WO2008095977A1 - Verfahren und vorrichtung zur flugstromvergasung fester brennstoffe unter druck - Google Patents
Verfahren und vorrichtung zur flugstromvergasung fester brennstoffe unter druck Download PDFInfo
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- WO2008095977A1 WO2008095977A1 PCT/EP2008/051497 EP2008051497W WO2008095977A1 WO 2008095977 A1 WO2008095977 A1 WO 2008095977A1 EP 2008051497 W EP2008051497 W EP 2008051497W WO 2008095977 A1 WO2008095977 A1 WO 2008095977A1
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- WIPO (PCT)
- Prior art keywords
- gasification
- flow
- moving bed
- ash
- entrained
- Prior art date
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- 238000002309 gasification Methods 0.000 title claims abstract description 167
- 239000004449 solid propellant Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 56
- 239000007789 gas Substances 0.000 claims description 62
- 239000000446 fuel Substances 0.000 claims description 32
- 229910052760 oxygen Inorganic materials 0.000 claims description 31
- 239000001301 oxygen Substances 0.000 claims description 31
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 30
- 239000000428 dust Substances 0.000 claims description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 239000008187 granular material Substances 0.000 claims description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- 239000001569 carbon dioxide Substances 0.000 claims description 8
- 239000002689 soil Substances 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 7
- 239000002918 waste heat Substances 0.000 claims description 7
- 238000002844 melting Methods 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 230000008018 melting Effects 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 239000000919 ceramic Substances 0.000 claims description 4
- 239000000470 constituent Substances 0.000 claims description 4
- 230000003179 granulation Effects 0.000 claims description 4
- 238000005469 granulation Methods 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 239000000654 additive Substances 0.000 claims description 3
- 229910010293 ceramic material Inorganic materials 0.000 claims description 2
- 239000012528 membrane Substances 0.000 claims description 2
- 239000011214 refractory ceramic Substances 0.000 claims description 2
- 238000007669 thermal treatment Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims 1
- 239000002956 ash Substances 0.000 description 63
- 238000006243 chemical reaction Methods 0.000 description 17
- 230000008569 process Effects 0.000 description 12
- 238000001816 cooling Methods 0.000 description 9
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 8
- 239000003077 lignite Substances 0.000 description 8
- 238000010791 quenching Methods 0.000 description 8
- 239000002893 slag Substances 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000005524 ceramic coating Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
- C10J3/34—Grates; Mechanical ash-removing devices
- C10J3/40—Movable grates
- C10J3/42—Rotary grates
-
- 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
- C10J3/466—Entrained flow processes
-
- 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
- C10J3/485—Entrained flow gasifiers
-
- 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
- C10J3/78—High-pressure apparatus
-
- 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
- C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
-
- 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
- C10J2300/093—Coal
-
- 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
- C10J2300/0973—Water
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Definitions
- the invention relates to a method and an apparatus for entrained flow gasification of solid fuels under pressure
- the raw gases must be strongly cooled / quenched immediately after exiting the gasification chamber of Flugstromvergasers at a short distance before they can enter the raw gas heat exchanger
- Many variants of the external Rohgasquenches were developed, of which the gas quench and the chemical quench have prevailed technically
- the Application of the gas quench leads to losses of working heat (exergy)
- the chemical quench in which carbonaceous substances are mixed into the hot raw gas stream, this disadvantage is largely avoided
- the chemical quench in continuous operation with high technical complexity and with serious disadvantages, such , B Tar and soot formation as well as formation of scale, connected
- the hot and the escaping from the entrained flow gasifier are cooled slag-containing raw gases used as an alternative quench cooling with water.
- this is simple and robust, but has the disadvantage that the resulting in the evaporation of water low temperature heat can be used practically only in the rarest cases.
- DE 26 40 180 B discloses the gasification of Festbrcnn ⁇ open different grain size (dust to coarse grained) with a lower fixed bed and an upper dust gasification zone, above the fixed bed generates a fluidized bed and about a dust gasification is to be performed.
