AU2006201142B2

AU2006201142B2 - Method and device for high-capacity entrained flow gasifier

Info

Publication number: AU2006201142B2
Application number: AU2006201142A
Authority: AU
Inventors: Dietmar Adler; Joachim Lamp; Friedemann Mehlhose; Manfred Schingnitz
Original assignee: Siemens Energy Global GmbH and Co KG
Current assignee: Siemens Energy Global GmbH and Co KG
Priority date: 2005-10-07
Filing date: 2006-03-20
Publication date: 2011-07-21
Anticipated expiration: 2026-03-20
Also published as: CN1944593B; ZA200607404B; AU2006201142A1; DE102005048488A1; DE102005048488B4; CA2534407A1; DE102006029595A1; DE102006029595B4; US20070079554A1; DE102005048488C5; DE202005021659U1; CN1944593A

Abstract

This invention relates to a method for the gasification of pulverized fuels that exist from solid fuels such as bituminous coals, lignite coals, and their cokes, petroleum cokes, coke from peat or biomass, in entrained flow, with an oxidizing medium containing free oxygen, by partial oxidation at pressures between atmospheric pressure and 80 bar, and at temperatures between 1,200 and 1,900 *C, at high reactor capacities between 1,000 and 1,500 MW, consisting of the component technologies: metering of the fuel, gasification reaction in a gasification reactor with cooled reaction chamber contour, quench-cooling, crude gas scrubbing, and partial condensation, wherein - a fuel, preferably a pulverized fuel, with a water content < 10 wt.% and a grain size < 200 gm, is supplied to multiple identically engaged metering systems that feed the fuel, preferably the pulverized fuel, through transport pipes (1.4) to multiple gasification burners (2.1) located at the head of a reactor (2), which are symmetrically arranged and contain additional oxygen infeeds, S:P59914 multiple dust burners (2.1) with oxygen infeed are ignited in the head of the gasification reactor (2) by ignition and pilot burners (2.2), the quantities of the pulverized fuel and oxygen fed to the dust burners (2.1) are determined, with the overall total of all amounts of pulverized fuel and oxygen supplied being determined, and with a regulating mechanism assuring that the oxygen ratio neither exceeds nor falls below a ratio of 0.35 to 0.65, regardless of the distribution of pulverized fuel and oxygen to the burners (2.1), the pulverized fuel is converted in the gasification reactor (2) at temperatures between 1,200 and 1,900 *C and at pressures between atmospheric pressure and 80 bar, into a crude synthesis gas and slag, the hot crude gas at 1,200 to 1,900 *C and the slag are cooled together down to the condensation point at temperatures between 180 OC and 240 *C in a quenching cooler (3) by injecting water, the cooled crude gas is fed to further treatment stages such as water scrubbing, partial condensation, or catalytic processes, and devices for implementing the method. S:P59914 4/5 Fig.4 1.1 2.1 Fg \2 3.2 3.4 3.1 -.

