EP2891771A1 - Procédé d'enrichissement de lignite brut - Google Patents

Procédé d'enrichissement de lignite brut Download PDF

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Publication number
EP2891771A1
EP2891771A1 EP14185476.0A EP14185476A EP2891771A1 EP 2891771 A1 EP2891771 A1 EP 2891771A1 EP 14185476 A EP14185476 A EP 14185476A EP 2891771 A1 EP2891771 A1 EP 2891771A1
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EP
European Patent Office
Prior art keywords
steam
drying
lignite
coal
jet
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP14185476.0A
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German (de)
English (en)
Other versions
EP2891771B1 (fr
Inventor
Hans Michael Hübner
Ralf Ackermann
Stephan Schwinn
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
RWE Power AG
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RWE Power AG
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Filing date
Publication date
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Publication of EP2891771A1 publication Critical patent/EP2891771A1/fr
Application granted granted Critical
Publication of EP2891771B1 publication Critical patent/EP2891771B1/fr
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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C19/00—Other disintegrating devices or methods
    • B02C19/06—Jet mills
    • B02C19/068—Jet mills of the fluidised-bed type
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
    • F01K17/06—Returning energy of steam, in exchanged form, to process, e.g. use of exhaust steam for drying solid fuel or plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K1/00—Preparation of lump or pulverulent fuel in readiness for delivery to combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K1/00—Preparation of lump or pulverulent fuel in readiness for delivery to combustion apparatus
    • F23K1/04—Heating fuel prior to delivery to combustion apparatus
    • 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
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/148—Injection, e.g. in a reactor or a fuel stream during fuel production of steam
    • 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
    • C10L2290/28—Cutting, disintegrating, shredding or grinding
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2201/00—Pretreatment of solid fuel
    • F23K2201/10—Pulverizing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2201/00—Pretreatment of solid fuel
    • F23K2201/10—Pulverizing
    • F23K2201/103—Pulverizing with hot gas supply
    • 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

