EP0205517A1 - Procede pour la production de vapeur pauvre en oxyde nitrique avec des combustibles fossiles - Google Patents
Procede pour la production de vapeur pauvre en oxyde nitrique avec des combustibles fossilesInfo
- Publication number
- EP0205517A1 EP0205517A1 EP86900139A EP86900139A EP0205517A1 EP 0205517 A1 EP0205517 A1 EP 0205517A1 EP 86900139 A EP86900139 A EP 86900139A EP 86900139 A EP86900139 A EP 86900139A EP 0205517 A1 EP0205517 A1 EP 0205517A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- combustion
- ceramic
- gasification
- stage
- gas
- 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.)
- Withdrawn
Links
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 239000002803 fossil fuel Substances 0.000 title claims abstract description 7
- 238000000034 method Methods 0.000 title claims description 14
- 238000002485 combustion reaction Methods 0.000 claims abstract description 57
- 239000007789 gas Substances 0.000 claims abstract description 56
- 239000000919 ceramic Substances 0.000 claims abstract description 25
- 238000002844 melting Methods 0.000 claims abstract description 9
- 230000008018 melting Effects 0.000 claims abstract description 9
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 6
- 239000007787 solid Substances 0.000 claims abstract description 6
- 238000002309 gasification Methods 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000002737 fuel gas Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 230000003647 oxidation Effects 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 238000005422 blasting Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000002893 slag Substances 0.000 claims description 3
- 229910052684 Cerium Inorganic materials 0.000 claims description 2
- 229910052581 Si3N4 Inorganic materials 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 238000000605 extraction Methods 0.000 claims description 2
- 229910052746 lanthanum Inorganic materials 0.000 claims description 2
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 claims description 2
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 2
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 2
- HQVNEWCFYHHQES-UHFFFAOYSA-N silicon nitride Chemical compound N12[Si]34N5[Si]62N3[Si]51N64 HQVNEWCFYHHQES-UHFFFAOYSA-N 0.000 claims description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims 1
- 239000013543 active substance Substances 0.000 claims 1
- 239000003054 catalyst Substances 0.000 claims 1
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims 1
- 229910052804 chromium Inorganic materials 0.000 claims 1
- 239000011651 chromium Substances 0.000 claims 1
- 229910052593 corundum Inorganic materials 0.000 claims 1
- 239000010431 corundum Substances 0.000 claims 1
- 239000000463 material Substances 0.000 claims 1
- 239000003245 coal Substances 0.000 abstract description 7
- 239000000446 fuel Substances 0.000 abstract description 5
- 230000003197 catalytic effect Effects 0.000 abstract description 3
- 239000003921 oil Substances 0.000 abstract description 3
- 235000002918 Fraxinus excelsior Nutrition 0.000 abstract 1
- 239000002956 ash Substances 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 101100393542 Peptoclostridium acidaminophilum grdC gene Proteins 0.000 description 9
- 230000015572 biosynthetic process Effects 0.000 description 7
- 230000005855 radiation Effects 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 4
- 235000011941 Tilia x europaea Nutrition 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000010304 firing Methods 0.000 description 4
- 239000004571 lime Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 239000008267 milk Substances 0.000 description 3
- 210000004080 milk Anatomy 0.000 description 3
- 235000013336 milk Nutrition 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000020169 heat generation Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 1
- 238000007084 catalytic combustion reaction Methods 0.000 description 1
- 229910010293 ceramic material Inorganic materials 0.000 description 1
- ZMIGMASIKSOYAM-UHFFFAOYSA-N cerium Chemical compound [Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce] ZMIGMASIKSOYAM-UHFFFAOYSA-N 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 229920005558 epichlorohydrin rubber Polymers 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 230000004992 fission Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C3/00—Combustion apparatus characterised by the shape of the combustion chamber
- F23C3/006—Combustion apparatus characterised by the shape of the combustion chamber the chamber being arranged for cyclonic combustion
- F23C3/008—Combustion apparatus characterised by the shape of the combustion chamber the chamber being arranged for cyclonic combustion for pulverulent fuel
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
- F23C6/04—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
- F23L15/04—Arrangements of recuperators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23M—CASINGS, LININGS, WALLS OR DOORS SPECIALLY ADAPTED FOR COMBUSTION CHAMBERS, e.g. FIREBRIDGES; DEVICES FOR DEFLECTING AIR, FLAMES OR COMBUSTION PRODUCTS IN COMBUSTION CHAMBERS; SAFETY ARRANGEMENTS SPECIALLY ADAPTED FOR COMBUSTION APPARATUS; DETAILS OF COMBUSTION CHAMBERS, NOT OTHERWISE PROVIDED FOR
- F23M5/00—Casings; Linings; Walls
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Definitions
- the invention relates to a method and a device by means of which fossil fuels can be converted into heat almost without nitrogen oxide and can be transferred to the water or water vapor in a steam generator.