- the solid fuel should be introduced into the fluidized bed. In the process itself, the fuel should be separated into fractions of different sizes.
- the object of the invention is derived from fundamentally further develop the method of entrained flow gasification, so that the serious disadvantages of entrained flow gasification can be used, in particular that fuels with high ash contents and high ash flow points can be used without problems that arising at the outlet of the gasifier crude gases fed without using an external Quenchung a Abhitze strong in Rohgas139 (2004)n and the resulting ash or slag can be separated with little investment effort from the raw gases and discharged from the Flugstromvergaser, it being ensured that the dust-like fuels used in the entrained flow gasifier are virtually completely gasified.
- the object of the invention is achieved by a method for entrained flow gasification of solid fuels under pressure, in which solid fuels with gasification agents consisting predominantly of oxygen, are converted in the flow stream to the gasification products raw gas and slag, that in an upward, internally circulating Air flow using first oxygen-rich gasification agent
- Solid fuels used are predominantly solid fuels, which essentially contain dust-like fuels and dusts containing carbon. Furthermore, special forms of solid fuels such. As fuel / water or fuel / oil slurries, can be used with variable solids content. The solid fuels can be used in dry and / or in one or more of these special forms for entrained flow gasification become. They include a wide range of coal, biomass or carbonaceous waste, and in small proportions even liquid or gaseous fuels and residues.
- the deducted from the flow of dust dust-laden raw gases are preferably fed to their further processing indirect heat exchangers and dust collectors.
- the C-containing dusts are almost completely separated from the dust-laden raw gases and returned to the flow stream as far as possible.
- the invention makes use of the knowledge that by a flow gasification with internally circulating air flow in conjunction with a arranged under the entrained flow gasification gasification virtually complete implementation dust-like fuels to oxidized ashes and slags and raw gases is feasible so that the dust-laden raw gases with Temperatures corresponding to those of the raw gas outlet temperatures of fluidized bed gasification, from the flow stream and the oxidized ash and slags with temperatures ⁇ 600 0 C, preferably ⁇ 500 0 C, more preferably ⁇ 400 0 C, can be removed from the moving bed.
- the vertical extent of the flow stream extends from the raw gas outlet at the upper end of the entrained flow gasifier to the surface of the bed of the moving bed.
- the moving bed extends down to the bottoms product discharge located at the bottom of the gasification reactor for entrained flow gasification.
- Essential to the invention is the self-regulating interaction of the processes of gasification of solid fuels and agglomeration of ashes to coarse agglomerates in the circulating air stream with the formation of the moving bed below the circulating air stream consisting of predominantly coarse-grained agglomerates, the material properties of the solid fuels in wide Limits can vary without disturbing influences on the process control.
- the teaching differs fundamentally from the proposals for solution described in DE 26 40 180 B.
- the gasification in the circulating air stream is designed as follows. Into the air stream are introduced as solid fuels, the gasified dust-like fuels and the recycled C-containing dusts and also Nachvergasungsrohgase and first gasification agent.
- the gasification agents are supplied in proportion to the introduced solid fuels in quantity and composition so that the Rohgasabgang temperatures are set below the critical ash intercept, but at least so high that the largely complete gasification of the C-containing components takes place.
- the dusts entrained with the dust-laden raw gases will have C contents of ⁇ about 30 to ⁇ about 80% by weight. After they have been separated from the raw gases, the carbonaceous dusts are almost completely returned to the flow stream and subjected to the gasification process again.
- oxygen-rich gasification agent Fundamental to the largely complete gasification is the use of oxygen-rich gasification agent. Their oxygen concentrations are within a range from 21 to 100 vol .-%, preferably from 40 to 70 vol .-%, in the case of the use of steam with steam / oxygen ratios of 0 to 1.5 kg / m 3 (iN) accordingly, adjusted.