Definitions

  • the invention relates to a process for refining crude lignite coal comprising pre-crushing the lignite-like lignite coal and a pre-crushing immediately downstream grinding and drying to dry lignite, wherein extracted from a coupled power plant process with at least one steam generator and at least partially used to dry the lignite coal wet lignite.
  • finishing may include at least the production of a dried, powdery or granular end product, which is supplied to a thermal utilization in a power plant or a further refinement for the enrichment of carbon in the final product.
  • a further finishing step for example, the production of hearth furnace coke, liquefaction, gasification or the production of fuel pellets can be provided.
  • Cryogenic wet lignite in the context of the present invention is to be understood as meaning the lignite mined and not treated, which may have a moisture content of between 40% and 60% by weight, depending on the conditions of the deposit or storage time prior to refining.
  • the raw lignite is usually supplied to a flue gas inerted with flue gas.
  • the raw lignite is crushed in the racket mill.
  • the flue gas is used to dry the wet coal and transported as a carrier gas produced lignite dust through a separator to the burner of the boiler. In that regard, a treatment of the raw lignite to dry lignite is not required.
  • the refining of lignite requires an optionally multi-stage grinding and separate drying of the raw lignite in a separate drying unit.
  • the drying units used are tube dryers, fluidized bed dryers or roller mills.
  • tube dryers and fluidized bed dryers as drying units usually a multi-stage pre-crushing and / or grinding of the raw lignite is provided.
  • fluidized bed dryers can only be operated with a relatively narrow feed grain belt, otherwise the fluidized bed would collapse.
  • the operation of tube dryers is energetically complex. These are usually operated with steam from a coupled power plant process.
  • the specific volume of steam required to operate a tube dryer is about 1.35 kg of steam per kilogram of raw coal.
  • the invention is therefore based on the object to provide a method for refining raw lignite coal comprising crushing and drying the lignite coal to dry lignite, which requires an energetically favorable drying with relatively little equipment expense.
  • a method according to the invention comprises a preliminary comminution of the pit-moist raw lignite coal and a pre-comminution preferably immediately downstream drying to dry lignite, wherein from a coupled power plant process with at least one steam generator steam is taken and this steam is at least partially used for drying the pit-wet raw lignite, the method comprises grinding and drying in a single process step, preferably a fine grinding and drying in a single process step, wherein the still pit-dried pre-broken raw lignite as regrind by means of at least one steam jet from the steam generation, which is introduced into a fluidized bed with fluidized bed, is crushed and broken.
  • a fine grinding and drying is thereby combined in one process step, which results in a considerable energetic optimization of the finishing process.
  • it is provided to use the raw lignite even within a suitably designed aggregate as a grinding body.
  • Mahlgutbett comprising the pre-crushed or pre-shredded raw lignite as regrind
  • entering steam jet interacts with the surrounding fluidized bed such that a momentum exchange between the steam jet and the ground material takes place, resulting in the comminution of the ground material and at the same time to its drying in the Steam atmosphere leads.
  • the steam jet is accelerated into the fluidized millbase bed together with a part of the millbase and, if this is so, that particle collisions occur within the millbase bed.
  • the individual lignite particles are exposed to an impact stress, which leads to a crushing without the use of grinding media or baffle installations within the unit in question.
  • a plurality of steam jets can be introduced in opposite directions in the Mahlgutbett, for example so that steam jets meet.
  • the comminution and drying can be carried out in at least one, preferably in several parallel hydraulic jet mills, preferably in fluidized bed counter-jet mills.
  • a fluidized bed counter-jet mill at least two or more steam jets, each loaded with regrind, are directed against each other to achieve particle collisions to the maximum extent possible.
  • Such comminution is particularly advantageous when the refining process is coupled to a power plant process, in which case suitably conditioned steam from the power plant process or steam generation process is available.
  • a subset of the dry lignite is thermally utilized in the power plant process, wherein the power plant process is otherwise preferably operated with raw lignite as fuel.
  • the steam for example, at a temperature of between 180 ° C and 330 ° C, preferably at a temperature between 200 ° C and 300 ° C and a vapor pressure between 4 bar and 6 bar, preferably introduced with a vapor pressure of 5 bar in the Mahlgutbett become.
  • both water and volatile components of the raw lignite are expelled as fuel gas from the lignite coal during drying, wherein the fuel gas is stored and / or thermally recycled separately.
  • the so-called volatile constituents or volatile gaseous constituents are to be understood as meaning exclusively hydrocarbons, but not the roughly capillary-bound water of the raw lignite coal.
  • a further process variant according to the invention provides that the grinding and drying takes place in two stages, wherein in one stage the grinding and drying by means of at least one jet of steam at a first low temperature and in a second stage by means of at least one jet of steam at a second higher temperature.
  • the low temperature may be on the order of 200 ° C
  • the higher temperature may be on the order of 300 ° C.
  • the dried ground material With an introduction of a steam jet with a temperature of about 200 ° C and a pressure of about 5 bar, only a fine comminution and Drying of the ground material, wherein preferably the dried ground material can then have a residual water content of about 2 wt .-% to 4 wt .-%.
  • the product obtained in this case still comprises appreciable amounts of volatile gaseous constituents.
  • steam at a temperature of about 300 ° C can be supplied, which has an expulsion of the volatile gaseous components from the raw lignite result.
  • volatile constituents may for example be stored separately and / or supplied for thermal utilization.
  • the second stage of the fine grinding and drying is operated as a function of the load of the steam generator.
  • a subset of dry lignite from which the volatile components have been expelled.
  • the volatiles can be compressed in this case as a fuel gas and fed to a natural gas network or a natural gas storage.
  • steam of relatively high energy content is needed, which is no longer available at the turbine power plant for power generation.
  • the partial stream of dry brown coal not supplied for thermal recycling can be coked into hearth furnace coke, for example in a further finishing step, if and insofar as this dry brown coal still contains gaseous volatile constituents. If the volatiles are already completely expelled in the second stage of fine grinding, the finished dried product is already present in the form of a high-quality coke.
  • vapor is provided as steam from a turbine of the coupled power plant process. For example, for this purpose, the steam between low-pressure part and medium-pressure part of a three-stage turbine be tapped.
  • FIG. 1 It is first referred to the FIG. 1 ,
  • FIG. 1 a lignite processing coupled with a power plant process is shown, wherein the refinement comprises a pre-comminution 1 and a fine comminution with drying 2.
  • the pre-crushing 1 for lignite-wet raw lignite can only include the breaking up of mined lignite coal obtained by mining using conventional crusher / pre-shredding systems.
  • the raw lignite may for example have been pre-crushed to a particle size of ⁇ 0 mm and ⁇ 10 mm in the pre-crushing process.
  • the pre-crushed raw lignite may, for example, have a moisture content of 54% by weight.
  • the moisture content is given here only as an example, of course, the moisture content of the raw lignite can vary depending on storage conditions and reservoir conditions.
  • an arrangement of parallel-connected fluidized bed counter-jet mills in which the insert grain from 0 mm to 10 mm to a target grain of ⁇ 1 mm with simultaneous drying to a moisture content of about 2 wt .-% to 3 wt .-% is obtained.
  • a suitable for carrying out the method hydraulic jet mill may, for example, include a Mahlgutraum, dip in the multiple jet pipes. About the jet pipes both a steam injection and possibly the introduction of ground material, which was previously deducted from the Mahlgutbett or a Mahlguteinleinlauf.
  • a Mahlgutaustrag can be done for example via a arranged within the Mahlgutraums classifier.
  • a partial stream A of the comminuted material stream discharged from the fine comminution and drying 2 in the form of dry brown coal is fed to a steam generator 3, which is designed, for example, as a boiler essentially fired with crude lignite coal. It can be provided, for example, that the steam generator 3 is fired to 75% with lignite and 25% with dry lignite.
  • the hot steam generated in the steam generator 3 drives a turbine 4, which in turn drives a generator 5, which feeds into a power grid 6.
  • a further partial stream B of dry lignite is fed to a second finishing stage 7, the aim of which is the production of a high-quality, marketable fuel.
  • a coking, gasification or liquefaction of lignite may be provided as a second upgrading stage 7.
  • a partial stream of steam C is withdrawn from the turbine 4.
  • This partial stream of steam C is introduced according to the invention as a jet of steam in the drying units provided there.
  • this partial stream of steam C is used for fluidizing the Mahlgutbetts provided within the drying units.
  • the steam is withdrawn between the low-pressure part and the medium-pressure part of the turbine 4 at a pressure of about 5 bar at a temperature of about 200 ° C, wherein about 0.95 kg of steam are required per kilogram used as regrind raw lignite.
  • FIG. 2 A variant of this method is in FIG. 2 represented where the same components and the same mass flows are provided with the same names there.
  • FIG. 2 illustrated variant of the method according to the invention differs essentially from the in FIG. 1 illustrated variant that the fine crushing and drying 2 one or more stages, but with a partial flow steam C, is operated, which has a higher energy content or has a higher temperature, namely about 300 ° C at a pressure of about 5 bar.
  • a hydraulic jet mill with steam at a temperature of about 300 ° C at about 5 bar pressure
  • both water and the gaseous volatiles of the lignite coal are expelled from this during comminution in such a way that almost 100% of that contained in the lignite coal Moisture is removed.
  • 100% lignite is used, about 54% by weight of water and 23.5% by weight of methane are produced.
  • a finished product from the fine crushing and drying 2 falls to a coke-like product with an increased carbon content, of which a partial flow A in the steam generator 3 is thermally recoverable, whereas a further partial flow B is obtained as finished finished product.
  • the vapor D from the fine comminution and drying 2 can be condensed in the vapor condenser 8 for the purpose of waste heat utilization, as in the method variant described above.
  • the resulting methane E is first cleaned in a filter 9 and then fed via a compressor 10 in a natural gas network 11.
  • the fine comminution and drying 2 may comprise two grinding and drying stages, wherein in a first stage a fine comminution and drying or grinding and drying with steam of lower energy content may be provided. This can be done, for example, during heavy load periods of the power grid, since in this case the maximum amount of steam on the turbine 4 must be available. At low load periods, a second grinding and drying stage may be provided, which is operated with higher energy content steam, in which case, for example, steam at a temperature of about 300 ° C at the turbine 4 can be tapped. Only in this load case would methane E be expelled from the raw lignite and fed to a separate utilization as fuel gas.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Food Science & Technology (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Drying Of Solid Materials (AREA)
EP14185476.0A 2013-09-20 2014-09-19 Procédé d'enrichissement de lignite brut Active EP2891771B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE201310015579 DE102013015579A1 (de) 2013-09-20 2013-09-20 Verfahren zur Veredelung von Rohbraunkohle