- tempera ture arises that are close to the theoretical combustion temperature. These temperatures are above the kinetic formation temperature for nitrogen oxides of 1300 ° C.
- the object of the invention is to create conditions at all points of the steam generator system that nitrogen oxide formation is not possible. For this purpose, conditions must be created at all points so that the nitrogen oxide formation temperature of 1300 ° C is not exceeded in an oxidizing atmosphere.
- the gasification consists of a ceramic-insulated combustion chamber, preferably a cyclone combustion chamber, which converts the fuel used, for example coal, with a partial air flow into a fuel gas with a low calorific value.
- the implementation of the fossil fuel in the first stage is therefore a partial oxidation.
- the gasification temperature is about 1500 - 1900 degrees C.
- the high gasification temperature makes it possible on the one hand to remove the resulting slags in liquid form, and on the other hand the reaction is accelerated so that a relatively complete conversion of the coal or the oils containing solids is ensured.
- a prerequisite for this high temperature is the well-insulating ceramic lining of the combustion chamber, for example with the wear-resistant and insulating ceramic materials such as silicon nitride and silicon carbide.
- the formation of the liquid ash is further promoted by the fact that the ash particles last longer in the reducing atmosphere of the gasification stage, ie. H. remain liquid at lower temperatures, soda. even the lower temperatures that occur in smaller plants and in the initial phase are still sufficient to achieve a liquid ash removal.
- this lower ash melting point of the 1st stage also means that the cracked gas in the blasting chamber must be cooled to lower temperatures before entering the touch heating surfaces. This temperature is approx. 900 grd C and with additives up to approx. 1050 grd C. To achieve this high gasification temperature or temperature of the partial oxidation, it is also necessary that the combustion air is preheated to a relatively high level between 300 and 700 ° C. This happens in the oxidation stages downstream heat exchangers or air heaters.
- the heat exchangers downstream of the oxidation stages also contain heating surfaces for water heating, evaporation and overheating of water vapor. This causes the gases to cool down after the gasification stage and combustion stage to temperatures of 200 ° C and below.
- the hydrogen sulfide be absorbed in lime milk suspension or in an absorption system which works with lime milk suspension.
- the milk of lime converts with the hydrogen sulfide to calcium sulfide, which easily becomes calcium oxide and sulfur by heating with gypsum can be implemented.
- a number of other regeneration processes are possible with this product.
- the use of gypsum for regeneration enables the gypsum mountain to be reduced in the future.
- the cleaned and cooled to below 100 grdC fuel gas is preheated in a heat exchanger before being passed on for combustion.
- the heat for this gas preheating is preferably obtained from a separate heat recovery circuit.
- the heat is recovered via a water circuit that cools the unpurified fuel gas on the heat-absorbing side, and heats the cold cleaned gas on the heat-emitting side using a compact high-performance heat exchanger. Since the water side in the heat exchanger. heat-absorbing side temperatures above 100 ° C may occur, the water circuit is provided with a pre-pressure, for example a nitrogen pad. It is also possible to place a heat pump between the cleaned and unpurified gas.
- a ceramic which can be in the form of a perforated stone plate or honeycomb ceramic.