- the high values of oxygen concentrations apply to dusty fuels with high ash contents and high ash flow points.
- the critical ash point ts p is the temperature which must be undershot, so that the ashes in the freeboard and during the cooling of the dust-laden raw gases do not lead to disruptive caking or laying.
- Non-representative, typical numerical examples for the critical ash intercept ts p are z. B. 700 0 C for biomasses, z. B. 1,000 0 C for lignite and z. B. 1.100 0 C for coal.
- lignite which have a critical ash point of, for example, 1,000 0 C, a largely complete gasification is given when the temperatures at the raw gas outlet values of 900 to 950 0 C (temperature range of 50 to 100 K).
- the invention thus exploits the temperature range relevant to most dust-type fuels between these two characteristic temperatures. If the critical ash point ts p below the temperature necessary for gasification, such. For example, in some biomasses, melting and addition point melting additives must be added to the entrained flow gasifier to the critical ash point ts p above the gasification temperature. In this case, the point-increasing additives can be introduced either together with the solid fuels or separately from them.
- the internally circulating air flow is formed as follows.
- the solid fuels, as well as the first gasification agents, are introduced from these locally separated into the gasification chamber in the lower region of the air flow.
- the dense phase promotion has proven itself; but it is also the entry in the form of slurries suitable.
- one or more, preferably distributed over the circumference of the entrained flow gasifier and preferably in a nozzle plane, supply nozzles are provided.
- the first gasification agents are injected by means of gasification agent nozzles, wherein the injection is oriented predominantly horizontally and predominantly radially to the flow axis of the gasification chamber and takes place with inlet velocities of> 10 to about 80 m / s.
- the gasification agent nozzles are also preferably in a nozzle plane. It is also possible to make the locally separate entry of the fuels and the gasification agent via one or more dust burner.
- the gasification in the internally circulating air flow allows due to the very high heating rates and rapid distribution in the reaction chamber, the use of baking and expanding coal, as well as the use of coals with high ash contents and highest ash flow points. For this, it is crucial that temperatures set in the flame areas exceed the ash point temperature by about 1,000 K and more.
- flame regions with temperatures up to> 2000 ° C. are formed in front of the gasification agent nozzles, which generate an upward, hot flow, preferably in the form of a central flow.
- the ash melts, melts and agglomerates.
- it is coarsened in its grain size (about 1 to 5 mm) until the agglomerates from the air flow down into the moving bed.
- the flame areas or the central flow widen until they fill the entire cross-section of the gasification space approximately in the form of a pipe flow at the latest at the raw gas outlet.
- the hot central flow is surrounded by a downward "cold" wall flow, in which the endothermic reactions also dominate.
- the wall flow includes the falling down particles falling out of the flame areas and the central flow due to gravity, and is heavily laden with solids
- the reaction area of the internally circulating stream of air thus consists of one or more central, hot reaction areas in which predominantly run the exothermic oxidation reactions and in which the granulation of the ash takes place and a near the carburetor head of the gasifier wall and the surface of the moving bed, "cold" reaction area in which dominate the endothermic gasification reactions and the main C-conversion takes place.
- the zone of the pipe flow at the upper end of the gasification chamber forms a kind of buffer zone for the required decay of the temperatures before the raw gas outlet.
- the moving bed is adapted to the requirements of the flow stream as follows.
- the second, low-oxygen gasification agents are supplied in quantity and composition so that on the one hand the ash softening point is not exceeded and on the other hand the moving bed regular, d. H. neither channel nor vortex-like, is flowed through.
- the low oxygen content ensures that the ashes and ash granules are almost completely oxidized while avoiding softening or melting. The requirement of relocation and slag-free operation of the moving bed is thus taken into account.
- oxygen concentrations in the range from about 5 to about 20% by volume have proven suitable.
- the oxygen supplied with the second low-oxygen gasifying agent is about 10 to 30% of the total oxygen supplied. The higher values are attributed to ash-rich coals, since the higher ash loadings carry higher carbon loads.