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EP2891771A1 true EP2891771A1 (fr) 2015-07-08
EP2891771B1 EP2891771B1 (fr) 2020-05-20

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116218579B (zh) * 2023-04-24 2023-07-18 羚羊环保科技有限公司 一种高硫高水分褐煤脱硫脱水生产装置

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0888818A1 (fr) * 1997-07-03 1999-01-07 HOSOKAWA ALPINE Aktiengesellschaft Procédé et dispositif de broyage à jet à lit fluidisé
DE10050520A1 (de) * 2000-10-12 2002-04-18 Karl Strauss Verfahren und Vorrichtung zum Betrieb einer Gasturbine
DE102007023336A1 (de) * 2007-05-16 2008-11-20 Rwe Power Ag Verfahren zum Betreiben eines Dampfturbinenkraftwerks sowie Vorrichtung zum Erzeugen von Dampf
WO2012133549A1 (fr) * 2011-03-31 2012-10-04 三菱重工業株式会社 Unité d'alimentation en matériau humide et système de production d'énergie composite par gazéification utilisant ledit matériau humide

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DD283676A5 (de) * 1988-03-03 1990-10-17 Gagarin Hoeeroemue Vallalat,Hu Verfahren zur vorbereitung von braunkohle zwecks weiterer verarbeitung
DE19824062A1 (de) * 1998-05-29 1999-12-02 Roland Nied Mahlverfahren unter Verwendung einer Strahlmühle

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0888818A1 (fr) * 1997-07-03 1999-01-07 HOSOKAWA ALPINE Aktiengesellschaft Procédé et dispositif de broyage à jet à lit fluidisé
DE10050520A1 (de) * 2000-10-12 2002-04-18 Karl Strauss Verfahren und Vorrichtung zum Betrieb einer Gasturbine
DE102007023336A1 (de) * 2007-05-16 2008-11-20 Rwe Power Ag Verfahren zum Betreiben eines Dampfturbinenkraftwerks sowie Vorrichtung zum Erzeugen von Dampf
WO2012133549A1 (fr) * 2011-03-31 2012-10-04 三菱重工業株式会社 Unité d'alimentation en matériau humide et système de production d'énergie composite par gazéification utilisant ledit matériau humide

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DE102013015579A1 (de) 2015-03-26

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