit-lignite raw lignite, depending on their origin, have a different cohesive behavior which has more or less great influence on the fluidisability of the coal.
- crude lignite is a natural product obtained by mining in terms of water content, carbon content and mineral composition different according to origin. Certain properties of the raw lignite must be taken into account when used as given.
- the applicant was able to find out, for example, that the fluidizability of the raw lignite coal is closely related to its flowability and that the flowability of the raw lignite coal surprisingly is due to
- the raw lignite coal to be dried is provided with the same type of coal in the form of dry brown coal before
- the stability of the treatment process according to the invention in particular the stability of the fluidized bed within the fluidized bed dryer can be surprisingly improved in that a part of the dried
- Lignite is circulated within the process, so that even poorly or not fluidisable raw lignite can be used in this way and at the same time relatively high throughput in the fluidized bed dryer problems and dried.
- Utilization of the fluidized bed dryer Utilization of the fluidized bed dryer. Disturbances of the fluidized bed can occur in particular at a high utilization of the fluidized bed dryer.
- Dry lignite between 10 and 30 ma%, preferably between 10 and 20 ma% based on the total bed mix.
- Dry lignite is regulated depending on the amount of the fluidized bed lignite supplied to the fluidized bed.
- a regulation can be provided in such a way that a specific ratio of dry brown coal to crude lignite is set and the dry lignite is dosed accordingly.
- the raw lignite can have a fluctuating water content / moisture content of up to 65 ma%.
- Dry lignite extracted in the fluidized bed dryer is determined in the hygroscopic area at constant system pressure by the fluidized bed temperature or by the course of the desorption isobars. The from the
- Fluidised bed dryer withdrawn dry lignite can be a medium
- Grain diameter d 50 from 0.4 mm to 0.8 mm, preferably from 0.1 mm to 0.4 mm, optionally also from 0.1 mm to 0.2 mm.
- the moisture content of the dry lignite may be between 10 and 15% by mass, preferably between about 15 and 18% by mass.
- Fluidized bed dryer can be up to 10 bar. Also, the
- Moisture content of the dry lignite coal is between 8 and 20 ma%, preferably between 10 and 16 ma%.
- the fluidized-bed dryer is preferably heated indirectly with steam as the heating medium.
- a part of the dryer vapor or alternatively external steam from a coupled power plant process can be used to fluidize the fluidized bed or the raw lignite coal within the
- Fluidized bed dryer can be used.
- the branched dry lignite can, using at least one mixing device with the raw lignite before task in the
- Fluid bed dryer are intimately mixed. Such mixing is not required under all circumstances, but significantly improves the adhesion of fine dry coal particles to the particles of wet lignite coal used.
- the dry lignite can be cooled behind the fluidized bed dryer and subjected to a post-milling, with a partial stream of dry lignite is diverted behind the post-grinding.
- Raw lignite is added.
- the particle size distribution can also be determined volumetrically by sieve classification, so that, if the particle size distribution differs, the subsequent grinding can be carried out accordingly.
- the reclaimed dry lignite can be added to the lignite coal between two milling stages or behind a final milling stage.
- Raw lignite and dry lignite ensures intimate mixing, so that possibly separate mixing devices are unnecessary. In the sense of a relatively effective or energy-efficient process management, however, it makes sense to recycle as little as possible dry lignite and to keep the route of the retired lignite to be carried too short as possible. However, consideration should also be given to aspects of explosion protection. For the latter reason, it is expedient and useful, the recycled lignite coal behind a Fine grinding the raw lignite this abandon and, for example by means of static or dynamic mixing devices in the supply to
- Fluid bed dryer to perform a mixing with the raw lignite.
- mixing can also be carried out using a conventional method
- Raw lignite and / or the load condition of the fluidized bed dryer is varied.
- the rheology and adhesion characteristics of the coalmine are to a large extent dependent on the compressibility of the raw lignite and hence the bulk density of the lignite coal in the compacted state.
- the bed of raw lignite in the fluidized bed by means of at least one arranged above the fluidized bed rotary Verteilerschurre, preferably according to a predetermined distribution based on the cross-sectional area of the fluidized bed dryer.
- FIG. 1 shows a schematic representation of the method principle of FIG
- Figure 2 a diagram in which the bulk material strength of materials of different flowability in dependence of
- Process principle which is the flow diagram of a fluidized bed drying plant illustrated, for example, to a power plant boiler for
- the lignite coal is ground for fine grinding in two mills arranged one behind the other to an average grain size (d 50 ) of about 0 mm to 2 mm.