- An advantage of the invention is that the chemical oxygen consumption for the oxidation of the ash constituents of the soil products or the fuel ash is relatively lower than in the classical fixed bed gasification, for example according to the principle Lurgi. From the latter it is known that for the oxidation of the predominantly non-vitrified fuel ashes to the highest oxidation states, a few percent of the gasification oxygen is needed, which is lost to the actual gasification process. This is not the case in the present invention, since the vast majority of the ashes of the dust-like fuels are melted under reducing gas atmospheres with minimal chemical oxygen demand and behave the formed ash granules inert to oxygen in the moving bed.
- the amount of the second gasification agent supplied is limited to such values that the flow rates of the forming Nachvergasungsrohgase at the upper end of the moving bed (based on the solids-free flow cross-section) 0.1 to 0.5 m / s, preferably 0.1 to 0.3 m / s do not exceed.
- the low upper limit of the flow velocities applies to conditions in the air flow, by which Use of gasifiers with relatively low oxygen concentrations predominantly very fine-grained ash granules with grain sizes mainly ⁇ 0.5 mm form (for example, dust-like fuels with high-melting ashes, but with low, critical ash intersections), and the high upper limit according to conditions in which Use of gasification agents with relatively high oxygen concentrations form predominantly coarse-grained ash granules with particle sizes mainly> 0.5 mm.
- the setting of high flow velocities of 0.5 m / s may prove to be expedient.
- large amounts of carbon are reacted, and the ash is cooled accordingly.
- high flow velocities have a positive effect on the fact that the particle sizes of the agglomerates forming the moving bed increase, with the positive result of making the through-bed of the moving bed more uniform.
- the flow rates of Nachvergasungsrohgase at the exit from the moving bed are sufficiently high at 0.1 to 0.5 m / s, so that the introduced into the gasification dust-like fuels deposit only a very small proportion on the moving bed.
- the C concentration in the moving bed is therefore usually so low that oxygen is more than stoichiometric in relation to the carbon and thus the carbon conversion is virtually complete, and the oxidation of all oxidizable ash constituents is guaranteed.
- the post-gasification raw gases entering the circulating air stream from the moving bed are mixed therein, thermally treated and participate in the gasification reactions in accordance with the present gasification conditions.
- second gasification agents are preferably used, which consist of oxygen and carbon dioxide (instead of water vapor) and whose temperature is as close as possible to the ambient temperature.
- This makes it possible to use the sensible heat of the oxidized soil products for the gasification process in Flugstromvergaser and on the other hand to dispense with the otherwise required for the ash handling aftercooling.
- the advantageousness of the use of carbon dioxide is evident from the fact that the outlet temperatures of the bottom products of below about 650 0 C, preferably below about 600 0 C in the case of oxygen and steam as a second gasification agent to below about 400 0 C, preferably be lowered below about 300 0 C in the case of carbon dioxide instead of water vapor.
- the nearly C-free, oxidized soil products can easily be landfilled or be recycled.
- Another advantageous embodiment of the invention consists in supplying steam, which is generated in the water jacket surrounding the gasification chamber, partially or completely to the second gasification means.
- the bed height of the moving bed during operation by a, z. B. radiometric, level measurement is determined and adjusted by controlling the bottom product take-off at the desired height and / or kept constant.
- the bottom product take-off takes place, for example, by means of a rotary grate according to known and proven design.
- the rotary grate at the same time takes over the function of feeding and distributing the second gasification agent over the cross section of the moving bed.
