WO2007090585A1 - Procede et reacteur de gazeification avec extraction du laitier liquide - Google Patents

Procede et reacteur de gazeification avec extraction du laitier liquide Download PDF

Info

Publication number
WO2007090585A1
WO2007090585A1 PCT/EP2007/000940 EP2007000940W WO2007090585A1 WO 2007090585 A1 WO2007090585 A1 WO 2007090585A1 EP 2007000940 W EP2007000940 W EP 2007000940W WO 2007090585 A1 WO2007090585 A1 WO 2007090585A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasification
zone
nozzle plane
bed
oxygen
Prior art date
Application number
PCT/EP2007/000940
Other languages
German (de)
English (en)
Inventor
Bernd Meyer
Original Assignee
Rwe Power Aktiengesellschaft
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 Rwe Power Aktiengesellschaft filed Critical Rwe Power Aktiengesellschaft
Publication of WO2007090585A1 publication Critical patent/WO2007090585A1/fr

Links

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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J3/46—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
    • 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
    • C10J2300/0953—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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • C10J2300/1634—Ash vitrification
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1838—Autothermal gasification by injection of oxygen or steam

Definitions

  • the invention relates to a method and a gasification reactor for the gasification of solid carbonaceous materials under elevated pressure in interconnected gasification chambers using gasification agents containing free oxygen, wherein dust-laden raw gas on the top side and liquid slag are withdrawn from the bottom.
  • a process for fluidized-bed gasification with liquid slag removal is known, for example, from DE 103 43 582 A1.
  • Subject of the application DE 103 43 582 A1 is a method in which over a bottom slag bath a reaction space for largely residual gasification of existing predominantly pyrolysis, carbonaceous bottom product, and above a separation bed are provided, wherein the separation bed the reaction space above the slag bath of the fluidized bed separates.
  • DE 103 43 582 A1 assumes that, due to the clear separation of the reaction spaces, a wide variety of fuels can be used while at the same time achieving almost complete carbon conversion.
  • the empty tube velocity of the gas flowing through the separation bed is limited to low values, according to DE 10343 582 A1 to 0.05 to 1 m / s. If the separation bed can not be flowed through uniformly - this is the case with very fine-grained fuels, fuels with a large grain spectrum and considerable coarse grain fractions and particulate fractions or biogenic fuels with very low apparent density of the residual coke or pyrolysis coke forming the bottom product Separation bed to unsteady flow and in the fluidized bed to form zones of low and zones strong base inflow. (n the consequence, strong local temperature differences build up in the fluidized bed and slagging also occurs.
  • DE 2640 180 A1 describes a process for the gasification of solid fuels, wherein the fuel is gasified in superimposed gasification chambers, at the bottom in a quiescent or quasi-stationary layer and above in a fluidized bed. It is proposed a dry ash deduction by means of a rotary grate, which can be alternatively designed as a tapping generator. Again, it lacks a solution for the slag-free operation of the fluidized bed when using the above-mentioned fuels that do not allow a uniform flow through the quiescent or quasi-stationary layer and no uniform fluidization of the fluidized bed. Attempts have now been made to circumvent the uniformity requirements of the fluidization in the fluidized bed by specifically establishing reaction areas with strong and weak flow reaction areas. For this purpose, so-called spouted bed (bubble bed) - methods or jet-bed (jet-bed) - methods have been proposed, but have the disadvantage that primarily only pulverized fuels can be used.
  • Gasification agent is injected together with pulverized coal via two nozzle planes arranged vertically one above the other.
  • the lower nozzle level is operated with excess oxygen and the upper nozzle level with steam.
  • a jet forms in front of the nozzles, in which the gasification reactions take place preferentially and which have no direct contact with the wall.
  • the slag forming in the lower area flows down the walls and is drawn off.
  • the disadvantage of the solution according to this JP 57174391 A is that only pulverized and pneumatically recoverable fuels can be used.
  • the patent teaches no how the carburetor inner wall in the transition region between underside combustion and topside endothermic gasification in continuous operation kept free of slag and how can be avoided that unvergaster residual coke is withdrawn with the slag.
  • the reaction chamber of the gasification according to JP 59053592 A is to be separated into a jet bed reaction space arranged at the top and a fluidized bed reaction space arranged underneath, wherein both reaction spaces are connected to one another by a constricted opening.