Description

AUSTRALIA Patents Act 1990 COMPLETE SPECIFICATION STANDARD PATENT Applicant(s): Future Energy GmbH Dr. Manfred Schingnitz Invention Title: METHOD AND DEVICE FOR HIGH-CAPACITY ENTRAINED FLOW GASIFIER The following statement is a full description of this invention, including the best method of performing it known to me/us: - 2 Method and device for high-capacity entrained flow gasifier TECHNICAL FIELD The present invention relates to a method for entrained flow gasification with very high capacity that can be used for supplying large-scale syntheses with synthesis gas. BACKGROUND In a gas production technique, the autothermic entrained flow gasification of solid, liquid, and gaseous fuels has been known in the technology of gas production for years. For reasons of synthesis gas quality, the ratio of fuel to gasification medium containing oxygen is chosen so that higher carbon compounds are completely cracked for reasons of synthesis gas quality into synthesis gas components such as CO and H 2 , and the inorganic components are discharged as molten slag; see J. Carl, P. Fritz, NOELL-KONVERSIONSVERFAHREN, EF-Verlag fir Energie- und Umwelttechnik GmbH, 1996, p. 33 and p. 73. According to various systems used in industry, gasification gas and molten slag can be discharged separately or together from the reaction chamber of the gasification device, as shown in DE 197 131 Al. Systems provided with a refractory lining or cooled systems are used for the internal confinement of the reaction S: P59914 2334953.2 (GHMatters) P591 14AU - 3 chamber structure of the gasification system; see DE 4446 803 Al. EP 0677 567 B1 and WO 96/17904 show a method in which the gasification chamber is confined by a refractory lining. This has the drawback that the refractory masonry is loosened by the liquid slag formed during gasification, which leads to rapid wear and high repair costs. This wear process increases with increasing ash content. Thus such gasification systems have a limited service life before replacing the lining. Also, the gasification temperature and the ash content of the fuel are limited; see C. Higman and M. van der Burgt, "Gasification", Verlag ELSEVIER, USA, 2003. A quenching or cooling system is also described, with which the hot gasification gas and the liquid slag are carried off together through a conduit that begins at the bottom of the reaction chamber, and are fed into a water bath. This joint discharge of gasification gas and slag can lead to plugging of the conduit and thus to limitation of availability. DE 3534015 Al shows a method in which the gasification media, powdered fuel and oxidizing medium containing oxygen, are introduced into the reaction chamber symmetrically through multiple burners in such a way that the flames are mutually S:P59914 23349532 (GHatters) P59114 AU -4 diverted. The gasification gas loaded with powdered dust flows upward and the slag flows downward into a slag-cooling system. As a rule, there is a device above the gasification chamber for indirect cooling utilizing the waste heat. However, because of entrained liquid slag particles there is the danger of deposition and coating of heat exchanger surfaces, which hinders heat transfer and may lead to plugging of the pipe system and/or erosion. The danger of plugging is counteracted by taking away the hot crude gas with a circulated cooling gas. Ch. Higmann and M. van der Burgt in "Gasification", page 124, Verlag Elsevier 2003, describe a method in which the hot gasification gas leaves the gasifier together with the liquid slag and directly enters a waste heat boiler positioned perpendicularly below it, in which the crude gas and the slag are cooled with utilization of the waste heat to produce steam. The slag is collected in a water bath, while the cooled crude gas leaves the waste heat boiler from the side. A series of drawbacks detract from the advantage of waste heat recovery by this system. To be mentioned here in particular is the formation of deposits on the heat exchanger tubes, which lead to hindrance of heat transfer and to corrosion and erosion, and thus to lack of availability. S: P59914 2334053_2 (GHMeters) PS114 AU - 5 CN 200 4200 200 7.1 describes a "Solid Pulverized Fuel Gasifier", in which the powdered coal is fed in pneumatically and gasification gas and liquefied slag are introduced into a water bath through a central pipe for further cooling. This central discharge in the central pipe mentioned is susceptible to plugging that interferes with the overall operation, and reduces the availability of the entire system. The capacity of the various gasification technologies mentioned is limited to about 500 MW, which is attributable in particular to the fuel infeed to the gasification reactor. It is to be understood that, if any prior art publication is referred to herein; such reference does not constitute an admission that the publication forms a part of the common general knowledge in the art, in Australia or any other country. SUMMARY OF THE INVENTION According to a first aspect, there is provided, a high capacity reactor for the gasification of pulverized fuels from solid fuels such as bituminous coals, lignite coals and their cokes, petroleum cokes, cokes from peat or biomass, in entrained flow, with an oxidising medium containing free oxygen at temperatures between 1,200 and 1,900 OC, and at pressures between atmospheric S :P59914 2334953_2 (GHMattes) P59114AU -6 pressure and 80 bar, into a crude synthesis gas and slag, the reactor comprising: a reactor head; an ignition and pilot burners disposed at said head of the reactor; a plurality of equal gasification burners disposed at said head of the reactor; a plurality of lock hoppers and dosing