- the object is achieved by a gasification reactor for entrained flow gasification of solid fuel under pressure consisting essentially of a coolable pressure vessel (3) and a heat shield equipped with inner jacket (7), wherein at the upper end of the pressure vessel (3) at least one Rohgasabgang (8 at least one bottom product outlet (9) is arranged at the lower end, wherein the pressure vessel (3) has at least room for a moving bed and an airflow circulating internally over the surface (12) of the moving bed and above for a buffer zone, at a height of approx 1 to 3 m above the surface (12) of the moving bed (13) supply nozzles (15) for the dust-like fuels and Vergasungsstoffdüsen (16) for the supply of first gasification means (17) are arranged, wherein the Vergasungsffendüsen are designed such that the first Gasification agents are injected into the stream of air so that an upward , hot central flow and a downward "cold" wall flow is formed, and wherein at the bottom product take-off (9) at least one supply
- the surrounding walls of the gasification space which extend from the raw gas outlet (8) at the upper end to the bottom product outlet (9) at the lower end of the gasification reactor for entrained flow gasification, are preferably formed over the height without appreciable cross-sectional changes, most simply in the form of a cylinder.
- the entire gasifier is preferably equipped analog fixed-bed gasifiers for cooling with a water jacket; but it can also be used water-cooled tubular membrane walls.
- the protection of the carburetor inner shell (7) on the hot side is preferably in one usual foundation and a ceramic thin coating, z. As with SiC or other refractory ceramic materials as ceramic protection.
- the gasification agent nozzles (16) are distributed according to an advantageous embodiment of the invention evenly distributed over the circumference of the outer pressure jacket (5), radially and 10 to 30 ° inclined upward.
- the feed ports (15) for the solid fuels are advantageously arranged at approximately the same height or below the gasification agent nozzles.
- the height arrangement of the gasifying agent nozzles and the supply nozzle can be varied within certain limits.
- the feed nozzles are located at about the same height or up to about 1 m below the gasification agent nozzles and at least about 1 m above the surface of the bed of the moving bed.
- the gasification agent nozzles and the supply nozzles are arranged on a common plane, approximately 1 to 3 m above the surface of the bed of the moving bed. Compliance with the vertical minimum distance of the feed port to the moving bed guarantees the undisturbed supply of solid fuels, and the equal or lower position of the feed nozzle against the gasification agent nozzles ensures that free oxygen does not react with the solid fuels near the wall.
- the bottom product take-off (9) is advantageously designed as a rotary grate.
- the internally circulating air flow (11) is formed above the surface (12) of the moving bed (13).
- the buffer zone is located above the internally circulating airflow (11).
- the combination of internally circulating air flow and moving bed below the circulating air flow in the manner according to the invention leads to a fundamental simplification of the entire system technology and the gasification operation.
- the most important simplifications concern the gasification reactor for entrainment gasification.
- the enclosure walls of the gasification space which extend from the raw gas outlet at the upper end to the bottom product outlet at the lower end of the entrained flow gasifier, are formed over the height without significant changes in cross section, most conveniently in the form of a cylinder.
- the heat protection of the carburetor inner shell on the hot side is preferably in a conventional foundation and a ceramic coating. A lining is not required. In the case of ceramic coatings are fast Arrival and departure times can be realized.
- the invention also includes a plant for entrained flow gasification under pressure.
- the plant consists of a gasification reactor according to the invention with associated facilities for the supply of gasification agents and solid fuels, for the further processing of the raw gases and the removal of the ash.
- the Rohgasabgang (8) of the gasification reactor is connected to a waste heat exchanger (25) in connection with a dust separator for separating the entrained dusts and a dense flow conveyor for returning the separated dusts in the internally circulating air stream (11) are connected downstream.
- the raw gases leaving the dust collector can be used or fed to a gas treatment device before use.
- Fig. 1 shows a highly simplified schematic representation of a gasification reactor (1) with internally circulating air flow.
- the gasification space (3) of the gasification reactor for entrainment gasification (1) is comprised of a cylindrical pressure vessel (4) which consists of an outer pressure jacket (5), a water space (6) and an inner shell (7).
- the inner shell (7) is furnished and tamped with a refractory material as a ceramic protection.