  • the upper jet-bed reaction space is supplied with pulverized coal, while coarser fluidized bed coal is supplied to the lower fluidized bed reaction space.
  • Liquid slag should flow from the upper jet bed reaction space into the lower fluidized bed reaction space, which is operated at moderate temperatures below the ash softening point.
  • the invention is therefore based on the object to improve the gasification with liquid slag withdrawal of the type mentioned so that a variety of solid fuels with a broad grain band at the same time Achieve almost complete carbon turnover can be used.
  • the invention is further based on the object to provide a gasification reactor for carrying out the method.
  • first gasification agents are introduced into a slag bath gasification zone with which the most extensive residual gasification of a carbonaceous bottoms product leaving a first spouted bed gasification zone at the bottom is carried out at temperatures above the ash flow point,
  • second gasification agents are introduced into the slag bath gasification zone and into the first spouted bed gasification zone with which the partial gasification of a carbonaceous bottoms product leaving a second spouted bed gasification zone at temperatures above the ash melting point above of the ash refuse point is carried out
  • That third gasification agents are introduced into the second Spouted -bed - gasification zone on the underside, with which the predominant gasification of the carbonaceous materials, which are introduced into this zone, is carried out at temperatures in the range below the ash-laying temperature to above the ash flow, and
  • the partial gasification of a carbonaceous overhead product, leaving the second Spouted-bed - gasification zone on top is carried out at temperatures below the ash temperature.
  • Essential to the invention is the embodiment of the method according to the fuel properties.
  • these are the ash behavior, characterized by the ash-laying temperature, ash melting point and ash flow point, grain size or piece size of the fuel and the grain size and the apparent density of the pyrolysis coke that forms.
  • the ash melting point or the ash pour point of different fuels usually vary between 800 to 1300 0 C or 1,000 and 1,500 0 C.
  • the ash transfer temperature is the temperature at which it of under the respective gasification conditions to operational interfering caking of ash on the walls of the gasifier or Rohgasabganges comes.
  • the ash-laying temperature is close to below the ash melting point and, among other factors, depends on the proportion and grain size of the free ash on the carbonaceous material.
  • the ash-laying temperature can not be predetermined theoretically or experimentally, but is determined in the gasification operation.
  • Fine-grained fuels are those with a grain size of about 0 - 1 mm understood as coarse-grained ones with a grain size of about 0 - 50 mm and lumpy or lumpy ones with an edge length of 50 mm up to 1m.
  • Coarse fuels are, for example, biomass compactates (pre-shredded straw bales and the like).
  • the pyrolysis cokes are fine-grained (approx. ⁇ 1 to 5 mm) to coarse-grained (approx. ⁇ 20 mm).
  • the former are usually of high volatility Fuels (biomass, plastics, low-carbon coals), the latter, however, low-volatile fuels (mainly coal).
  • the gasification reactions are carried out as follows.
  • the slag bath - gasification zone consists of flame areas, which form before the injection sites of the gasification center) and which are directed into the center of the gasification room.
  • the Schlackebad - gasification zone forms, in simplified terms, a reaction area in which run as far as possible, the exothermic gasification reactions.
  • the vapor / oxygen ratio of the first gasification agent is adjusted according to the ash flow point so that the gasification temperatures in the entire reaction region significantly exceed the ash flow point.
  • the composition of the first gasification agents themselves have values for the steam / oxygen ratio of 0.5 to 1, 5 kg / m 3 in proven advantageous according ash pour points of about 1500-1000 0 C.
  • the partial gasification of the carbonaceous bottoms product leaving the bottom of the second spouted bed gasification zone is carried out at temperatures in the range above the ash melting point to above the ash flow point.
  • An exothermic and an endothermic reaction zone are formed.
  • the exothermic reaction zone in which predominantly the exothermic gasification reactions take place, consists of the flame zone in front of the injection sites of the second gasification means and the region of the upward center flow, which is formed as a spout flow.
  • the Spo ⁇ t flow is achieved in that the second gasification agent burn through the bed of solids of the first Spoutedbed - gasification zone channel-like and thereby form upward flow channels.