systems arranged to supply said pulverized fuels to said plurality of equal gasification burners; individual transport lines assigned to each gasification burner, said individual transport lines connecting and feeding said pulverized fuels from said lock hopper and dosing systems to the respective gasification burner; wherein each gasification burner is connected and fed by at least two different lock hoppers and dosing systems; and a measuring system configured to measure and regulate amounts of pulverized fuel and oxygen flowing in each of said plurality of equal gasification burners, said measuring system controlling the overall total amounts of pulverized fuel and oxygen flowing in the reactor. According to a second aspect, there is provided an apparatus for gasifying combustible dusts comprising hard coal, S:P59914 23349532 (GHMatter) P59114AU lignite, petroleum coke, or solid grindable residues, and slurries, comprising: an entrained gasification reactor for gasifying the combustible dusts at temperatures ranging from 1200 to 1900 0 C and pressures of up to 80 bar; wherein said gasification reactor comprises a plurality of gasification burners, each burner having an individual feed port; wherein each gasification burner comprises a plurality of supply ports connected to said feed port; a plurality of lock hopper and dosing systems arranged to supply dust or slurries to the gasification burners; and a plurality of supply lines corresponding in number with said plurality of supply ports leading from each lock hopper and dosing system to said supply ports, and configured to provide dust or slurries to each feed port of each burner. In high performance entrained flow reactors, it is necessary to arrange a plurality of gasification burners if one wants to achieve secure conversion of the combustible. In order to ensure start up and secure operation of such reactors, a central ignition and pilot burner is disposed that is surrounded by 3 dust burners symmetrically spaced 120 degrees apart from each other. In order to allow introducing the large amounts of combustible dust of, for example, 100-400 t/h into the S :P59914 2334953_2 (GH~ates) P59114 AU - 8 gasification reactor operated under pressure, a plurality of lock hopper and dosing systems are arranged for supplying dust to the gasification burners. It is also possible to associate a lock hopper and dosing system with each gasification burner. Another possibility is to connect each lock hopper and dosing system to a plurality of gasification burners in order to increase their availability. There is also provided a method in which one single lock hopper and dosing system is associated with each gasification burner. For this purpose, supply lines lead from each lock hopper and dosing system to a respective one of the gasification burners. Each of the burners may have three feed ports for these supply lines. Further, supply lines may lead from each lock hopper and dosing system to the feed ports in the various gasification burners. The supply lines of three lock hopper and dosing systems may thus lead to different gasification burners so that three gasification burners each having three feed ports may be provided. Each feed port is supplied with combustible from another lock hopper and dosing system. There may be fewer lock hopper and dosing systems than gasification burners. Two lock hopper and dosing systems may, for example, supply combustible to three gasification burners through lines. The combustible dust of each lock hopper and dosing system is distributed evenly S:P59914 23349532 (GHMater) P591 14AU -9 to the gasification burners through the respective supply lines. Providing a plurality of lock hopper and dosing systems offers the advantage that the burners will continue to operate steadily upon failure of one of them. In case each gasification burner is supplied through at least two supply lines, one supply line is led from each lock hopper and dosing system to each burner so that redundancy is provided in the event of a system failure. As all the gasification burners are supplied uniformly with combustible dust, it is possible to mix combustible dusts from diverse lock hopper and dosing systems of the large plants in the gasification burner. There is also disclosed a method for the gasification of pulverized fuels that exist from solid fuels such as bituminous coals, lignite coals, and their cokes, petroleum cokes, coke from peat or biomass, in entrained flow, with an oxidizing medium containing free oxygen, by partial oxidation at pressures between atmospheric pressure and 80 bar, and at temperatures between 1,200 and 1,900 0 C, at high reactor capacities between 1,000 and 1,500 MW, consisting of the component technologies: metering of the fuel, gasification reaction in a gasification reactor with cooled reaction chamber S: P59914 2'34"32 (GHMAtters) P59114AU - 10 contour, quench-cooling, crude gas scrubbing, and partial condensation, wherein - a fuel, preferably a pulverized fuel, with a water content < 10 wt.