EP2862914A1 - Procédé de réglage destiné au fonctionnement d'un gazéificateur à lit mobile et d'un réacteur à lit mobile - Google Patents

Procédé de réglage destiné au fonctionnement d'un gazéificateur à lit mobile et d'un réacteur à lit mobile Download PDF

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Publication number
EP2862914A1
EP2862914A1 EP20140189101 EP14189101A EP2862914A1 EP 2862914 A1 EP2862914 A1 EP 2862914A1 EP 20140189101 EP20140189101 EP 20140189101 EP 14189101 A EP14189101 A EP 14189101A EP 2862914 A1 EP2862914 A1 EP 2862914A1
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EP
European Patent Office
Prior art keywords
fluidized bed
gasification agent
bed reactor
bed
control method
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.)
Pending
Application number
EP20140189101
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German (de)
English (en)
Inventor
Georg Kreutner
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
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Syncraft Engineering GmbH filed Critical Syncraft Engineering GmbH
Publication of EP2862914A1 publication Critical patent/EP2862914A1/fr
Pending legal-status Critical Current

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Classifications

    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10J3/482—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
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam

Definitions

  • the present invention relates to a control method for operating a fluidized bed gasifier and a correspondingly designed device in the form of a fluidized bed reactor.
  • the fluidized bed gasification describes a stepped gasification process in which after complete pyrolysis or carbonization of a carbonaceous material as complete as possible gasification of the coke produced takes place together with a pyrolysis gas in a fluidized bed reactor in a so-called.
  • This fluidized bed reactor comprises an adjoining an inlet and a frustoconical widening region, which merges into an end provided with an outlet cylinder portion.
  • 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.
  • a gasification agent such as air
  • a time for switching from a construction to a mining operation is thus in principle easier to recognize and associated with less serious consequences than a termination of a mining operation.
  • switching in both directions are required.
  • the necessary decisions i.d.R. met by specially trained monitoring and technical personnel.
  • the invention is based on the finding that the most stable possible operation of a floating bed reactor described above requires operation in the build-up mode. Here is achieved by addition of gasification a high material conversion at high gas yield. However, in order not to cause any further increase in a width of the floating bed, must be taken specifically targeted for a reduction of the floating bed. However, in order to prevent a reduction in efficiency of the gasification process or even a collapse of the fluidized bed or irreversible tipping into a fluidized bed gasification, in contrast to a known control no intervention at the reactor inlet by restricting the Kokseintrags and / or increasing the use of gasification performed. On the contrary, it has turned out that, for a targeted reduction of the suspended bed, additional gasification agent can be introduced directly into the fluidized bed, which is also easy to control.
  • a method according to the invention is characterized in that a supporting layer of the fluidized bed in the suspended bed reactor is constantly operated in a build-up mode and, in overlapping time, degradation of the fluidized bed is carried out by introducing additional gasification agent.
  • additional gasification agent is introduced into the non-supporting layer of the fluidized bed during operation of the device in the construction mode.
  • this process takes place using at least one nozzle or lance.
  • lances are used, with the additional positive effect of significantly minimizing occurring at an adjacent wall of the reactor during the injection local heating by a length of about 10 cm to preferably more than 20 cm in a cylindrical part of Projecting reactor, wherein the diameter of a reactor in this area, for example can be at about 1.5 m and more.
  • these lances are covered in operation by a coke bed or thickness of the non-bearing layer of the fluidized bed, which is sufficient to ensure the fullest possible implementation of the additionally introduced gasification agent in product gas.
  • the temperatures in this region of the reactor are already around 600 ° C., ie above the autoignition temperature of the coke. If additionally gasification agent is injected at this point, then the gasification agent reacts immediately with the coke and gasifies it. The injection must therefore take place within the fluidized bed and thus directly into the coke.
  • the bed above the injection must still be so high that a largely to the fullest possible implementation of the introduced gasification agent is ensured to prevent reaction of the gasification agent with product gas and thus an efficiency reduction and effectively increase the output of the system to product gas.
  • These parameters may e.g. as part of a learning process in a particular plant in the course of the initial start-up and be set.
  • a distribution of the additionally introduced gasification agent to two to about 15 lances, preferably about six lances, which are arranged distributed in an embodiment of the invention over a circular cross-sectional plane equidistant.
  • the lances become advantageous individually and in particular used at intervals for injecting the additional gasification agent into the non-supporting layer of the fluidized bed. This prevents localized oversized degradation of the non-bearing layer of the fluidized bed and also limits local heating within the non-structural layer of the fluidized bed.
  • Particularly preferably directly adjacent lances are virtually skipped in the course of a continuous change in the injection of the additional gasification agent in order to prevent a direct adjacency of local overheating with uniform or even degradation of the non-bearing layer of the floating bed.
  • a substantially constant entry of additional gasification agent will result in a consistent additional yield of product gas.
  • the gas permeability of the supporting layer remains largely constant at high values. Instabilities of the bed up to a transition to the fluidized bed are largely prevented, especially during the now proposed bed degradation.
  • the injection of the additional gasification agent by targeted degradation in the region of the non-bearing layer causes an increase in the implementation of small-particle coke particles in product gas.
  • the gas yield and thus the overall performance of the system with low structural adaptation are thus still increased.
  • the essential parameter in the gasification of biomass is the lambda value or the air ratio, which is usually in the range of about 0.3 and about 0.4 in gasification plants.
  • the lambda value depends on the gasification agent used, for the air, oxygen, steam or even water mist can be used.
  • respective plants are operated in a lambda window of about 0.31 to about 0.36, wherein the lambda value of about 0.31 indicates a classic construction operation and the lambda value of about 0.36 a classic mining operation .
  • the lambda value below the fluidized bed, ie at the reactor inlet is kept constant at about 0.31.
  • the additional injection of gasification agent in the non-bearing layer is varied in the course of the regulation in a lambda window of about 0.00 - about 0.05.
