EP2886190A1 - Procédé et dispositif destinés au déchargement d'impuretés - Google Patents

Procédé et dispositif destinés au déchargement d'impuretés Download PDF

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Publication number
EP2886190A1
EP2886190A1 EP14199061.4A EP14199061A EP2886190A1 EP 2886190 A1 EP2886190 A1 EP 2886190A1 EP 14199061 A EP14199061 A EP 14199061A EP 2886190 A1 EP2886190 A1 EP 2886190A1
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EP
European Patent Office
Prior art keywords
impurities
gasification agent
container
contaminants
nozzle bottom
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
EP14199061.4A
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German (de)
English (en)
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EP2886190B1 (fr
Inventor
Jan Armin Krueger
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.)
SYNCRAFT ENGINEERING GmbH
Original Assignee
Syncraft Engineering GmbH
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Filing date
Publication date
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Publication of EP2886190A1 publication Critical patent/EP2886190A1/fr
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Publication of EP2886190B1 publication Critical patent/EP2886190B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • C10J3/523—Ash-removing devices for gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0943—Coke

Definitions

  • the present invention relates to a method and a device for discharging contaminants from a carburettor for carbonaceous material, in particular a fluidized bed gasifier or floating bed reactor.
  • the fluidized bed gasification describes a stepped gasification process in which, after pyrolysis or carbonization of a carbonaceous material to a type of coke as complete as possible gasification of the coke produced takes place together with a pyrolysis gas in a suspended bed reactor in a so-called.
  • a fluidized bed reactor comprises an adjoining an inlet and a frustoconical widening region, which merges into a cylinder section end provided with an outlet.
  • This body contains a fixed bed held in the influx of a gasifier which is formed from coke from the previous pyrolysis process.
  • This coke is held in suspension by an appropriate introduction and metering of a gasification agent, such as air, in an elevated position and continuously reacted or gasified in a product gas.
  • impurities in the form of, for example, stones, sand grains, slags, nails, other metal parts or the like are present in the suspended bed reactor in the course of suspended bed gasification. accumulate.
  • impurities are usually supplied unnoticed through the carbonaceous input material, since they are partially enclosed or enclosed in mechanically shredded or shredded tree parts of organic material, for example. Accumulations of impurities of the above-exemplified species can reduce the efficiency of the plant and in the long term by agglomeration or even malfunction lead, in particular to blockages or mechanical damage within the suspended bed reactor.
  • the invention is based on the essential finding that impurities always have a higher density than a coke to be reacted in the suspended bed reactor over time or as the conversion or gasification of the coke fraction progresses.
  • a device can be used in an adapted manner, which is known as gravitational or air classifier in particular from grain mills ago, even if there carry out the chaff and if possible only a flour body of a grain of further processing is supplied. It was therefore found to be crucial that a layer formed as possible as a fixed bed within the gasification reactor is lifted from an inlet area, ie in the full sense of the word really "floats" on the gas flow, as in the floating bed gasification according to the disclosure of DE 10 2007 012 452 A1 the case is.
  • a method according to the invention is characterized in that charred biomass in the influx of the gasification agent as a fixed bed in the suspended bed reactor suspended and below this airfoil sinking contaminants substantially against an influx of gasification agent into a room or otherwise moved in particular by gas flows which is used to collect the contaminants and is designed accordingly. According to the invention, contaminants can thus be removed substantially continuously without having a negative effect on a quantity of gas produced, its quality or an overall efficiency of a plant.
  • prepared bio-material to be reacted is fed from below or at a lowest point in a gasification reactor with a mechanical device at the point where impurities could settle and accumulate.
  • a selective removal of impurities in a manner described herein is thus not possible in principle.
  • the gasification agent is introduced through a nozzle bottom into an inlet region below the reduction unit and from there introduces coke to the reduction unit.