% and a grain size < 200 pm, is supplied to multiple identically engaged metering systems that feed the fuel, preferably the pulverized fuel, through transport pipes to multiple gasification burners located at the head of a reactor, which are symmetrically arranged and contain additional oxygen infeeds, - multiple dust burners with oxygen infeed are ignited in the head of the gasification reactor by ignition and pilot burners, - the quantities of the pulverized fuel and oxygen fed to the dust burners are determined, with the overall total of all amounts of pulverized fuel and oxygen supplied being determined, and with a regulating mechanism assuring that the oxygen ratio neither exceeds nor falls below a ratio of 0.35 to 0.65, regardless of the distribution of pulverized fuel and oxygen to the burners, S:P59914 2334953_2 (GHMttern) P59114AU - 11 - the pulverized fuel is converted in the gasification reactor at temperatures between 1,200 and 1,900 *C and at pressures between atmospheric pressure and 80 bar, into a crude synthesis gas and slag, - the hot crude gas at 1,200 to 1,900 *C and the slag are cooled together down to the condensation point at temperatures between 180 *C and 240 *C in a quenching cooler by injecting water, - the cooled crude gas is fed to further treatment stages such as water scrubbing, partial condensation, or catalytic processes. This enables the conversion of fuels refined into pulverized fuel, such as lignite and bituminous coals, petroleum coke, solid grindable refuse, and solid-liquid suspensions, so-called slurries, into synthesis gas. The fuel is reacted at temperatures between 1,200 and 1,900 *C with a gasification medium containing free oxygen, at pressures up to 80 bar, by partial oxidation to gases containing CO and H 2 . This is done in a gasification reactor that is distinguished by a multiple burner system and by a cooled gasification chamber. S: P59914 2334953.2 (GHMtaers) P59114AU - 12 The gasification method for the gasification of solid fuels containing ash at very high capacities with an oxidizing medium containing oxygen can be based on an entrained flow reactor whose reaction chamber contour may be confined by a cooling system, with the pressure in the cooling system being kept higher than the pressure in the reaction chamber. In one embodiment the process for preparing the fuel and feeding it to the gasification burners may be as follows: with dry pneumatic infeed by the dense-flow transport principle, the fuel is dried, pulverized to a grain size of < 200 pm, and passed through operational bunkers to pressurized sluices, in which the dust like fuel is brought to the desired gasification pressure by introducing a non-condensing gas such as N 2 or CO 2 . Different fuels can be used here at the same time. By a system of multiple such pressurized sluices, they can be loaded and pressurized alternately. The dust under pressure then can then be sent to metering tanks, in the bottom of which a very dense fluidized bed is produced by likewise introducing a non-condensing gas, with one or more transport pipes immersed in the bed and opening into the burners of the gasification reactor. A separate infeed and metering system is associated with each high-capacity burner. The fluidized fuel dust can be caused to flow to the burners by applying a pressure differential between the metering tanks and the burners of the gasification reactor. The amount of S:P59914 2334953_2 (GHMatter) P59114AU - 13 flowing fuel dust can be measured, regulated, and monitored by measurement devices and monitors. With the proposed reactor, there may be the ability to pulverize the undried fuel likewise to a grain size of < 200 pm and to mix the pulverized fuel with water or oil and to feed it as a slurry to the burners of the gasification reactor. The method of infeed, which is not described at this point, is configured by one skilled in the art according to the means known to him. An oxidizing medium containing free oxygen may be supplied to the burners at the same time, and the slurry can be converted to crude synthesis gas by partial oxidation. The gasification may take place at temperatures between 1,200 and 1,900 *C and at pressures up to 80 bar. The reactor may have a cooled reaction chamber contour that is made up of a cooling shield. This can consist of a tubular shield welded gas-tight that is studded and lined with a material that is a good heat conductor. The crude gas produced in the gasification reactor may leave the gasification reactor together with the liquid slag formed from the fuel ash and can be sent to a chamber located perpendicularly below it, in which the hot crude gas and the liquid slag are cooled by injecting water. The gas can be cooled S:P59914 2334953_2 (GHMarem) P59114AU - 14 completely down to the condensation point of the gas by spraying in excess water. The temperature is then between 180 and 240 oC, depending on the pressure. In one embodiment, a limited amount of cooling water can be fed in to cool the crude gas and slag by partial cooling to 700 to 1,100 OC, for example, and then to utilize the sensible heat of the crude gas to produce steam in a waste heat boiler. Partial quenching or partial cooling may prevent or sharply reduces the risk of slag caking on the tubes of the waste heat boiler. The water or recycled gas condensate needed for complete or partial cooling can be supplied through nozzles that are located directly on the jacket of the cooling chamber. The cooled slag can then be collected in a water bath and is discharged from the process. The crude gas cooled to temperatures between 200 and 300 *C may then sent to a crude gas scrubber, which is suitably a Venturi scrubber. The entrained dust can then be removed down to a particle size of about 20 pm. This degree of purity may be inadequate for carrying out subsequent catalytic processes, for example crude gas conversion. It also has to be considered that salt mists can also be entrained in the crude gas, which have detached from the powdered fuel during gasification and are carried off with the crude gas. To remove both the fines < 20 pm and the salt mists, the scrubbed crude gas can be fed to a condensation step in S: P59914 2334953_2 (GHMatters) P59114AU - 15 which the crude gas may be chilled indirectly by 5 to 10 OC. Water can then be condensed from the crude gas saturated with steam, which may take up the