  • the endothermic reaction zone in which the endothermic gasification reactions are provided, occupies the remaining space of the first spouted-bed gasification zone, which is more or less formed as a loose fixed bed.
  • the still occurring gas release by post degassing of the pyrolysis coke in the fixed bed contributes.
  • solids are constantly carried into the exothermic reaction zone by gravity and shear forces and gasified.
  • gasification temperatures above the ash flow point and in the endothermic reaction region gasification temperatures above the ash melting point are set.
  • the carbonaceous materials include the feedstocks to be gasified, the bottom carbonaceous product leaving the entrained flow gasification zone and separated dust introduced into the second spouted bed gasification zone via the recycle system.
  • an exothermic and an endothermic reaction region are formed.
  • the exothermic reaction area consists of the flame area before the injection sites of the third gasification means and the area of upward center flow which is formed as a spout flow.
  • the gas velocity is increased abruptly, since here the majority of the gasification gas is formed and the volatile constituents of the fuel are released spontaneously.
  • the typical loosened spout flow is formed at the level of the injection of this third gasification agent with centrally ascending solid fountains and so-called kidney flow.
  • the latter includes the central upward flow of gas and solid and the peripheral downflow, predominantly of solids.
  • the endothermic reaction area predominantly covers the area of this peripheral downflow. It is increasingly forming upwards towards the middle of the second spouted-bed gasification zone. The endothermic reaction area thus envelops the exothermic reaction area and protects the carburetor walls and the gasification agent nozzles from slagging.
  • the vapor / oxygen ratio of the third Vergas ⁇ ngsstoff is chosen so that set in the exothermic reaction region gasification temperatures above the ash flow point and in the endothermic reaction region gasification temperatures below the Ascheverlegungstemperatur.
  • values of 0.3 to 2 kg / m ⁇ N. proved to be suitable.
  • the value range to be selected for the respective fuel is determined on the basis of the fuel properties, in particular the ash melting behavior and the ash-laying temperature, during the operation of the gasifier.
  • the value to be set of the steam / oxygen ratio is regulated either according to a measured temperature, preferably the temperature at the crude gas outlet, or with the aid of the methane content of the raw gas leaving the gasifier. The fact is used that there is a fuel-typical relationship between the temperature at the raw gas outlet and the methane content of the raw gas. The latter can be determined with a short time delay by means of on-line analysis.
  • the entrainment gasification zone flows smoothly out of the second spouted-bed gasification zone, at the level where the renal flow passes into the upward flow.
  • the entrained-flow gasification zone is designed so that a uniform gas-solid flow is present over the entire flow cross-section, in which the solids are more or less less homogeneously distributed.
  • This zone is intended as a uniform reaction area in which only endothermic Gasification reactions occur, with gasification temperatures are set well below the ash-laying temperature.
  • An advantageous embodiment of the method provides to completely blow the second gasification agent together with the first gasification centers.
  • a further advantageous embodiment of the method envisages introducing at most a portion of the second gasification agent together with the first gasification agent.
  • the steam / oxygen ratio of the first and the second gasification agent is preferably set in the same size, optionally deviating from the size of the vapor / oxygen ratio of the third gasification center. It is also possible to use all three gasification agents with the same composition of steam and oxygen, i. with an equal steam / oxygen ratio, foundedbiasen. In the first case! are only two, in the second case even only a gasification agent is produced by mixing oxygen and steam.
  • [O 2 (1)] is the volume flow of the gasification oxygen of the first gasifying agent
  • [O 2 (2)] is the volume flow of the gasification oxygen of the second
  • [O 2 (3)] is the volume flow of the gasification oxygen of the third gasifying agent.
  • the empty-tube velocities are the gas velocities related to the free flow cross-section which are set at the upper end of the respective gasification zone on average.
  • three conditions are preferably to be met.
  • the first condition concerns the ratio to be set of the volume flow rate of the third gasification oxygen to the sum of the volume flows of first and second gasification oxygen [O 2 ratio 3] according to equation (1):
  • High values for [O 2 ratio 3] are preferably set for high volatile fuels (especially biomass) and vice versa, ensuring that the necessary heat is introduced into the slag bath.