- the raw lignite is then fed to a fluidized bed dryer 3 with mixing with dry brown coal, as will be described below.
- the fluidized bed dryer 3 is for example via corresponding
- the steam feed for acting on the heat exchanger is provided with the reference numeral 4 in the process sketch (FIG. 1).
- the fluidized-bed dryer 3 is operated in a known manner under slight overpressure, wherein the raw lignite is fed via a rotary valve, not shown, and via a arranged in the upper part of the fluidized bed dryer 3 Verteilerschurre on the fluidized bed.
- the withdrawn from the fluidized bed dryer 3 vapor 5 is after dedusting in an electrostatic precipitator 6 different others
- Low-temperature heat from the vapor condensation can be coupled, for example, in the boiler feedwater preheating a power plant process.
- the vapor can be further compressed alternatively and returned to the fluidized bed dryer 3 for the purpose of heating.
- the energy from the vapor can also be coupled into an ORC process (organic rankine cycle).
- a partial stream 7 of the vapor 5 is fed to the fluidized-bed dryer 3 as a fluidizing medium.
- withdrawn dry brown coal 8 is first cooled in a cooler 9, then ground in a mill 10 and fed to a dry lignite coal 1 1.
- E1 to E4 E1 denotes a removal point behind the fluidized bed dryer 3 and in front of the cooler 9, E2 denotes a removal point behind the cooler 9 and before the mill 10, E3 denotes a removal point behind a mill 10 and before the dry lignite silo 11.
- E4 finally designates a sampling point behind the dry lignite silo 1 1.
- the recirculating partial stream of dry lignite is taken at E4, since due to the provided in the dry lignite silo 1 1 stocking better dosability of the recirculating partial flow is ensured.
- Thenbraunkohlesilo 1 1 may be provided on the discharge side with a Austragszellenrad which is operable at variable speed.
- the dry lignite silo 1 1 may have two separate dry lignite deductions, one of which for the dry lignite recirculation or
- Dry lignite blending is provided, the other hand, the withdrawal of dry brown coal as a usable product of
- Transport path can also be used to fill the fluidized bed dryer 3 before starting with dry lignite. It is before a first task of raw lignite when commissioning the fluidized bed dryer 3
- Dust from the fluidized bed can compensate and the fluidized bed and all control circuits of the fluidized bed dryer can continue to operate normally.
- the positions R1 to R4 denote possible return points for the
- the recycling point R1 is provided immediately behind the raw coal bunker 1, the return point R2 between a first and a second mill, the return point R3 behind a second mill and before the fluidized bed dryer 3.
- the return point R4 is provided immediately before the fluidized bed dryer 3.
- Fluidisier sadness in the fluidized bed is.
- the flowability of the lignite coal to be introduced into the drying process can be significantly improved.
- Dry lignite hereinafter referred to as TBK 1 to TBK 5
- flowability was determined as a ratio of a solidification stress to a compressive strength.
- Solidification stress and o c the compressive strength can be determined both by means of a known uniaxial compression test and by commercially available ring shear devices.
- a ring shear device is, for example, from Dr. Ing. Dietmar Schulze Bulk Solids Measurement (Ring shear ST-XS) commercially available.
- Dr. Ing. Dietmar Schulze Bulk Solids Measurement Ring shear ST-XS
- the yield strength of bulk material can be classified as follows: ffc ⁇ 1 not flowing
- the bulk material capacity G c as a function of the solidification stress ⁇ for areas of different flowability is shown for example in FIG.
- the samples examined by the applicant were examined at a temperature of about 19 ° C at a relative humidity of about 30% relative humidity.
- the raw lignite sample 2 shows the most unfavorable flow properties.
- the raw lignite sample 2 was then mixed with various proportions of TBK 2 dry lignite (dry lignite from sample 2) in proportions by weight of 5%, 10%, 15% and 20%. Then, the mixture was examined for flowability, the measurement result is shown in Table 2.
- Table 2 Table 2:
- Sample 2 has a particularly low bulk density. This corresponds to the unfavorable flowability for this sample, as indicated in Table 1. If a bulk material has an unfavorable flowability, then the individual particles are not mobile in the bed, so remain cavities and the bulk density is low. Consequently, the samples are compressible, so that the bulk density depends on the load. The greatest compressibility is also found in sample 2.