described fine dust and salt particles. The condensed water containing the dust and salt particles can be separated from the crude gas in a following separator. The crude gas purified in this way can then be fed directly, for example, to a desulfurization system. It would be advantageous if at least some embodiments of the present disclosure provided a gasification method that permits maximum capacities of 1,000 to 1,500 MW with reliable and safe operation. BRIEF DESCRIPTION OF THE DRAWINGS Other features of the application will become apparent from the following detailed description considered in connection with the accompanying drawings. It is to be understood, however that the drawings are designed as an illustration only and not as a definition of the limits of the disclosure. The Figures show: Fig. 1 shows an example in which each gasification burner is associated with one lock hopper and dosing system; S:P59914 23349532 (GH tters) P59114AU - 16 Fig. 2 shows an example in which three gasification burners are associated with three lock hoppers and dosing systems, whereas each dust burner has one feed line from each of the three lock hoppers and dosing systems; Fig. 3 shows an example in which three gasification burners are associated with two lock hoppers and dosing systems, whereas each gasification burner has one feed line from each of the two lock hoppers and dosing systems; Fig. 4: shows a block diagram of one embodiment of the technology; Fig. 5: shows an embodiment of a metering system for pulverized fuel; Fig. 6: shows an embodiment of a device for feeding pulverized fuel for high-capacity generators; Fig. 7: shows an embodiment of a gasification reactor with full quenching; and Fig. 8: Shows an embodiment of a gasification reactor with partial quenching. DETAILED DESCRIPTION OF EMBODIMENTS OF THE INVENTION Notwithstanding any other forms which may fall within its scope, preferred forms of the invention will now be described, by way of example only with reference to the accompanying drawings in which: S: P59914 23349532 (GHMatters) P59114AU - 17 Fig. 1 shows an example in which each lock hopper and dosing system 1, 2, 3 is associated with one gasification burner 4, 5, 6. The objective is to feed a gasification reactor for entrained flow gasification of carbon dust with an gross input of 1,000 MW with the 180 Mg/h carbon dust needed for this purpose. For this purpose, there are three lock hopper and dosing systems 1, 2, 3 (FIG. 1), each supplying a gasification burner 4, 5, 6 through supply ports 4.1 through 6.3 thereof with 60 Mg/h combustible dust through three supply lines 1.1 through 3.3 with a feed capacity of 20 Mg/h. The capacity of each dust supply line 1.1 through 3.3 can be set in the range from 15-30 Mg/h. The three dust supply lines 1.1 through 3.3 of each lock hopper and dosing system 1, 2, 3 thereby end in a gasification burner 4, 5, 6, supplying it with the 60 Mg/h carbon dust mentioned. All three lock hopper and dosing systems 1, 2, 3 must be in operation. Operation with two of the three gasification burners 4, 5, 6 results in unacceptable crooked burning in the gasification reactor. In the event of a failure of only one of supply lines 1.1 through 3.3, burner 4, 5, 6 of concern may also be operated for a limited time with two supply lines. Fig. 2 shows an example in which three lock hoppers and dosing systems 1, 2, 3 are associated with all three gasification burners 4, 5, 6. The objective is the same as in FIG. 1. S: P59914 2334953_2 (GHMatters) P59114AU - 18 However, the three supply pipes 1.1 through 3.3 of each lock hopper and dosing system 1, 2, 3 are not connected to one gasification burner, but with all the three. Upon failure of one lock hopper and dosing system 1, 2, 3, each gasification burner 4, 5, 6 may also be supplied for a limited time from the two still operating lock hopper and dosing systems 1, 2, 3. Fig. 3 shows two lock hopper and dosing systems 1, 2 which are connected to three gasification burners 4, 5, 6. The objective is to supply a gasification reactor for entrained flow gasification of carbon dust having an output of 500 MW with the 90 Mg/h carbon dust needed for this purpose. For this purpose, 2 lock hopper and dosing systems 1, 2, each having a capacity of 45 Mg/h, are arranged, each of the three supply lines 1.1 through 2.3 having an output of 15 Mg/h. Each gasification burner 4, 5, 6 is supplied from two supply lines 1.1 through 2.3 originating from a respective one of the lock hopper and dosing systems 1, 2. As a result, two lock hopper and dosing systems 1, 2 can be utilized for middle performance gasification reactors having three gasification burners 4, 5, 6. Figure 4 is a block diagram showing the process steps of pneumatic metering of pulverized fuel, gasification in a gasification reactor with cooled reaction chamber structure 2, S: P59914 2334953_2 (GHMaters) P59114AU - 19 quench-cooling 3, crude gas scrubbing 4, in which there can be a waste heat boiler 4.1 between the quench-cooling 3 and the crude gas scrubbing 4, and a condensation or partial condensation 5 follows the crude gas scrubber 4. Figure 5 shows a metering system for pulverized fuel consisting of a bunker 1.1 followed by two pressurized sluices 1.2, into which lead lines 1.6 for inert gas, and at the top of which depressurization lines 1.7 exit, with lines to the metering tank 1.3 leaving the pressurized sluices 1.2 from the bottom. There are fittings on the pressurized sluices 1.2 for monitoring and regulating. A line 1.5 for fluidizing gas leads into the metering tank from below, which provides for fluidizing the gas, and the fluidized pulverized fuel is fed through the transport line 1.4 to a gasification reactor 2. Figure 