  • removal of contaminants from an inlet region is performed continuously in the sense that no interruption of ongoing operation of the overall device is made. Accordingly, the above-mentioned space is used for accumulating and also discharging accumulated impurities.
  • the nozzle bottom is moved between at least two positions using a lifting means to selectively discharge collected contaminants, in particular by using a ramp in pressure-tight and lockable container inside.
  • An inflow of the gasification agent into the inlet region is preferably largely stopped off in the nozzle bottom lowered or displaced for targeted removal of contaminants and a fixed bed in the suspended bed reactor then suspended by a gasification agent introduced into the reduction unit via a nozzle unit.
  • An apparatus for achieving the above-mentioned object is characterized in that charred biomass is arranged in the influx of the gasification agent held as a fixed bed within the levitation of suspended air and below the fixed bed, a space for collecting impurities is provided.
  • charred biomass is arranged in the influx of the gasification agent held as a fixed bed within the levitation of suspended air and below the fixed bed, a space for collecting impurities is provided.
  • the container is separated from the inlet region by a baffle plate, which only allows an opening for the entry of contaminants from the inlet region and in particular from a nozzle bottom into the container.
  • a baffle plate which only allows an opening for the entry of contaminants from the inlet region and in particular from a nozzle bottom into the container.
  • an opening slit is arranged behind the baffle plate, which is designed for discharging accumulated impurities via a ramp in a particular separately lockable container inside.
  • adjacent to the inlet area provided by a gasifying agent nozzle bottom is provided, in particular for targeted removal of accumulated impurities between two positions by a lifting means or other drive means movable and in particular lowering, pivoting and / or rotatable or in other Way is designed to be displaced.
  • a nozzle bottom is connected to slides and a drive means such that, in the course of a displacement of the nozzle base, at the same time a supply of biomass is completed and at least one discharge for contaminants is opened.
  • a one-piece structural unit is formed from a nozzle bottom, a slide as a closure of a biomass supply and a closure solid discharge to a ramp out through another slide and an opening arranged to shift in the opening or a hole for selectively opening a solid Exit to the ramp. From this arrangement results in a reduced travel .DELTA.h this unit compared with a nozzle bottom alone.
  • only one drive is needed.
  • the nozzle bottom adjoining the inlet region, in the connection for the gasification agent is designed to be inclined on one side. Based on this feature is the nozzle bottom for discharging collected impurities in an embodiment of the invention, as it were inclined a chute, wherein the chute is in a second position of the nozzle bottom substantially aligned with a ramp which is connected to a collecting container.
  • At least one of the aforementioned containers has level indicators or a window for optical inspection and, accordingly, a filling of at least one of the containers is monitored by sensors.
  • FIG. 11 shows one from the DE 10 2007 012 452 A1 , to which reference is hereby fully made, known device 1 for the fluidized bed gasification of a carbonaceous material or biomass as a complete system in a sectional view.
  • a biomass B which is usually prepared by comminution and separation of foreign substances, into a pyrolysis unit 2 with gas nozzles 3, from there via an oxidation unit or transport path 4 with nozzle unit 5 to the outlet of a product gas P from a reduction unit 6, which is provided here for the introduction and metering of gasification agent V with a nozzle unit 7.
  • the reduction unit 6 here comprises a nozzle section 7 for supplying gasification agent V, a first section 8, which widens approximately frustoconically, into a cylinder section 9 terminates, which expires via a now frusto-conical tapered portion 10 in an outlet 11 for product gas P out.
  • a normal degree of filling of the reduction unit 6 with a bed of coke pieces in the form of a fixed-bed floating layer 12 shown hatched here is shown in FIG FIG. 11 indicated. This level is monitored with a distance sensor 13 for filling level measurement of the floating layer 12 from Koks Suitechen.
  • the floating layer 12 builds up quite quickly after starting up the device 1 described above in the reactor 12, whereby the entire system 1 then operates in a fundamentally stable production mode.
  • biomass B is charred to a coke material K.
  • a screw conveyor then takes place a controlled supply of this coke material K, which is registered under the action of gaseous gasification agent V via an inlet region 14 in the reduction unit 6.