- At the upper end of the entrained flow gasifier (1) is the raw gas outlet (8) and at the lower end of the bottom product withdrawal (9), of which in the figure, only the upper contour of the rotary grate (10) is indicated.
- the internally circulating air flow (11) is formed above the surface (12) of the moving bed (13).
- a level (14) at a height of about 1 m above the surface (12) of the moving bed (13) are 180 ° offset, two supply nozzle (15) for the dense stream entry of the dusty dry lignite (2) and 6 gasification nozzles ( 16) for the feed of the first gasification agent (17).
- the Gasification nozzles (16) are distributed uniformly over the circumference of the outer pressure jacket (5). They are oriented radially and inclined 30 ° upwards.
- the Rohgasabgang (8) communicates with waste heat exchanger (25) in connection with a hot gas fan (26) for separating the entrained dusts and a dense flow conveyor for returning the separated dusts (20) in the internally circulating air stream (11) are connected downstream.
- the gasification reactor for entrained-flow gasification (1) is gasified at a pressure of 33 bar powdery dry lignite (2) with a water content of 12 wt .-%, an ash content of 6 wt .-% and a critical ash-sintering temperature of 1000 0 C.
- the quantitative supply of the first gasification agent (17) is explained below for the sake of clarity on the basis of one kilogram of dry lignite (2).
- On 1 kg of dry lignite (2), a total of 0.366 m 3 (iN) of oxygen (18), 0.058 m 3 (iN) of carbon dioxide (29) and 0.171 kg of water vapor (19) are supplied.
- the first gasification means (17) are injected at a flow rate of 30 m / s and a temperature of 280 0 C via the Vergasungsffendüsen (16) in the gasification space (3) of the gasification reactor (1).
- the internally circulating air stream (11) in addition to the first gasification agent (17) and the dust-like dry lignite (2) recycled dusts (20) and the moving bed (12) upwardly exiting Nachvergasungsrohgas (21) introduced.
- the second gasification means (28) which are mixed from oxygen (18) and carbon dioxide (29) in the volume ratio of 10 vol .-% oxygen and 90 vol .-% carbon dioxide, with a temperature of 80 0 C introduced into the moving bed (13).
- the extracted via the bottom product take-off (9), oxidized soil products (30) leave the entrained flow gasifier (1) with a temperature of 140 0 C.
- Their C content is ⁇ 2 Ma .-%, so that they will be disposed of or disposed of without further treatment can.
- the second gasification means (28) are quantitatively supplied so that set on the surface (12) of the moving bed (13) flow rates based on the free flow area by 0.3 m / s. This ensures a uniform, regular flow through the moving bed (13).
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Processing Of Solid Wastes (AREA)
- Industrial Gases (AREA)
- Gasification And Melting Of Waste (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2008212869A AU2008212869B2 (en) | 2007-02-07 | 2008-02-07 | Method and device for the entrained-flow gasification of solid fuels under pressure |
EA200901048A EA017334B1 (ru) | 2007-02-07 | 2008-02-07 | Способ и установка для газификации твёрдого топлива в потоке под давлением |
BRPI0807202-7A2A BRPI0807202A2 (pt) | 2007-02-07 | 2008-02-07 | Método e dispositivo para a gaseificação de fluxo arrastado de combustíveis sólidos sob pressão |