- this ceramic contains a catalytic additive, which is on the ceramic or with wash coat coated ceramic is applied from 50 to 95% lanthanum and 5 to 50% cerium.
- the combustion in the combustion ceramic saves flame space, so that the heat exchanger units can be arranged immediately after the combustion ceramic.
- the combustion temperature is less than 1300 ° C without taking heat dissipation from the combustion zone into account.
- the flue gas leaving the steam generator after this conversion is almost completely free of nitrogen oxide and sulfur.
- the device for performing the method shows.
- Fig. 1 with 1 the supply of fuel, with 2 the gasification tank, with 3 the ceramic lining, with 4 the supply of preheated air, with 5 the supply of water vapor and with 6 the removal of the slag chnet.
- Some of these wall heating surfaces can be designed as superheaters.
- the heating surfaces 8, 9 and 10 can serve for air preheating, water heating, water evaporation and overheating.
- the deposited dust is removed via 14 and 15.
- the smooth tube heat exchanger for the unpurified fuel gas from the heat recovery circuit is designated, with 13 the compact high-performance heat exchanger on the cleaned gas side and with 14 the circulation pump for the circulating water.
- the cleaning unit of the gasification gas is designated. It is used to remove the hydrogen sulfide, for example by adding lime milk 60, which reacts to lime sulfide.
- the reaction product is removed via 19.
- the cleaned gasification gas enters a gas preheater 13, from which, heated at 21, it enters the flameless catalytic combustion chamber 22. Also in this combustion chamber is part of the 23 in the regenerative heat exchanger warmed air 24 via channel 25.
- the gasification gas is reacted with air in the ceramic 26.
- the exhaust gas emerging from this ceramic cools in the vertical tubes of the straight tube heat exchanger 27.
- the cooled exhaust gas leaves the heat generator at 28 and is introduced into the chimney 29.
- the feed water pump 40 conveys the feed water through the. Preheater 9 and 10 in the drum 41. Via the downpipes 42 it gets into the fin walls 43 and 44 of the fuel gas cooling section and in the straight tube heat exchanger 27 of the oxidation stage. Via the pipes 45, 46 and 47, the boiling water flows into the drum 41, where steam separation also takes place. Over 50 the saturated steam flows into the middle wall superheater 51 and from there via the injection control 52 into the final superheater 8. The live steam reaches the turbine via the pipeline 53.
- the energy of a coal stream of 4.17 t / h which corresponds to a thermal output of 30 MW with a lower calorific value of 6733 kcal / kg and an underlying system efficiency of 92%, is to be implemented without nitrogen oxide and used to produce superheated steam at a pressure of 64 bar and a temperature of 520 grdC.
- 30-degree air with a volume flow of 8.24 m3iN / s flows through a rotating LUVO 23 and is warmed up to 350 grdC by the exhaust gases from the oxidation process.
- a partial flow of 5.32 m3iN / s of the 350-degree air 57 is branched off and passed via 55 to the cracked gas tract.
- the 350% air in the melting chamber 2 becomes a fission gas stream at a temperature of approx. 1700 ° C 6.76 m3iN / s implemented.
- the 1700-degree cracked gas is cooled to 900 ° C. by radiation and convection before it hits the first touch heating surface 8, the final superheater.
- the temperature of the cracked gas drops to 160 ° C.
- the cracked gas cools down further to approx. 80 ° C. At this temperature it leaves the cracked gas tract in order to be freed of its remaining solid particles in a dedusting unit 16, and then subsequently from its sulfurous compounds in a desulfurization unit 18. With approx.
- the cleaned gas flows at 20 into the high-performance heat exchanger 13, which it with 120 grdC leaves and arrives in the combustion chamber of the combustion chamber tract 22.
- the cracked gas is mixed with the remaining partial flow of the 350-degree air 56 of 2.92 m3iN / s and catalytically converted to exhaust gas 9.26 m3iN / s in a structural ceramic unit 26 at 1283 grdC .
- No nitrogen oxide is formed, since the nitrogen oxide formation temperature is not reached at any point in the combustion.