  • an entry of coke material K into the reduction unit 6 and the conversion of coke material K in the floating layer 12 are in equilibrium.
  • the fixed bed 12 is lifted from the supply of Koks Suitechen from the pyrolysis reactor 2 within the frusto-conically extending first portion 8 of the reduction unit 6 of the inlet portion 14.
  • a zone is formed in which contaminants or slag, which are not carried along by the upwardly directed flow, accumulate against the flow direction at the lowest point of the reduction unit 6.
  • upstream process stages such as the initial charging of the device 1 with biomaterial B or the pyrolysis in the pyrolysis unit 2, have the impurities have not yet shown any process-relevant disadvantages or they have not even been present in particular in the form of slags.
  • Embodiments of the present invention will now be described with reference to other figures, which in particular use the advantageous properties of a floating bed method outlined above to carry out a removal of contaminants from an inlet area continuously in the sense that no interruption of ongoing operation of the overall device must be made , In this case, a disturbance caused above, for example, by a blockage within the reduction unit 6 is excluded as far as technically possible.
  • a preparation of a biomass B the above with reference to the figure of FIG. 11 described overall system 1 is supplied, no stricter requirements, so there are no additional costs.
  • all exemplary embodiments described below can be retrofitted in existing systems or floating layer reduction units 6 and corresponding control and control methods can be expanded.
  • FIG. 1 shows a sectional view of a section of a reduction unit 6 around an inlet region 14 according to a first embodiment of the invention.
  • the inlet area 14 is here opposite to the representation of FIG. 11 has been modified so that gasification agent V instead of an annular nozzle unit 7 here now the gasification agent V is flowed through a port 15 at the inlet portion 14 parallel to a central axis M of the reduction unit 6 and against gravity.
  • the transport unit 4 is arranged at the inlet region 14, via which new coke material K is supplied.
  • a spiral or screw conveyor for needs-based dosage zussender in previous sections of an overall system according to FIG. 11 used to coke charred biomass K.
  • the coke K is introduced into the reduction unit 6 in the inlet region 14 in the inflow of the gasification agent V substantially perpendicularly and counter to the force of gravity.
  • the coke particles are held as a fixed bed 12 in suspension and progressively converted into product gas P.
  • the reduction unit 6 again and enter the inlet area 14 again, where they are prevented by a nozzle plate 16 at a further decrease. From the nozzle bottom 16, the accumulating impurities S then migrate over time into a container 17 running essentially perpendicular to the direction of the gas flow V as a space for accumulating impurities S.
  • An effective removal of contaminants S from the inlet region 14 takes place adjacent in a space formed as a gas-tight container or a container 17, which basically dispenses with the use of a lock, which always represents a potential vulnerability in a device can.
  • the size of the container 17 is chosen so that an emptying should normally take place only every 100 hours of operation, especially in the course of an inspection of the entire system, which of course depends on the amount of impurities contained in a carbonaceous starting material S.
  • the container 17 is separated from the inlet region 14 by a baffle plate 18, which has only one opening 19 for the entry of impurities S from the inlet region 14 and in particular of the from the nozzle bottom 16 forth in the container 17 allows.
  • the container 17 is in the embodiment of FIG. 1 expanded beyond an indicated flange connection and constructed in several parts.
  • the baffle plate 18 By means of the baffle plate 18, the container 17 is separated from the inlet region 14 except for an opening 19 which runs approximately radially with respect to a subsequent tube contour and behind which contaminants S accumulate.
  • FIG. 2 shows the baffle plate 18 in a perspective view as a detail of the cylinder jacket of the inlet portion 14, indicating the mounting position resulting in the opening 19, which may be crescent-shaped.
  • a height b of about 20 mm can be seen, for discharging accumulated impurities S via a ⁇ at an angle of about 30 ° to about 45 ° inclined ramp 21 in a lockable container 22 inside, see FIG. 1 .
  • This entire container arrangement is pressure-tight. It is also pressure-tight connected to the inlet region 14.
  • a shut-off device 23 designed here in the form of a ball valve, the container 22 can be filled with accumulated impurities S.
  • the container can be removed or emptied by opening and connected again pressure-tight.