  • the value for [O 2 - ratio 2] indicates the proportion of gasification oxygen that is used for partial gasification in the first Spo ⁇ ted tted gasification zone.
  • the low values apply to fine-grained fuels, to fuels whose pyrolysis cokes have a low apparent density, but also to coarse-grained to coarse-grained fuels which form a fine-grained pyrolysis coke.
  • the high values apply to fuels containing a coarse-grained pyrolysis coke form high apparent density.
  • the fuels which form very fine-grained residual cokes with very low apparent density include the already mentioned biogenic solid fuels or gasified waste plastics.
  • the third condition concerns the volumetric flow rate of the total gasification oxygen [ ⁇ O 2 ] according to equation (3)
  • [ ⁇ O 2 ] [O 2 (1)] + [O 2 (2)] + [O 2 (3)] such that the empty tube velocity at the top of the second spouted bed gasification zone 0, 3 to 3 m / s.
  • Low values of [ ⁇ O 2 ] and low empty tube velocities apply to fuels that form fine-grained pyrolysis cokes or pyrolysis cokes with low apparent density.
  • High values of [ ⁇ O 2 ] with high empty tube velocities are attributed to fuels that form coarse-grained pyrolysis cokes or pyrolysis cokes with high apparent density.
  • the object underlying the invention is further characterized by a gasification reactor, the gasification chamber is bounded on the underside of the liquid surface of a slag bath and on the upper side of a Rohgasabgang and the nozzle planes for injecting gasification agents, which is preferably radially aligned with respect to the gasification space and preferably evenly over the Scope of the gasification room are distributed, thereby solved
  • the slag bath gasification zone, the first spouted bed gasification zone, the second spouted bed gasification zone and finally above the entrainment gasification zone are arranged one after the other in the gasification space from bottom to top,
  • each nozzle plane Vergasungsstoffdüsen on at least one respective sectional surface, which preferably intersects the gasification chamber horizontally, and
  • the Vergasu ⁇ gsstoffdüsen a nozzle plane are arranged either in one or more imaginary cut surfaces.
  • the nozzle plane with which the first gasification agents are injected into the slag bath gasification zone is referred to as the first nozzle plane.
  • the nozzle planes with which the second and third gasification agents are injected into the two spouted-bed gasification zones are referred to as second and third nozzle planes, respectively.
  • the gasification agent nozzles of the first, the second and the third nozzle plane are arranged on a respective cut surfaces.
  • Arrangement on each cut surfaces reduces the plant engineering effort.
  • One of the cut surfaces of the second nozzle plane may be identical to one of the cut surfaces of the first nozzle plane.
  • the gasification agent nozzles of the first nozzle plane may be arranged adjacent to those of the second nozzle plane on this sectional surface. Furthermore, an advantageous simplification of the adjacent arrangement of the gasifying agent nozzles is that at least a part of the gasifying agent nozzles of the second nozzle level is identical to gasifying agent nozzles of the first nozzle level, i. that the first and the second gasification agents are injected together with this part of the gasification agent nozzles.
  • all gasifying agent nozzles of the second nozzle level are identical to all gasifying agent nozzles of the first nozzle level, which are located on at least one sectional surface, there is de facto only one common nozzle plane for injecting the first and the second gasifying agents. With this arrangement, the plant engineering effort can be reduced to a minimum.
  • a part of the gasifying agent nozzles of the second nozzle plane may be arranged on at least one sectional surface, wherein the sectional surfaces are located between the first and the third nozzle plane. It is advantageous if the distance between the cut surfaces of the second nozzle plane and the distance between the uppermost cut surface of the second nozzle plane to the third nozzle plane are preferably selected to be equal.
  • An advantageous embodiment of the gasification reactor provides to introduce a portion of the second gasification agent together with the first gasification means with Vergasungsstoffdüsen on a sectional surface and inject the other part of the second gasification agent by means of Vergasungsstoffdüsen on a second interface, preferably halfway between the first and the third Nozzle level is arranged.
  • the third ' gasification means are injected by means of the third nozzle level on the underside in the second Spouted-bed gasification zone.
  • the gasifying agent nozzles of the nozzle levels are provided with different inclination to the horizontal.
  • the gasifying agent nozzles of the first nozzle level are preferably 10 to 30 ° downwards to achieve an intense heat input into the slag bath and a complete gasification of the residual coke on and above the liquid surface of the slag bath.