- the exhaust gas formed only has an air excess of 3-8%.
- the extreme freedom from pollutants significantly reduces the signs of corrosion, so that lower exhaust gas temperatures are possible.
- the exhaust gas is cooled to 407 ° C, in order to be subsequently further cooled to 130 ° C in the rotary LUVO 23; the 130% exhaust gas is discharged via the chimney 29 via a fan.
- the 120-degree feed water flow of 10.2 kg / s is pumped with the feed water pump 40 through the ECOs 9 and 10 of the cracked gas tract, where it heats up to 197 ° C. At this temperature it flows into the drum 41, from where it flows through downpipes 42 in partial flows on the one hand into the fin walls of the cracked gas tract, and on the other hand onto the Rohrman tel side of the straight tube heat exchanger 27 of the combustion chamber tract flows.
- saturated steam or boiling water flows over 45, 46 and 47 at 280 ° C into the drum 41.
- the saturated steam is removed from the steam chamber of the drum and passed via 50 to the wall superheater 51, where the steam in a first stage is heated to 420 ° C.
- an injection control 52 approx. 0.4 kg / s feed water of 120 grdC was added, which reduced the superheated steam to 382 grdC. is cooled. At this temperature it reaches the final superheater 8, where it is brought to its concession state of 520 grdC and 64 bar and then passed on to the turbine via 53.
- the air 24 for the gasification and combustion flows through the LUVO 23, which has a diameter of approximately 4 m, and then divides into two partial flows 56 and 57.
- One partial flow 57 enters the cracked gas tract and mixes with the ground hard coal 1 and the water vapor 5 in a ceramic-lined, fully insulated cyclone melting chamber 2 with two burners of the same size.
- the melting chamber 2 has a diameter of approximately 4.2 m and a cylindrical height of approximately 4.2 m.
- the liquid ash is drawn off with the exclusion of air via the funnel adjoining the lower end of the cylindrical part.
- the cracked gas is fed into the blasting chamber of the steam generator via a channel 2 of approximately 2.5 mx 0.75 m, which projects somewhat into the lower part of the melting chamber.
- the hot cracked gas is cooled in an empty train with an edge length of 4.0 m and 3.5 m and a height of approx. 6.5 m before it hits the 1st touch heating surface .
- the fuel gas is cooled to the extent that it can be freed from its solid particles in a fabric filter unit 17 in a rectangular second train of 2.5 mx 4.0 m.
- a subsequent desulfurization unit 18 which has a diameter of approx. 3.5 m and a height of approx. 4.5m, the sulfurous compounds are removed from the cracked gas.
- a high-performance heat exchanger 13 with the outer dimensions of 1.8 mx 1.38 mx 0.8 m, the cracked gas is heated again and then fed to the combustion chamber tract.
- the conversion to exhaust gas takes place catalytically in a ceramic 26 lying under the combustion chamber space.
- the free heat is dissipated in a straight tube heat exchanger 27.
- This heat exchanger consists of a base plate with the same dimensions as the combustion chamber and it has a height of 3.0 m.
- the exhaust gas flows through 8640 ISO pipes (20 x 2.0).
- FIG. 2 shows the individual components of the device according to the invention in a compact heat generation unit with integrated gas cleaning at a thermal output of 30 MW.
- the fully ceramic-insulated gasification chamber with liquid ash extraction is designated by 1. It is connected to the radiation evaporator 3 via the connection channel 2.
- This radiation evaporator 3 consists of fin tubes through which water flows.
- the radiation evaporator forms together with the 2nd part, which consists of the superheater and preheater part, which is equipped with heat exchanger blocks 4, 5, 6 and for the heat recovery circuit 7 and 3, the entire cracked gas tract.
- the opening to the dedusting unit 16 which consists of a bag filter, is designated.
- the connection channel from the deduster unit to the desulfurization unit 9, to which the high-performance heat exchanger 10 belongs designated.
- the connecting channel 11 guides the cleaned gas into the combustion chamber tract 12 with the structural ceramic units and the straight tube evaporator. All of the exhaust gas flows to the chimney 14 via the exhaust gas duct 13.