  • FIG. 3 shows a section of a reduction unit 6 according to a second embodiment of the invention in section analogous to the representation of FIG. 1
  • the basic principle of operation remains the same, only the type, location and removal of stored impurities S have been changed here for a discontinuous removal of accumulated impurities S.
  • the nozzle bottom 16 adjoining the inlet region 14 in the connection 15 for the gasification agent V is designed to be inclined on one side at an angle ⁇ of approximately 10 ° to approximately 45 °, but gas medium V continues to flow vertically from below.
  • This arrangement is again designed to be pressure-tight.
  • FIG. 1 shows a section of a reduction unit 6 according to a second embodiment of the invention in section analogous to the representation of FIG. 1
  • the nozzle plate 16 can be moved between the described position and at least one second position by a lifting means 27 by a height ⁇ h of about 30 cm here.
  • the nozzle bottom 16 is in alignment with the ramp 25 in such a way that contaminants S accumulated on the nozzle bottom 16 slide over the ramp 25 into the container 26.
  • a ball valve 28 is provided so that the container 26 could also be opened or removed for emptying.
  • both embodiments have in common that discharge of contaminants S out of the inlet region is carried out continuously in the sense that no interruption of ongoing operation of the overall device has to be undertaken. Accordingly, the above-mentioned space 17, 26 is used for accumulating and also discharging accumulated impurities S.
  • a significant advantage of this second embodiment over the first embodiment lies in the fact that here an entire cross-sectional width of the upwardly directed reactor is opened down and thus impurities in the form of larger pieces can be removed, and that due to the pressure-tight design even during the current Operation of the entire system.
  • the nozzle base 16 is designed so that it can be changed in the vertical position, without causing the supply of gasification agent V must be interrupted.
  • a "runoff" accumulated impurities S in the gas-tight container 26 are made easier with the nozzle bottom 16 down under the action of gravity.
  • FIG. 4 shows a sectional view of an arrangement according to a combination of a slightly modified first and the second embodiment of the invention analogous to the representations of FIGS. 1 and 3 . It has been found in experiments using a combination Störstoff-collectors according to the first and the second embodiment that in the variant of FIG. 3 when comparatively "large" impurities S are removed, behind an inner contour or the baffle plate 18 accumulates impurities in the form of ash, as the skilled person usually knows only of combustion processes. However, a continuous withdrawal even of such ash shares also reduces the possibility of forming larger clutter by agglomeration within the described device in addition.
  • an arrangement according to FIG. 5 as a substantially pure combination of the first and the second embodiment of the invention analogous to the representation of FIG. 1
  • it is particularly suitable to separate ash-like contaminants S as well as comparatively "large" contaminants S in larger quantities in an uninterruptible long-term operation and to remove them from the device without the need for an interruption of operation.
  • a check of corresponding inspection openings or windows on the containers 17, 22, 26 can be included in the routine of a routine inspection.
  • a filling of the container 17 and / or 22 and / or 26 is monitored by sensors. When a certain filling limit is reached, a corresponding message is then automatically sent to a plant operator.
  • FIG. 6 a sectional view of the section around the reduction unit 12 according to the embodiment of figure 4 as a variant with features that are applicable to all the above embodiments in an adapted manner:
  • a gas-permeable closure is provided in the transport path 4 from the oxidation unit, here indicated as a lowerable bulkhead 29 for the safe retention of coke material K slipping out of the transport path 4 into the inlet region 14.
  • a gas-permeable closure is provided in the transport path 4 from the oxidation unit, here indicated as a lowerable bulkhead 29 for the safe retention of coke material K slipping out of the transport path 4 into the inlet region 14.
  • a nozzle unit 7 for introducing and metering gasification agent V1 directly into the reduction unit 6 is provided.
  • a nozzle unit 7 for introducing and metering gasification agent V1 directly into the reduction unit 6 is provided.
  • FIG. 7 shows a sectional view of a fourth embodiment of the invention analogous to the representation of FIG. 1 .
  • This fourth embodiment of the invention provides an alternative to the embodiment according to FIG. 3 is that here now a displacement of the nozzle base 16 no longer substantially parallel to the central axis M, but substantially perpendicular this is done by a Verschiebe shimmere ⁇ b from here about 125 mm.