6 shows alternative design of the device for feeding pulverized fuel for high-capacity generators 2, wherein a bunker 1.1 has three discharges for pulverized fuel, each leading to pressurized sluices 1.2, with each of the three pressurized sluices transporting pulverized fuel streams to one of three metering tanks 1.3, from which transport lines 1.3 lead to the dust burners 1.2 with oxygen infeed of the reactor. There are three dust burners 2.1 on each reactor 2 with oxygen feed, with S: P59914 23349532 (GHNattem) P59114AU - 20 an ignition and pilot burner 2.2 to start the reaction. Because of such intensive fluidized fuel flows and the presence of three burners 2.1, it is possible to achieve maximum capacities of 1,000 to 1,500 megawatts with reliable and safe operation. Figure 7 shows a gasification reactor 2 with full quenching 3, with the ignition and pilot burner 2.2 and the dust burners 2.1, through which the fluidizing gas or a slurry of fuel and liquid is fed into the reactor, being positioned in the center of the head of the reactor 2. The reactor has a gasification chamber 2.3 with a cooling shield 2.4 whose outlet opening 2.5 leads to the quench-cooler 3, whose quenching chamber 3.1 has quenching nozzles 3.2, 3.3, and a crude gas discharge 3.4, through which the finished crude gas can leave the quench-cooler 3. The slag that leaves the quench-cooler through an outlet opening 3.6 is cooled in the water bath 3.5. Figure 8 shows a gasification reactor 2 with partial quenching, with the gasification reactor located in the upper part, in which dust burners 2.1 gasify the dust from the transport line 1.4, and with an ignition and pilot burner 2.2 positioned in the center. The gasification reactor 2 has a bottom opening into the quenching chamber 3.1, into both sides of which lead quenching nozzles 3.2, with waste heat boilers 4.1 placed below this. S: P59914 2334953_2 (GHMatter) P59114 AU - 21 The function will be described with a first example with reference to material flows and procedural processes: 240 Mg/h of pulverized coal is fed to a gasification reactor with a gross capacity of 1500 MW. This pulverized fuel prepared by drying and grinding crude bituminous coal has a moisture content of 5.8 %, an ash content of 13 wt.%, and a calorific value of 24,700 kJ/kg. The gasification takes place at 1,550 OC, and the amount of oxygen needed is 208,000 m 3 I. H./h. The crude coal is first fed to a state-of-the-art drying and grinding system in which the water content is reduced to 1.8 wt.%. The grain size range of the pulverized fuel produced from the crude coal is between 0 and 200 pm. The ground pulverized fuel (Fig. 1) is then fed to the metering system, the functional principle of which is shown in Fig. 2. The metering system consists of three identical units, as shown in Fig. 3, with each unit supplying 1/3 of the total amount of powder, or 80 Mg/h, each to a dust burner. The three dust burners assigned to them are at the head of the gasification reactor, whose principle is shown in Fig. 4. The usable pulverized fuel according to Fig. 2, which shows one unit of the powder metering system, goes from the operational bunker 1.1 to alternately operated pressurized sluices 1.2. There are 3 pressurized sluices in each unit. S:P59914 2334953_2 (GHMattes) P59114AU - 22 Pressurized suspension to the gasification pressure is performed with an inert gas such as nitrogen, for example, which is fed in through the line 1.6. After suspension, the pressurized pulverized fuel is fed to the metering tank 1.3. The pressurized sluices 1.2 are depressurized through the line 1.7 and can be refilled with pulverized fuel. The 3 mentioned pressurized sluices in each unit are loaded alternately, emptied into the metering tank, and depressurized. This process then begins anew. A dense fluidized bed is produced in the bottom of the metering tank 1.3 by feeding in a dry inert gas through the line 1.5, likewise nitrogen, for example, that serves as the transport gas; 3 dust-transport lines 1.4 are immersed in the fluidized bed. The amount of pulverized fuel flowing in the transport lines 1.4 is measured and regulated in relation to the gasification oxygen. The gasification reactor 2 is shown and further explained in Fig. 3. The transport density is 250-420 kg/M 3 . The gasification reactor 2 is shown and further explained in Fig. 3. The pulverized fuel (Fig. 3) flowing through the transport lines 1.4 to the gasification reactor 2 is discharged into 3 metering systems, each with a capacity of 80 Mg/h. The total of 9 transport lines 1.4 lead in groups of three each to 3 gasification burners 4.1 located at the head of the reactor 2. At the same time, 1/3 of the total amount of oxygen of 208,000 m 3 NTP/h is fed to each gasification burner. The dust burners are S: P59914 2334953_2 (GHNtters) P591 14AU - 23 arranged symmetrically at angles of 1200, and in the center there is an ignition and pilot burner that heats the gasification reactor 2 and serves to ignite the dust burner 4.1. The gasification reaction, or the partial oxidation at temperatures of 1,550 *C, takes place in the gasification chamber 2.3, which is distinguished by a cooled reaction chamber contour 2.4. The monitored and measured amount of pulverized fuel is subjected to ratio regulation with the supplied oxygen, which provides that the ratio of oxygen to fuel neither exceeds nor falls below a range of X = 0.35 to 0.65. The value of X represents the ratio of the needed amount of oxygen for the desired partial oxidation to the amount of oxygen that would be necessary for complete combustion of the fuel used. The amount of crude gas formed is 463,000 m 3 NTP/h and is distinguished by the following analysis:

H

2 19.8 vol.% CO 70.3 vol.%

CO

2 5.8 vol.%

N

2 3.8 vol.%

NH

3 0.03 vol.% HCN 0.003 vol.% COS 0.04 vol.%

H

2 S 0.4 vol.% S: P59914 2334953.2 (GHMatter) P591 14AU - 24 The hot crude gas at 1,550 *C leaves the gasification chamber 2.3 together with the liquid slag through the discharge 2.5 and is cooled to 212 OC in the quenching chamber 3.1 by injecting water through the rows of nozzles 3.2 and 3.3, and is then sent through the outlet 3.4 to the crude gas scrubber 4, which serves as a water scrubber to remove dust. The cooled slag is collected in a water bath 3.5 and is discharged downward. The crude gas washed with water after the water scrubber 4 is sent for partial condensation 5 to remove fines < 20 pm in size and salt mists not separated in the water scrubber 4. For this purpose, the crude gas is cooled by about 5 oC, with the salt particles dissolving in the condensed water droplets. The purified crude gas saturated with steam can then be fed directly to a catalytic crude gas converter or to other treatment stages. According to Example 2, the process of pulverized fuel feed is to occur according to Fig. 5 and Fig. 6, and the actual gasification in the same way as in Example 1. The hot crude gas and the hot liquid slag likewise pass through the discharge 2.5 into a quenching chamber 3.1, in which the crude gas is cooled to temperatures of 700 - 1,100 *C, not with excess water, but only by spraying in a limited amount of water through nozzle rings 3.2, and are then sent to the waste heat boiler 4.1 to S:P59914 2334953_2 (GHMatters) P59114.AU - 25 utilize the sensible heat of the crude gas to produce steam (Fig. 8). The temperature of the partially cooled crude gas is chosen so that the slag particles entrained by it are cooled in such a way as to prevent deposition on the heat exchanger tubes. As in Example 1, the crude gas cooled to about 200 *C is then fed to the water scrubber and partial condensation. In the claims which follow and in the preceding description, except where the context requires otherwise due to express language or necessary implication, the word "comprise" or variations such as "comprises" or "comprising" is used in an inclusive sense, i.e. to specify the presence of the stated features but not to preclude the presence or addition of further features in various disclosed embodiments. S:P59914 2334953_2 (GHIatter) P59114AU - 26 List of reference symbols used 1. Pneumatic metering systems for pulverized fuel 1.1 Bunker 1.2 Pressurized sluice 1.3 Metering tank 1.4 Transport line 1.5 Line for fluidizing gas. 1.6 Line for inert gas into 1.2 1.7 Depressurization line from 1.2 2. Gasification reactor with cooled reaction chamber structure 2.1 Dust burner with oxygen infeed 2.2 Ignition and pilot burner 2.3 Gasification chamber 2.4 Cooling shield 2.5 Discharge opening 3 Quenching cooler 3.1 Quenching chamber 3.2 Quenching nozzles 3.3 Quenching nozzles 3.4 Crude gas outlet 3.5 Water bath with slag S: P59914 2334953_2 (GHMfem) P59114 AU - 27 3.6 Bottom discharge from 3 3.7 Lining 4 Crude gas scrubber 4.1 Waste heat boiler 5 Condensation, partial condensation S :P59914 2334953_2 (GHMatters)PS9114AU