  • the gasifying agent nozzles of the second nozzle levels are preferably inclined 45 ° down to 60 ° upwards.
  • the horizontal or upwardly inclined arrangement is advantageous in carburetors high power and correspondingly large diameters of the gasifier chamber of more than 2 to 3 m, to bring the gasification agents as far as possible in the middle of the gasification chamber.
  • the gasifying agent nozzles are preferably arranged downwards in order to avoid the penetration of liquid slag into the interior of the nozzles.
  • the gasification agent nozzles of the third nozzle plane are preferably arranged 0 to 30 ° down or 10 to 45 ° inclined upwards.
  • the upwardly or downwardly inclined arrangement of the second nozzle plane gasifier nozzles is required to contact the flames with the opposing walls excluded. Again, the upward arrangement of carburetor high performance is beneficial.
  • the spout flow in the first spouted-bed gasification zone is produced according to the invention in different ways.
  • carburetors with diameters of the reaction space smaller than 2 to 3 m it proves to be advantageous if the second gasification agents are completely injected together with the first gasification agents by means of gasification agent nozzles on a sectional surface at the level of the slag bath gasification zone, whereby a central spout flow in the flow axis of the first spouted-bed - gasification zone is pronounced.
  • the gasification chamber comprising the three gasification zones can be executed over the entire height in a cylindrical contour without appreciable cross-sectional changes.
  • the construction of the gasification reactor is thereby simplified considerably.
  • the advantage of the invention is that, for the first time, a wide variety of solid fuels with a broad grain band can be gassed without damage while at the same time achieving almost complete carbon conversion.
  • Essential to the invention is the use of high gasification temperatures with liquid slag formation in the three lower gasification zones, which is made possible by the formation of the stepped spouted-bed gasification and its expansion to the predominant gasification space.
  • the slag-free transition from the high gasification temperatures at the level of the slag bath to the low gasification temperatures below the ash-laying temperature at the gasifier outlet can be realized technically with simple means.
  • the invention combines the advantages of slag bath, fluidized bed, spouted bed and entrained flow gasification and avoids the disadvantages of these processes in terms of their restrictions on the fuels to be gasified.
  • the solution according to the invention is also very simple in its apparatus design, robust in operation and flexible to changing fuel properties.
  • fuels with distinctly different properties for example biomass alternating with brown coal or lignite alternating with hard coal, can be used.
  • An essential advantage of the invention is also that biomass of different nature alone or in the Mixture with coal and other solid fuels can be gasified. There is even the possibility of biomass in compacted form, z. B. as pre-shredded straw bales to use.
  • the drawing shows a highly simplified and schematic representation of a carburetor 1 for the production of synthesis gas for use in a methanol synthesis using the method according to the invention.
  • the exemplary embodiment is explained with reference to the gasification of dried biomass, especially the technically demanding mono-gasification of natural, dried straw.
  • the straw is gasified with a water content of 12% by mass, a calorific value of 15.3 MJ / kg and an ash content of 3.86% by mass (both based on 12% by mass of water content).
  • the straw is conditioned in a known manner by addition of an alkali-binding clay mineral in order to incorporate and fix excess ash contents of the ash, which would otherwise evaporate and cause detrimental contamination in colder plant components, into solid and liquid aluminosilicates.
  • the characteristic temperatures are the ash melting behavior of the so conditioned straw ash: ash transfer temperature 950 0 C, ash melting point 1,210 0 C, ash flow point 1,320 0 C.
  • the conditioned straw forms a very fine-grained pyrolysis coke with very low apparent density.
  • conditioned straw 2 consisting of 24 t of straw in the form of pellets and larger compact materials up to about 200 mm edge length and about 0.5 - 1 t of finely ground clay mineral, are introduced into the carburetor 1.
  • the carburetor 1 is operated at 26 bar overpressure and has a thermal output of 100 MW.
  • the carburetor 1 comprises the cylindrical, vertical gasification chamber 3 with a clear inner diameter of 1, 8 m and a vertical extension of 11, 5 m. The latter extends from the liquid surface 4 of the slag bath 5 to the crude gas outlet 6. From the gasifier 1 the underside liquid slag 7 and the upper side via the crude gas outlet "6 dust-laden raw gas 8 is pulled off.