CA002676671A CA2676671A1 (en) | 2007-02-07 | 2008-02-07 | Method and device for the entrained-flow gasification of solid fuels under pressure |
CN2008800044676A CN101605876B (zh) | 2007-02-07 | 2008-02-07 | 在加压下对固体燃料进行气流床气化的方法和装置 |
US12/525,927 US8518134B2 (en) | 2007-02-07 | 2008-02-07 | Method and device for the entrained-flow gasification of solid fuels under pressure |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102007006981A DE102007006981B4 (de) | 2007-02-07 | 2007-02-07 | Verfahren, Vergasungsreaktor und Anlage zur Flugstromvergasung fester Brennstoffe unter Druck |
DE102007006981.4 | 2007-02-07 |
Publications (1)
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WO2008095977A1 true WO2008095977A1 (de) | 2008-08-14 |
Family
ID=39398934
Family Applications (1)
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PCT/EP2008/051497 WO2008095977A1 (de) | 2007-02-07 | 2008-02-07 | Verfahren und vorrichtung zur flugstromvergasung fester brennstoffe unter druck |
Country Status (12)
Country | Link |
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US (1) | US8518134B2 (de) |
CN (1) | CN101605876B (de) |
AU (1) | AU2008212869B2 (de) |
BR (1) | BRPI0807202A2 (de) |
CA (1) | CA2676671A1 (de) |
DE (1) | DE102007006981B4 (de) |
EA (1) | EA017334B1 (de) |
PL (1) | PL209860B1 (de) |
TR (1) | TR200905679T1 (de) |
UA (1) | UA95338C2 (de) |
WO (1) | WO2008095977A1 (de) |
ZA (1) | ZA200904988B (de) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
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US20120266539A1 (en) * | 2009-09-18 | 2012-10-25 | Thyssenkrupp Uhde Gmbh | Method for the combined residue gasification of liquid and solid fuels |
RU2530088C1 (ru) * | 2013-04-23 | 2014-10-10 | Леонид Анатольевич Ярыгин | Установка газификации твердого топлива |
WO2018055095A1 (fr) | 2016-09-26 | 2018-03-29 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procede de gazeification de charge de matiere carbonee dans un reacteur a flux entraîne, a rendement ameliore |
CN114496104A (zh) * | 2022-04-02 | 2022-05-13 | 中国矿业大学(北京) | 一种采煤条件下采空区遗煤自燃程度评估方法及系统 |
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US8769964B2 (en) * | 2010-01-05 | 2014-07-08 | General Electric Company | System and method for cooling syngas produced from a gasifier |
US20110197510A1 (en) * | 2010-02-16 | 2011-08-18 | Boris Nickolaevich Eiteneer | Method and apparatus to reactivate carbon solids |
US9120985B2 (en) * | 2010-05-26 | 2015-09-01 | Exxonmobil Research And Engineering Company | Corrosion resistant gasifier components |
DE102011008187B4 (de) * | 2011-01-10 | 2015-08-27 | Suncoal Industries Gmbh | Verfahren zur Erzeugung von Brenn- und Syntheserohgas |
WO2012144101A1 (ja) * | 2011-04-19 | 2012-10-26 | 北海道特殊飼料株式会社 | 燃焼装置及び燃焼方法と、それを用いた発電装置及び発電方法 |
CN102618330B (zh) * | 2011-12-29 | 2014-02-26 | 武汉凯迪工程技术研究总院有限公司 | 一种高温常压生物质气化岛工艺 |
US9109171B2 (en) | 2013-11-15 | 2015-08-18 | General Electric Company | System and method for gasification and cooling syngas |
CN104178222B (zh) * | 2014-08-12 | 2016-05-25 | 新奥科技发展有限公司 | 一种催化气化工艺的配煤方法 |
DE102016210348A1 (de) | 2016-06-10 | 2017-12-14 | Technische Universität Bergakademie Freiberg | Verfahren und Vorrichtung zur Nachoxidation von kohlenstoffhaltigen Vergasungsprodukten |