- the dry lignite also differ significantly in bulk density. However, there is no correlation between the raw lignite and the dry lignite, a low bulk density of Raw lignite does not necessarily mean a low bulk density of dry lignite.
- the dry lignite are only very small to measurable compressible in the considered range of solidification stress. As the proportion of dry lignite increases, both the bulk density and the bulk density increase below a solidification stress of approximately 4 kPa. This is consistent with the better flow resistance
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Drying Of Solid Materials (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP13724262.4A EP2852799B1 (de) | 2012-05-23 | 2013-05-22 | Verfahren zur aufbereitung von grubenfeuchter rohbraunkohle |
CA2872454A CA2872454C (en) | 2012-05-23 | 2013-05-22 | Process for the beneficiation of pit-moist raw brown coal |
AU2013265332A AU2013265332B2 (en) | 2012-05-23 | 2013-05-22 | Method for processing pit-moist raw brown coal |
CN201380026540.0A CN104334989B (zh) | 2012-05-23 | 2013-05-22 | 用于对矿湿性原褐煤进行选矿的方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102012010078A DE102012010078A1 (de) | 2012-05-23 | 2012-05-23 | Verfahren zur Aufbereitung von grubenfeuchter Rohbraunkohle |
DE102012010078.7 | 2012-05-23 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2013174828A1 true WO2013174828A1 (de) | 2013-11-28 |
Family
ID=48470981
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2013/060437 WO2013174828A1 (de) | 2012-05-23 | 2013-05-22 | Verfahren zur aufbereitung von grubenfeuchter rohbraunkohle |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP2852799B1 (de) |
CN (1) | CN104334989B (de) |
AU (1) | AU2013265332B2 (de) |
CA (1) | CA2872454C (de) |
DE (1) | DE102012010078A1 (de) |
WO (1) | WO2013174828A1 (de) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103880261A (zh) * | 2014-03-18 | 2014-06-25 | 嘉兴绿方舟环保技术有限公司 | 一种循环流化床风干系统 |
CN105157353A (zh) * | 2015-03-06 | 2015-12-16 | 中昊晨光化工研究院有限公司 | 一种ptfe悬浮树脂的干燥系统及方法 |
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US4422846A (en) * | 1980-09-17 | 1983-12-27 | Firma Carl Still Gmbh & Co. Kg | Method and apparatus for indirectly drying and preheating fine material |
DD232338A1 (de) * | 1984-08-28 | 1986-01-22 | Orgreb Inst Kraftwerke | Verfahren und anordnung zur aufbereitung fester feuchter brennstoffe |
DE2901723C2 (de) | 1978-02-10 | 1986-04-17 | Monash University, Clayton, Victoria | Verfahren und Vorrichtung zum Trocknen eines Feststoffmaterials |
DE19618880A1 (de) * | 1996-05-10 | 1997-11-13 | Rheinische Braunkohlenw Ag | Verfahren zum Aufbereiten von Braunkohle |
DE19620047A1 (de) | 1996-05-18 | 1997-11-20 | Rheinische Braunkohlenw Ag | Verfahren und Vorrichtung zum Trocknen von Braunkohle |
EP1944544A2 (de) * | 2007-01-12 | 2008-07-16 | RWE Power Aktiengesellschaft | Kleinstückiger Brennstoff aus Braunkohle sowie Verfahren zu dessen Herstellung |
DE102010003612A1 (de) * | 2010-04-01 | 2011-10-06 | Brandenburgische Technische Universität Cottbus | Verfahren und Vorrichtung zum Trocknen von Kohle |
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JPS5458601A (en) * | 1977-10-20 | 1979-05-11 | Nagata Seisakusho Co Ltd | Drying of lignite |
DD244044A3 (de) * | 1982-12-06 | 1987-03-25 | Bkw Geiseltal Veb | Verfahren zur behandlung oberflaechenfeuchter rohbraunkohle |