  • the dust-laden raw gas 8 is dedusted in a hot cyclone 9. From the hot cyclone 9 Exceeds top side dedusted raw gas 10 and bottom deposited dust 11. The separated dust 11 is returned by means of a return system, which consists of a downpipe 12, an L-valve 13 and a connecting line 14, back into the carburetor 1. The L-valve 13th is operated with the conveying gas 15.
  • the gasification space 3 is, as seen from below, subdivided into the superimposed gasification zones of the slag bath gasification zone 16, the first spouted bed gasification zone 17, the second spouted bed gasification zone 18 and the fly gas gasification zone 19.
  • the slag bath gasification zone 16 with a small vertical extension is located at the level of the first nozzle plane 20.
  • the first spouted bed gasification zone 17 is located between the first nozzle plane 20 and the third nozzle plane 21 and has a vertical extension of 2.5 m.
  • the first nozzle plane 20 simultaneously assumes the function of the second nozzle plane, which is not carried out in the carburetor 1 small power.
  • the second nozzle level would be applicable if carburetors with significantly larger diameters than carburettor 1 were to be used.
  • the second spouted-bed gasification zone 18 extends from the third nozzle plane 21 to about 4 m above it.
  • the Flight flow - gasification zone 19 closes the gasification chamber 3 upwards up to the level of the raw gas outlet 6 and has a vertical extent of about 5 m.
  • the height delimitation of the two lower gasification zones 16 and 17 takes place through the first nozzle plane 20 and the third nozzle plane 21.
  • the first nozzle plane 20 and the third nozzle plane 21 are each located on a sectional surface 22.
  • the first gasification means 23 are introduced into the slag bath gasification zone 16 by means of six gasification agent nozzles 24 of the first nozzle plane 20.
  • the second gasification means 25 are injected together with the first gasification means 23 by means of the six gasification agent nozzles 24 of the first nozzle plane 20.
  • the third gasification means 26 are injected by means of six gasification agent nozzles 24 of the third nozzle plane 21.
  • the gasifying agent nozzles 24 of the two nozzle planes 20 and 21 are uniformly arranged radially over the circumference of the gasifying chamber 3 and vertically one above the other at the positions 5 min , 15 ", etc., for 60 minutes 15 ° downwards.
  • the conditioned straw 2 is introduced by gravity into the second spouted-bed gasification zone 18 via the inclined tube 27.
  • the entry opening 28 of the inclined tube 27 is located at the level of 2 m above the third nozzle plane 21.
  • the entry port 29 of the connecting line 14 is at the same height.
  • the gasification center are injected as follows:
  • the steam / oxygen ratio of the liquids is 23, 25 and 26 is 0.5 kg / m 3 i.N. ,
  • the volume flow of the total gasification oxygen [ ⁇ O 2 ] is 4,700 m 3 i. N / h.
  • an empty tube velocity of 0.6 m / s is set.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé de gazéification doté d'une extraction (7) de laitier liquide constitué de matériaux solides contenant du carbone par recours à des moyens de gazéification qui contiennent de l'oxygène libre. Du gaz brut (10) chargé en poussière est extrait du côté supérieur et du laitier liquide du côté inférieur (7). Des premiers moyens de gazéification sont placés dans une zone (16) de gazéification du bain de laitier et permettent de réaliser une gazéification résiduelle très poussée d'un produit de fond contenant du carbone à une température supérieure au point de fluidisation des cendres. Des deuxièmes moyens de gazéification sont installés dans la zone (16) de gazéification du bain de laitier et dans la première zone (17) de gazéification du lit fluidisé et permettent de réaliser la gazéification partielle d'un produit de fond contenant du carbone à une température supérieure au point de fusion des cendres jusqu'à une température supérieure au point de fluidisation des cendres. Des troisièmes moyens de gazéification sont installés du côté inférieur de la deuxième zone (18) de gazéification du lit fluidisé et permettent de gazéifier les matériaux qui contiennent du carbone dans cette zone à des températures situées au-dessus de la température de déplacement des cendres jusqu'à une température supérieure au point de fluidisation des cendres. Dans une zone (19) de gazéification de l'écoulement volant, et sans addition de moyens de gazéification, a lieu la gazéification partielle d'un produit de tête qui contient du carbone et qui quitte la deuxième zone (18) de gazéification du lit fluidisé par son côté supérieur, à une température inférieure à la température de déplacement des cendres.
PCT/EP2007/000940 2006-02-06 2007-02-03 Procede et reacteur de gazeification avec extraction du laitier liquide WO2007090585A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102006005626.4 2006-02-06
DE200610005626 DE102006005626B4 (de) 2006-02-06 2006-02-06 Verfahren und Vergasungsreaktor zur Vergasung verschiedenster Brennstoffe mit breitem Körnungsband mit Flüssigschlackeabzug