DE102016210350B4 (de) | 2016-06-10 | 2018-01-18 | Technische Universität Bergakademie Freiberg | Vergasungsreaktor zur Erzeugung von Synthesegasen aus festen Vergasungsstoffen mit Hilfe sauerstoffhaltiger Vergasungsmittel |
CN107460007A (zh) * | 2017-09-26 | 2017-12-12 | 安徽鼎梁生物能源科技开发有限公司 | 一种流动可控的气化炉及流动处理方法 |
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2007
- 2007-02-07 DE DE102007006981A patent/DE102007006981B4/de not_active Expired - Fee Related
-
2008
- 2008-02-07 WO PCT/EP2008/051497 patent/WO2008095977A1/de active Application Filing
- 2008-02-07 CA CA002676671A patent/CA2676671A1/en not_active Abandoned
- 2008-02-07 BR BRPI0807202-7A2A patent/BRPI0807202A2/pt not_active IP Right Cessation
- 2008-02-07 AU AU2008212869A patent/AU2008212869B2/en not_active Ceased
- 2008-02-07 TR TR2009/05679T patent/TR200905679T1/xx unknown
- 2008-02-07 CN CN2008800044676A patent/CN101605876B/zh not_active Expired - Fee Related
- 2008-02-07 PL PL389089A patent/PL209860B1/pl unknown
- 2008-02-07 EA EA200901048A patent/EA017334B1/ru not_active IP Right Cessation
- 2008-02-07 US US12/525,927 patent/US8518134B2/en not_active Expired - Fee Related
- 2008-07-02 UA UAA200909195A patent/UA95338C2/ru unknown
-
2009
- 2009-07-17 ZA ZA200904988A patent/ZA200904988B/xx unknown
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GB1597691A (en) * | 1977-01-05 | 1981-09-09 | Ruhrkohle Ag | Process and plant for the gasification of solid fuels particularly of bituminous coal |
US4445910A (en) * | 1981-02-06 | 1984-05-01 | Zimmerman Edwin H | Gas generating system and process |
EP0214417A2 (de) * | 1985-09-02 | 1987-03-18 | Rheinische Braunkohlenwerke AG. | Verfahren zur Herstellung von Synthesegas aus festen Brennstoffen |
EP0554529A1 (de) * | 1992-02-03 | 1993-08-11 | Deutsche Babcock Energie- und Umwelttechnik Aktiengesellschaft | Verfahren und Vorrichtung zur Vergasung von brennbaren Materialien |
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US20120266539A1 (en) * | 2009-09-18 | 2012-10-25 | Thyssenkrupp Uhde Gmbh | Method for the combined residue gasification of liquid and solid fuels |
RU2530088C1 (ru) * | 2013-04-23 | 2014-10-10 | Леонид Анатольевич Ярыгин | Установка газификации твердого топлива |
WO2018055095A1 (fr) | 2016-09-26 | 2018-03-29 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procede de gazeification de charge de matiere carbonee dans un reacteur a flux entraîne, a rendement ameliore |
CN114496104A (zh) * | 2022-04-02 | 2022-05-13 | 中国矿业大学(北京) | 一种采煤条件下采空区遗煤自燃程度评估方法及系统 |
CN114496104B (zh) * | 2022-04-02 | 2022-06-28 | 中国矿业大学(北京) | 一种采煤条件下采空区遗煤自燃程度评估方法及系统 |
Also Published As
Publication number | Publication date |
---|---|
EA200901048A1 (ru) | 2009-12-30 |
UA95338C2 (ru) | 2011-07-25 |
PL389089A1 (pl) | 2010-03-29 |
TR200905679T1 (tr) | 2009-10-21 |
DE102007006981A1 (de) | 2008-08-14 |
BRPI0807202A2 (pt) | 2014-05-27 |
DE102007006981B4 (de) | 2009-01-29 |
CN101605876A (zh) | 2009-12-16 |
AU2008212869B2 (en) | 2012-05-24 |
ZA200904988B (en) | 2010-03-31 |
CA2676671A1 (en) | 2008-08-14 |
US20100088959A1 (en) | 2010-04-15 |
EA017334B1 (ru) | 2012-11-30 |
CN101605876B (zh) | 2013-07-10 |
US8518134B2 (en) | 2013-08-27 |
AU2008212869A1 (en) | 2008-08-14 |
PL209860B1 (pl) | 2011-10-31 |
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