DD264970A1 (de) * | 1987-11-24 | 1989-02-15 | Orgreb Inst Kraftwerke | Verfahren zum besseren vermischen von oberflaechenfeuchtem eintragsschuettgut in eine wirbelschicht |
DD279937B5 (de) * | 1989-02-06 | 1993-08-19 | Ver Energiewerke Ag | Vorrichtung zur trocknung, mahlung und verbrennung ballastreicher brennstoffe |
DE4409056C2 (de) * | 1994-03-11 | 1998-03-26 | Ver Energiewerke Ag | Verfahren und Anordnung zum Vortrocknen von gebrochener Rohbraunkohle für eine druckaufgeladene Wirbelschichtfeuerung |
DE19612187C2 (de) * | 1996-03-27 | 2001-11-15 | Bbp Energy Gmbh | Verfahren zur Zerkleinerung und Trocknung von Braunkohle |
CN2494964Y (zh) * | 2001-08-11 | 2002-06-12 | 哈尔滨工业大学达通热能工程有限公司 | 全自动高水分原煤流化床干燥设备 |
EP2350239B1 (de) * | 2008-11-24 | 2018-03-28 | RWE Power Aktiengesellschaft | Verfahren zur aufbereitung von braunkohle |
CN101581533B (zh) * | 2009-06-04 | 2010-10-06 | 山东天力干燥设备有限公司 | 过热蒸汽褐煤预干燥装置及其工艺 |
DE102010003613A1 (de) * | 2010-04-01 | 2011-10-06 | Brandenburgische Technische Universität Cottbus | Verfahren und Vorrichtung zum Trocknen von Kohle |
CN201871393U (zh) * | 2010-10-27 | 2011-06-22 | 丁钟宇 | 煤泥破碎搅拌机 |
CN102353237B (zh) * | 2011-08-18 | 2013-12-11 | 西安交通大学 | 一种集成于火力发电厂的高水分褐煤预干燥方法和系统 |
-
2012
- 2012-05-23 DE DE102012010078A patent/DE102012010078A1/de not_active Withdrawn
-
2013
- 2013-05-22 AU AU2013265332A patent/AU2013265332B2/en not_active Ceased
- 2013-05-22 CN CN201380026540.0A patent/CN104334989B/zh not_active Expired - Fee Related
- 2013-05-22 CA CA2872454A patent/CA2872454C/en not_active Expired - Fee Related
- 2013-05-22 EP EP13724262.4A patent/EP2852799B1/de not_active Not-in-force
- 2013-05-22 WO PCT/EP2013/060437 patent/WO2013174828A1/de active Application Filing
Patent Citations (7)
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DE2901723C2 (de) | 1978-02-10 | 1986-04-17 | Monash University, Clayton, Victoria | Verfahren und Vorrichtung zum Trocknen eines Feststoffmaterials |
US4422846A (en) * | 1980-09-17 | 1983-12-27 | Firma Carl Still Gmbh & Co. Kg | Method and apparatus for indirectly drying and preheating fine material |
DD232338A1 (de) * | 1984-08-28 | 1986-01-22 | Orgreb Inst Kraftwerke | Verfahren und anordnung zur aufbereitung fester feuchter brennstoffe |
DE19618880A1 (de) * | 1996-05-10 | 1997-11-13 | Rheinische Braunkohlenw Ag | Verfahren zum Aufbereiten von Braunkohle |
DE19620047A1 (de) | 1996-05-18 | 1997-11-20 | Rheinische Braunkohlenw Ag | Verfahren und Vorrichtung zum Trocknen von Braunkohle |
EP1944544A2 (de) * | 2007-01-12 | 2008-07-16 | RWE Power Aktiengesellschaft | Kleinstückiger Brennstoff aus Braunkohle sowie Verfahren zu dessen Herstellung |
DE102010003612A1 (de) * | 2010-04-01 | 2011-10-06 | Brandenburgische Technische Universität Cottbus | Verfahren und Vorrichtung zum Trocknen von Kohle |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103880261A (zh) * | 2014-03-18 | 2014-06-25 | 嘉兴绿方舟环保技术有限公司 | 一种循环流化床风干系统 |
CN103880261B (zh) * | 2014-03-18 | 2015-11-18 | 嘉兴绿方舟环保技术有限公司 | 一种循环流化床风干系统 |
CN105157353A (zh) * | 2015-03-06 | 2015-12-16 | 中昊晨光化工研究院有限公司 | 一种ptfe悬浮树脂的干燥系统及方法 |
Also Published As
Publication number | Publication date |
---|---|
CN104334989A (zh) | 2015-02-04 |
CN104334989B (zh) | 2016-08-17 |
CA2872454C (en) | 2019-10-08 |
DE102012010078A1 (de) | 2013-11-28 |
EP2852799B1 (de) | 2018-11-21 |
EP2852799A1 (de) | 2015-04-01 |
CA2872454A1 (en) | 2013-11-28 |
AU2013265332A1 (en) | 2014-12-04 |
AU2013265332B2 (en) | 2017-06-29 |
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