- the main dimensions of the unit shown in FIG. 2 for the gasification chamber (1) are 4.20 m in height (20) and 4.20 m in diameter (21).
- the dimensions of the fuel gas cooling and cleaning part are the height (22) of 12.0 m, the lower width (23) of 8.0 m, the upper width (24) of 5.0 m and the total depth (25) of 4 m.
- the combustion chamber tract (12) has a height of (26) of 3.0 m and a diameter (27) of 2.5 m.
- the entire heat generation unit can be made even more compact on the planning side.
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Chimneys And Flues (AREA)
Abstract
Il est possible de produire de la chaleur pratiquement sans oxyde nitrique à partir de combustibles fossiles comme le charbon, le pétrole et le gaz si la combustion de ces produits s'effectue en plusieurs étapes. Le combustible (1) qui contient parfois des cendres est mélangé à de l'air (4) et de la vapeur d'eau (5) chauffés à haute température et converti en gaz combustible dans une chambre de fusion (2) entièrement garnie de céramique; le gaz combustible obtenu est refroidi pour préchauffage du circuit et production de vapeur (53), débarrassé des matières solides (16) et de l'acide sulfhydrique (18) et amené à un étage de combustion (22) catalytique ou non catalytique sans flamme. L'étage de combustion n'atteint qu'une température nettement inférieure à 1300oC en raison de la valeur calorifique moindre du gaz introduit dans la céramique de combustion (26), de sorte que la combustion s'effectue presque sans oxyde nitrique.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19843447147 DE3447147A1 (de) | 1984-12-22 | 1984-12-22 | Verfahren und vorrichtung fuer die stickoxidfreie dampferzeugung mit fossilen brennstoffen |
DE3447147 | 1984-12-22 |
Publications (1)
Publication Number | Publication Date |
---|---|
EP0205517A1 true EP0205517A1 (fr) | 1986-12-30 |
Family
ID=6253709
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP86900139A Withdrawn EP0205517A1 (fr) | 1984-12-22 | 1985-12-19 | Procede pour la production de vapeur pauvre en oxyde nitrique avec des combustibles fossiles |
Country Status (5)
Country | Link |
---|---|
US (1) | US4716844A (fr) |
EP (1) | EP0205517A1 (fr) |
JP (1) | JPS62501230A (fr) |
DE (2) | DE3447147A1 (fr) |
WO (1) | WO1986003821A1 (fr) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0432293B1 (fr) * | 1989-12-21 | 1995-03-01 | Kawasaki Jukogyo Kabushiki Kaisha | Procédé pour la récupération de gaz résiduaires d'un foyer à charbon |
DE69224239T2 (de) * | 1991-07-05 | 1998-05-20 | Thermatrix Inc | Verfahren und Vorrichtung zur gesteuerten Reaktion in einer Reaktionsmatrix |
US5165884A (en) * | 1991-07-05 | 1992-11-24 | Thermatrix, Inc. | Method and apparatus for controlled reaction in a reaction matrix |
US5325796A (en) * | 1992-05-22 | 1994-07-05 | Foster Wheeler Energy Corporation | Process for decreasing N2 O emissions from a fluidized bed reactor |
US6003305A (en) | 1997-09-02 | 1999-12-21 | Thermatrix, Inc. | Method of reducing internal combustion engine emissions, and system for same |
US5989010A (en) | 1997-09-02 | 1999-11-23 | Thermatrix, Inc. | Matrix bed for generating non-planar reaction wave fronts, and method thereof |
US6015540A (en) * | 1997-09-02 | 2000-01-18 | Thermatrix, Inc. | Method and apparatus for thermally reacting chemicals in a matrix bed |
US6282371B1 (en) | 1998-07-02 | 2001-08-28 | Richard J. Martin | Devices for reducing emissions, and methods for same |