  • a sensor or level sensor is provided.
  • This fill level measurement is preferably carried out via a radar sensor, one or more rotary vane switches or via a combination of a radar sensor and at least one rotary vane switch. If the filling level reaches a certain level, it is possible, after blocking the rotary vane switch, to switch over to a particularly controlled dismantling of the floating bed in the non-load-bearing part as independent confirmation of a measurement of the radar sensor.
  • the suspended bed reactor preferably at least two arranged at different heights in the region of the non-supporting layer rotary vane switch for averaging signals for a control of the level is provided.
  • a second possibility is the intermittent timing of the injection effected via the lances, which alternative or in addition to a preceding executed local temperature reduction can be used in particular by admixtures.
  • a spatial and / or temporal diversification of the injection represents a possibility for local limitation of heating.
  • a lance is operated only a short time and then switched to the next lance, eg with a uniform arrangement of eg seven lances over the circumference distributed.
  • a spatial separation of the local heating can be achieved by skipping each directly adjacent lance, that is to say switching over from a first to a third lance, etc., with a substantially constant injection quantity.
  • FIG. 2 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.
  • known device 1 for the fluidized bed gasification of a carbonaceous material or biomass as a complete system in a sectional view.
  • the entire process path from the supply of a biomass B in a pyrolysis 2 with gas nozzles 3, from there via an oxidation unit or transport section 4 with nozzle unit 5 to the outlet of a product gas P from a reduction unit 6 with nozzle unit 7 for introduction and metering of gasification V shown in context.
  • the reduction unit 6 then comprises an approximately frustoconical widening to the nozzle unit 7 first section 8, which opens into a cylinder portion 9, which terminates via a now frustoconical 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 floating layer 12 shown hatched here is in FIG. 2 indicated.
  • An essential basis is the recognition that the fluidized bed 12 can be subdivided into a load-bearing layer 15 and a non-load-bearing layer 16. Between these layers, a transition is usually fluid and may extend over a larger portion. As secured for these layers 15, 16 but in the floating bed of FIG. 1a the respective areas.
  • the non-load-bearing layer 16 can be selectively dismantled separately in order to reduce the thickness of the floating bed 12.
  • additional gasification agent Vz is introduced into the non-load-bearing layer 16 of the fluidized bed 12 in the fluidized bed reactor or the reduction unit 6.
  • the supporting layer 15 of the fluidized bed 12 in the reduction unit 6 is constantly operated in the construction mode by a corresponding regulation of the nozzle unit 7. Temporally overlapping this, a degradation of the floating bed 12 by introducing additional gasification agent Vz is carried out in the non-supporting layer 16. Thus, with an overall increased turnover of the expanded fluidized bed reactor 6 overflowing or overfilling with coke pieces is avoided.
  • FIG. 1b shows a qualitative course of the temperature T over the height of the expanded fluidized bed reactor 6.
  • a lambda value is maintained at about 0.31
  • the additional injection of gasification agent Vz in the non-gas supporting layer 16 in a lambda window is varied from about 0.00 to about 0.05. Accordingly, starting from the position of the nozzle unit 7, a temperature T increases abruptly to almost constant values of about 1,000 ° C. due to the metered introduction of gasification agent V and only drops significantly to values greater than when a lower edge of the continuously developing supporting layer 15 is reached about 600 ° C from.
  • the temperature T decreases to values of about 600 ° C from. This is an area of non-bearing layer 16 is reached, is introduced into the additional gasification agent Vz.
  • the temperature T rises almost impulsively back to values of about 1,000 ° C, and then over a short distance h of an overlap with coke until leaving the non-supporting layer 16 to cool again to about 600 ° C.
  • Figure 1c represents a detail FIG. 1a with details for the injection of additional gasification agent Vz in the non-supporting layer 16 in the region of the cylinder portion 9. Accordingly, projects as a lance 17 piece of pipe by a length L of more than about 20 cm and a diameter d of about 25 mm in the one Diameter of more than about 1.5 m having cylinder portion 9 and thus in the coke of the non-bearing layer 16 inside.
  • the temperature T here is still at about 600 ° C and thus significantly above an autoignition temperature of coke.
  • the injection of additional gasification agent Vz leads to an immediate reaction and gasification of the surrounding coke.
  • a product gas P already flowing through the non-bearing layer 16 at a speed v forces a hot conversion zone 18 in its flow direction. Even if the reaction zone 18 subsequently reaches temperatures of approximately 1000 ° C. in a small radius directly adjacent to an outlet of the lance 17, coke has such good thermal insulation that a distance L of the reaction zone 18 from one wall of the cylinder section 9 is sufficient so as not to cause any significant warming here.
  • a sufficiently powerful covering layer over the lance 17 should also be taken into account.
  • a thickness h of the covering layer is sufficient if the injected additional gasification agent Vz has been converted substantially completely into product gas P. This is metrologically detectable, so that a corresponding coverage height h of the lances 17 can be adjusted with coke of the non-supporting part 16 of the floating bed 12.
  • FIG. 1a indicated two lances 17, but 6 equidistantly on the circumference of the cylinder portion 9 distributed lances 17 are provided. These lances can basically be operated simultaneously. Due to the possibility of high, local temperatures, however, clumping or slagging of the coke in the region of the respective conversion zones 18 can occur over a longer period of time. This slagging can subsequently lead to an impairment of the operation.
  • the lances 17 are subjected intermittently in time to an additional gasification agent Vz to be injected, i. It is switched from one actively injecting lance 17 to a next.
  • lances 17, which are acted upon in addition by gasification means Vz which are additionally to be injected are not immediately adjacent to one another, so that no larger areas of buildup or coke clumping can form in the non-bearing layer 16.
  • a first, third and fifth lance 17 successively or at the same time inject additional gasification agent Vz, then follow the second, fourth and sixth lance 17 and so on after a short run time of the injection process.
  • the temperature in the reaction zone 18 is reduced by adding water vapor or even water droplets in the form of mist to the additionally injected gasification agent Vz.
  • the person skilled in the art is familiar with further possibilities for lowering a temperature in the reaction zone 18 up to an admixture of inert exhaust gases from the thermal conversion of the product gas P into the additionally injected gasification agent Vz.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP20140189101 2013-10-16 2014-10-15 Procédé de réglage destiné au fonctionnement d'un gazéificateur à lit mobile et d'un réacteur à lit mobile Pending EP2862914A1 (fr)