  • An accumulation of impurities S located on the nozzle bottom 16 is effected in the course of the displacement caused by the lifting means 27 or by a substantially in one plane pivoting of the nozzle bottom 16 by an amount under the action of gravity against the influx of gasification agent V to the blocking means 23rd passed into the gas-tight container 26 as now absolutely deepest point of this part of the plant. That already with reference to the figure of FIG. 6 described gas-permeable bulkhead 29 during this process certainly prevents any slipping of coke K out of the transport unit 4 into the inlet region 14.
  • a wiper AB indicated only in terms of its position can effectively support removal or stripping of accumulated contaminant S from the nozzle base 16 in the course of the displacement movement.
  • FIG. 8a shows an adaptation of the embodiment of FIG. 7
  • the nozzle bottom 16 is now part of a cylindrical body 30, which is now rotatably supported in the region A with the connection 15 for gasification agent V in the inlet region 14.
  • the gasification agent V flows through the nozzle bottom 16, as already known.
  • a curvature of the nozzle plate 16 causes over the preceding embodiments, no significant difference in function and accumulation of impurities S.
  • the cylindrical body 30 is now rotated by about 90 °, so fall on the nozzle bottom 16 accumulated impurities S through a through recess 31 and a Pipe section 32 passes into the container 26 arranged below.
  • FIGS. 8a shows this cylindrical body 30 with cylindrical continuous and closed recess 31 with the adjoining, continuous pipe section 32 for clarity in three-dimensional View with all hidden edges.
  • the sequence of figures of FIGS. 8b to 8e shows a rear view through the cylindrical recess 31 in the direction of the curved nozzle bottom 16, followed by a representation of the first figure 90 ° tilted body 30 in which now the through recess 31 is connected to the inlet portion 14 with a view through the pipe section 32 therethrough , where d denotes a diameter of the through-hole 31 within the cylindrical body 30, which corresponds to a free cylindrical width in the region of the connection 15 and of the inlet region 14, with a side view in FIG FIG. 8d ..
  • This width d is in the described system about 115 mm, but it is to be adapted in the expert dimensions to a respective size of plant. See the side-by-side side view of the cylindrical body 30. In a final sketch, see FIG. 8e a plan view corresponding to the rear view of the curved nozzle bottom 16 is shown.
  • FIG. 9 builds on the of FIG. 3 and takes into account the possibility of isolating the coke entry, as in FIG. 6 indicated.
  • the ramp 25 is moved up to the discharge of impurities S approximately at the height of the transport path for the entry of coke K up.
  • the nozzle base 16 is integrated into a one-piece structural unit, here as an obliquely opposite to a central axis plane, for example, welded.
  • the structural unit is designed as a hollow cylindrical section 33 in the cylindrical inlet region 14 displaceable.
  • the cylindrical section 33 further comprises a slide 34 as a closure for the supply of biomass K and a further slide 35 as a closure of solids discharge to the ramp 26 out.
  • an opening 36 is provided as a hole in the cylindrical portion 33. Through this opening 36 is in the course of a displacement of the section 33 by an amount .DELTA.h access to the ramp 26 for removal of contaminant S from the nozzle plate 16 is opened, wherein at the same time each supply of biomass K is interrupted by the slide 34 as a closure. Thus, in principle, no biomass K reach the ramp 26 via the inlet region 14, or mix with impurities S in any conceivable manner.
  • the lateral sectional view of the cylindrical portion 33 of FIG. 10a illustrates how a switchover is effected by appropriate design of the slide 34, 35 and arrangement of the opening 36 in the direction of displacement, see also FIG. 10b in a 90 ° rotated side view.
  • a travel .DELTA.h the nozzle plate 16 is reduced and thus the overall design has been shortened.
  • only one drive is used for closing a supply of biomass K together with a displacement of the nozzle plate 16.
  • connection around the inlet region 14 can be modified in a manner which is obvious to a person skilled in the art in order to be able to meet in particular space requirements. Also, for example, with regard to the embodiment according to FIG. 5 be considered that, shifting the branch with the ramp 25, the two containers are merged into a container, which is then also operated via only one closure means operable.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Processing Of Solid Wastes (AREA)
EP14199061.4A 2013-12-18 2014-12-18 Procédé et dispositif destinés au déchargement d'impuretés Active EP2886190B1 (fr)