US6145454A (en) * | 1999-11-30 | 2000-11-14 | Duke Energy Corporation | Tangentially-fired furnace having reduced NOx emissions |
DE102008064321A1 (de) * | 2008-09-19 | 2010-04-01 | Ecoenergy Gesellschaft Für Energie- Und Umwelttechnik Mbh | Externe Frischluftvorwärmung bei Feststofffeuerungen |
Family Cites Families (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3818869A (en) * | 1973-01-02 | 1974-06-25 | Combustion Eng | Method of operating a combined gasification-steam generating plant |
US4060378A (en) * | 1974-12-11 | 1977-11-29 | Energiagazdalkodasi Intezet | Method of firing and furnace therefor |
CA1070963A (fr) * | 1976-03-08 | 1980-02-05 | Exxon Research And Engineering Company | Minimisation de la production d'oxydes d'azote lors du fonctionnement de chambres de combustion de turbines a gaz |
US4097217A (en) * | 1976-12-09 | 1978-06-27 | The Keller Corporation | Method for converting combustor from hydrocarbonaceous fuel to carbonaceous fuel |
DD145181A3 (de) * | 1978-09-28 | 1980-11-26 | Helmut Peise | Reaktor zur gaserzeugung durch partialoxidation unter erhoehtem druck |
US4289502A (en) * | 1979-05-30 | 1981-09-15 | Texaco Development Corporation | Apparatus for the production of cleaned and cooled synthesis gas |
US4290269A (en) * | 1979-10-09 | 1981-09-22 | Modo-Chemetics Ab | Process for the efficient conversion of water-containing organic materials as fuels into energy |
US4344373A (en) * | 1979-10-30 | 1982-08-17 | Agency Of Industrial Science And Technology | Method for pyrolyzing |
US4354821A (en) * | 1980-05-27 | 1982-10-19 | The United States Of America As Represented By The United States Environmental Protection Agency | Multiple stage catalytic combustion process and system |
US4295818A (en) * | 1980-05-27 | 1981-10-20 | United States Of America | Catalytic monolith and method of its formulation |
US4336769A (en) * | 1981-03-31 | 1982-06-29 | Foster Wheeler Energy Corporation | Integral vapor generator/gasifier system |
FR2517025A1 (fr) * | 1981-11-25 | 1983-05-27 | Fives Cail Babcock | Installation de chaudiere a combustible solide |
US4430094A (en) * | 1981-12-21 | 1984-02-07 | Foster Wheeler Energy Corporation | Vapor generating system having a plurality of integrally formed gasifiers extending to one side of an upright wall of the generator |
DE3339741A1 (de) * | 1983-09-09 | 1985-05-15 | Insumma Projektgesellschaft mbH, 8500 Nürnberg | Brennwertgeraet fuer kohlenwasserstoffe |
US4558651A (en) * | 1983-10-19 | 1985-12-17 | International Coal Refining Company | Fired heater for coal liquefaction process |
US4602573A (en) * | 1985-02-22 | 1986-07-29 | Combustion Engineering, Inc. | Integrated process for gasifying and combusting a carbonaceous fuel |
-
1984
- 1984-12-22 DE DE19843447147 patent/DE3447147A1/de not_active Withdrawn
-
1985
- 1985-09-06 DE DE19853531815 patent/DE3531815A1/de not_active Withdrawn
- 1985-12-19 US US06/865,721 patent/US4716844A/en not_active Expired - Fee Related
- 1985-12-19 WO PCT/EP1985/000722 patent/WO1986003821A1/fr not_active Application Discontinuation
- 1985-12-19 EP EP86900139A patent/EP0205517A1/fr not_active Withdrawn
- 1985-12-19 JP JP61500372A patent/JPS62501230A/ja active Pending
Non-Patent Citations (1)
Title |
---|
See references of WO8603821A1 * |
Also Published As
Publication number | Publication date |
---|---|
DE3447147A1 (de) | 1986-06-26 |
US4716844A (en) | 1988-01-05 |
DE3531815A1 (de) | 1987-03-19 |
WO1986003821A1 (fr) | 1986-07-03 |
JPS62501230A (ja) | 1987-05-14 |
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