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AT501482013 2013-10-16

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
CN113969192A (zh) * 2021-10-08 2022-01-25 陈松涛 一种离心悬浮固定床复合气化炉、生产系统和生产方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
DE3617802A1 (de) * 1986-05-27 1987-12-03 Rheinische Braunkohlenw Ag Verfahren zur herstellung von wasserstoff und kohlenmonoxid enthaltenen gasen aus festen brennstoffen
EP1201731A1 (fr) * 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
WO2005040439A1 (fr) * 2003-10-28 2005-05-06 Ebara Corporation Incinerateur et gazogene
EP1666567A1 (fr) * 2003-08-04 2006-06-07 Suntory Limited Dispositif, systeme et procede de carbonisation
DE102007012452A1 (de) 2007-03-15 2008-09-25 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Vergaser

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
DE3617802A1 (de) * 1986-05-27 1987-12-03 Rheinische Braunkohlenw Ag Verfahren zur herstellung von wasserstoff und kohlenmonoxid enthaltenen gasen aus festen brennstoffen
EP1201731A1 (fr) * 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
EP1666567A1 (fr) * 2003-08-04 2006-06-07 Suntory Limited Dispositif, systeme et procede de carbonisation
WO2005040439A1 (fr) * 2003-10-28 2005-05-06 Ebara Corporation Incinerateur et gazogene
DE102007012452A1 (de) 2007-03-15 2008-09-25 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Vergaser

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
CN113969192A (zh) * 2021-10-08 2022-01-25 陈松涛 一种离心悬浮固定床复合气化炉、生产系统和生产方法
CN113969192B (zh) * 2021-10-08 2024-01-16 陈松涛 一种离心悬浮固定床复合气化炉、生产系统和生产方法

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