Publications (1)

Publication Number Publication Date
WO2007090585A1 true WO2007090585A1 (fr) 2007-08-16

Family

ID=37909276

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2007/000940 WO2007090585A1 (fr) 2006-02-06 2007-02-03 Procede et reacteur de gazeification avec extraction du laitier liquide

Country Status (2)

Country Link
DE (1) DE102006005626B4 (fr)
WO (1) WO2007090585A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104789268A (zh) * 2015-04-25 2015-07-22 北京四维天拓技术有限公司 一种橡胶气化装置及运行方法

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007006977B4 (de) 2007-02-07 2011-06-16 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur verschlackenden Vergasung fester Brennstoffe unter Druck
DE102011114171A1 (de) 2011-09-19 2013-03-21 Thyssenkrupp Uhde Gmbh Verfahren zur Herstellung von Synthesegas durch Vergasung einer Biomasse in einer Wirbelschicht
CN102911741B (zh) * 2012-10-18 2013-12-25 东南大学 循环流化床煤气化的装置
CN103965968B (zh) * 2014-05-22 2016-01-20 哈尔滨工业大学 一种带有蒸汽升压装置的恩德粉煤气化炉
DE102016210350B4 (de) * 2016-06-10 2018-01-18 Technische Universität Bergakademie Freiberg Vergasungsreaktor zur Erzeugung von Synthesegasen aus festen Vergasungsstoffen mit Hilfe sauerstoffhaltiger Vergasungsmittel

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2640180A1 (de) * 1976-09-07 1978-03-16 Projektierung Chem Verfahrenst Verfahren und vorrichtung zur gaserzeugung aus festen brennstoffen
DD138992A1 (de) * 1977-09-16 1979-12-05 Rheinische Braunkohlenw Ag Verfahren und vorrichtung zum vergasen von festem,kohlenstoffhaltigem material
EP0030323A1 (fr) * 1979-12-08 1981-06-17 Rheinische Braunkohlenwerke AG. Procédé de fonctionnement d'un réacteur à lit fluidisé pour gazéifier des matières carbonacées
DE3033115A1 (de) * 1980-09-03 1982-04-22 Rheinische Braunkohlenwerke AG, 5000 Köln Verfahren zum betreiben eines wirbelbettreaktors zum vergasen von kohlenstoffhaltigem material
EP0214417A2 (fr) * 1985-09-02 1987-03-18 Rheinische Braunkohlenwerke AG. Procédé de production de gaz de synthèse à partir de combustibles solides
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
ES2190689A1 (es) * 2000-03-15 2003-08-01 Azcoitia Y Villanueva Luis De Procedimiento de obtencion de gas combustible a partir de materiales combustibles.
DE10343582A1 (de) * 2003-09-18 2005-05-19 Rwe Power Ag Verfahren und Vorrichtung zur Wirbelschichtvergasung mit Flüssigschlackeabzug

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS57159886A (en) * 1981-03-30 1982-10-02 Hitachi Ltd Spouted bed gasification of coal
JPS57174391A (en) * 1981-04-22 1982-10-27 Hitachi Ltd Coal gasification
JPS58194986A (ja) * 1982-05-10 1983-11-14 Mitsubishi Heavy Ind Ltd 多段噴流床式ガス化炉
JPS5953592A (ja) * 1982-09-22 1984-03-28 Hitachi Ltd 石炭ガス化方法
JPS59145289A (ja) * 1983-02-07 1984-08-20 Hitachi Ltd 噴流層石炭ガス化炉
JPS6065094A (ja) * 1983-09-20 1985-04-13 Babcock Hitachi Kk 噴流層石炭ガス化炉
JPS61243895A (ja) * 1985-04-23 1986-10-30 Mitsubishi Heavy Ind Ltd 加圧噴流床ガス化炉
JPS61246287A (ja) * 1985-04-24 1986-11-01 Mitsubishi Heavy Ind Ltd 噴流床石炭ガス化炉
JPH066708B2 (ja) * 1985-05-21 1994-01-26 三菱重工業株式会社 石炭のガス化方法
JPH086101B2 (ja) * 1986-11-27 1996-01-24 バブコツク日立株式会社 石炭ガス化脱硫方法