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ATGM50176/2013U AT14489U1 (de) 2013-12-18 2013-12-18 Verfahren und Vorrichtung zum Austragen von Störstoffen

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EP2886190A1 true EP2886190A1 (fr) 2015-06-24
EP2886190B1 EP2886190B1 (fr) 2020-07-15

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3333249A1 (fr) * 2016-08-03 2018-06-13 Manfred Rosenkranz Procédé et dispositif de liquéfaction à courte distance de la biomasse et des substances organiques similaires (des composés hydrocarbonées)
EP3819359A1 (fr) 2019-11-08 2021-05-12 SynCraft Engineering GmbH Procédé et dispositif de réglage du niveau de remplissage dans un réacteur à lit flottant
CN116064155A (zh) * 2021-11-01 2023-05-05 中国石油化工股份有限公司 一种汽油深度脱硫的方法和系统

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WO2008110383A2 (fr) * 2007-03-15 2008-09-18 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Gazéificateur
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CN201151710Y (zh) * 2007-10-27 2008-11-19 太原海力丰科技发展有限公司 分级煤气化装置
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GB673648A (en) * 1948-01-08 1952-06-11 Directie Staatsmijnen Nl Improvements in or relating to the conversion of finely divided solid carbonaceous material into gas mixtures
US4023280A (en) * 1976-05-12 1977-05-17 Institute Of Gas Technology Valve for ash agglomeration device
US4308806A (en) * 1978-04-05 1982-01-05 Babcock-Hitachi Kabushiki Kaisha Incinerator for burning waste and a method of utilizing same
GB2077614A (en) * 1980-06-16 1981-12-23 Ahlstroem Oy Fluidized bed combuster
US5158449A (en) * 1991-01-08 1992-10-27 Institute Of Gas Technology Thermal ash agglomeration process
WO2008110383A2 (fr) * 2007-03-15 2008-09-18 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Gazéificateur
DE102007012452A1 (de) 2007-03-15 2008-09-25 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Vergaser
WO2010046222A2 (fr) 2008-10-23 2010-04-29 Burkhardt Gmbh Procédé et dispositif pour la gazéification thermochimique de combustibles solides
DE102009047445A1 (de) 2009-12-03 2011-06-09 Burkhardt Gmbh Anlage zum Erzeugen eines Produktgases aus organischen Einsatzstoffen

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EP3333249A1 (fr) * 2016-08-03 2018-06-13 Manfred Rosenkranz Procédé et dispositif de liquéfaction à courte distance de la biomasse et des substances organiques similaires (des composés hydrocarbonées)
EP3819359A1 (fr) 2019-11-08 2021-05-12 SynCraft Engineering GmbH Procédé et dispositif de réglage du niveau de remplissage dans un réacteur à lit flottant
US11583815B2 (en) 2019-11-08 2023-02-21 Syncraft Engineering Gmbh Process and apparatus for adjusting the filling level in a floating bed reactor
CN116064155A (zh) * 2021-11-01 2023-05-05 中国石油化工股份有限公司 一种汽油深度脱硫的方法和系统

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AT14489U1 (de) 2015-12-15

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