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2640180A1 (de) * 1976-09-07 1978-03-16 Projektierung Chem Verfahrenst Verfahren und vorrichtung zur gaserzeugung aus festen brennstoffen
DD138992A1 (de) * 1977-09-16 1979-12-05 Rheinische Braunkohlenw Ag Verfahren und vorrichtung zum vergasen von festem,kohlenstoffhaltigem material
EP0030323A1 (fr) * 1979-12-08 1981-06-17 Rheinische Braunkohlenwerke AG. Procédé de fonctionnement d'un réacteur à lit fluidisé pour gazéifier des matières carbonacées
DE3033115A1 (de) * 1980-09-03 1982-04-22 Rheinische Braunkohlenwerke AG, 5000 Köln Verfahren zum betreiben eines wirbelbettreaktors zum vergasen von kohlenstoffhaltigem material
EP0214417A2 (fr) * 1985-09-02 1987-03-18 Rheinische Braunkohlenwerke AG. Procédé de production de gaz de synthèse à partir de combustibles solides
ES2190689A1 (es) * 2000-03-15 2003-08-01 Azcoitia Y Villanueva Luis De Procedimiento de obtencion de gas combustible a partir de materiales combustibles.
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
DE10343582A1 (de) * 2003-09-18 2005-05-19 Rwe Power Ag Verfahren und Vorrichtung zur Wirbelschichtvergasung mit Flüssigschlackeabzug

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104789268A (zh) * 2015-04-25 2015-07-22 北京四维天拓技术有限公司 一种橡胶气化装置及运行方法

Also Published As

Publication number Publication date
DE102006005626B4 (de) 2008-02-28
DE102006005626A1 (de) 2007-08-09

Similar Documents

Publication Publication Date Title
DE102007006981B4 (de) Verfahren, Vergasungsreaktor und Anlage zur Flugstromvergasung fester Brennstoffe unter Druck
DE102005035921B4 (de) Verfahren zur endothermen Vergasung von Kohlenstoff
DE2947222C2 (de) Vorrichtung zur Vergasung von festen, staubförmigen bis stückigen kohlenstoffhaltigen Brennstoffen und deren Verwendung
DE202006020602U1 (de) Vorrichtung zum Austrag von Schlacke aus Vergasungsreaktoren
DE102006005626B4 (de) Verfahren und Vergasungsreaktor zur Vergasung verschiedenster Brennstoffe mit breitem Körnungsband mit Flüssigschlackeabzug
EP0670910B1 (fr) Procede et dispositif de production de fonte brute a partir du minerai de fer ou de traitement thermique et/ou chimique d'un materiau aisement decomposable
DE102013202356A1 (de) Verfahren und Vorrichtung zur Festbettdruckvergasung fester Brennstoffe
DE60033782T2 (de) Verfahren zur vergasung von kohlenstoffhaltigen treibstoffen in einem festbettvergaser
DE102008043131B4 (de) Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe
EP1201731A1 (fr) Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
DE102016210350B4 (de) Vergasungsreaktor zur Erzeugung von Synthesegasen aus festen Vergasungsstoffen mit Hilfe sauerstoffhaltiger Vergasungsmittel
DE102012202129B4 (de) Verfahren und Einrichtung zur Festbettvergasung
DE102007006982B4 (de) Verfahren und Vorrichtung zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DD145276A5 (de) Verfahren und vorrichtung zur vergasung von kohle
EP3548587B1 (fr) Procédé et appareil de réduction de carbone dans le produit inférieur d'un gazéificateur à lit fluidisé
DE3530240C2 (de) Verfahren zum Schmelzen von zumindest teilweise reduziertem Eisenerz, sowie Vorrichtung zur Durchführung dieses Verfahrens
DE102008037318B4 (de) Verfahren, Vorrichtung und Anlage zur Flugstromvergasung fester Brennstoffe unter Druck
DE2741805A1 (de) Verfahren und vorrichtung zum vergasen von festem, kohlenstoffhaltigem material
DE2920922A1 (de) Verfahren und vorrichtung zur vergasung von kohle
DE102007006980B4 (de) Verfahren zur Vergasung fester Brennstoffe in der Wirbelschicht unter erhöhtem Druck
DE102007006979B4 (de) Verfahren zur Schlackebadvergasung
EP3067407B1 (fr) Système et méthode pour la gazéification de matière carbonée
DE3430219A1 (de) Verfahren zum vergasen von festen brennstoffen
DE102012202143B3 (de) Verfahren und Vorrichtung zur Schlackebadvergasung fester Brennstoffe
DE2751911B2 (de) Verfahren und Gas-Generator für die Vergasung von Kohlenstaub

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application
122 Ep: pct application non-entry in european phase

Ref document number: 07703251

Country of ref document: EP

Kind code of ref document: A1