Claims

1. A high capacity reactor for the gasification of pulverized fuels from solid fuels such as bituminous coals, lignite coals and their cokes, petroleum cokes, cokes from peat or biomass, in entrained flow, with an oxidising medium containing free oxygen, at temperatures between 1,200 and 1,900 OC and at pressures between atmospheric pressure and 80 bar, into a crude synthesis gas and slag, the reactor comprising: a reactor head; an ignition and pilot burners disposed at said head of the reactor; a plurality of equal gasification burners disposed at said head of the reactor; a plurality of lock hoppers and dosing systems arranged to supply said pulverized fuels to said plurality of equal gasification burners; individual transport lines assigned to each gasification burner said individual transport lines connecting and feeding said pulverized fuels from said lock hopper and dosing systems to the respective gasification burner; wherein each gasification burner is connected and fed by at least two different lock hoppers and dosing systems; and a measuring system configured to measure and regulate amounts of pulverized fuel and oxygen flowing in each of said S: P59914 2334953_2 (GHMatters) P59114AU - 29 plurality of equal gasification burners, said measuring system controlling the overall total amounts of pulverized fuel and oxygen flowing in the reactor.

2. A high capacity reactor as claimed in claim 1, wherein said plurality of equal gasification burners comprise at least three gasification burners and wherein said plurality of lock hopers and dosing systems, wherein each gasification burner of said plurality of equal gasification burners is connected and fed with pulverized fuel over two burner individual transport lines with each of said three lock hoppers and dosing systems.

3. The high capacity reactor as claimed in claim 1, wherein said plurality of equal gasification burners comprise three gasification burners and said plurality of lock hoppers and dosing systems comprise at least two lock hoppers and dosing systems, wherein each gasification burner is connected and fed with pulverized fuel over two burner individual transport lines with each of said two lock hoppers and dosing system.

4. An apparatus for gasifying combustible dusts comprising hard coal, lignite, petroleum coke, or solid grindable residues, and slurries, comprising: S:P59914 2334953_2 (GHatters) P59114AU - 30 an entrained gasification reactor for gasifying the combustible dusts at temperatures ranging from 1200 to 1900 0 C and pressures of up to 80 bar; wherein said gasification reactor comprises a plurality of gasification burners, each burner having an individual feed port; wherein each gasification burner comprises a plurality of supply ports connected to said feed port; a plurality of lock hopper and dosing systems arranged to supply dust or slurries to the gasification burners; and a plurality of supply lines corresponding in number with said plurality of supply ports leading from each lock hopper and dosing system to said supply ports, and configured to provide dust or slurries to each feed port of each burner.

5. The apparatus as claimed in claim 4, wherein a number of the third plurality of lock hopper and dosing systems is fewer than the number of the first plurality of gasification burners.

6. The apparatus as claimed in claim 5, wherein there are three gasification burners and two lock hopper and dosing systems. S:P59914 2349M_2 (GHattesm) P59114AU - 31

7. The apparatus as claimed in claim 6, wherein each gasification burner is simultaneously supplied from two lock hopper and dosing systems through at least two supply lines, each of these two supply lines being associated with a different lock hopper and dosing system.

8. The apparatus as claimed in claim 4 wherein said plurality of lock hopper and dosing systems are configured to simultaneously supply dust or slurries to feed at least two of said plurality of gasification burners.

9. A method for the gasification of pulverized fuels substantially as herein described with reference to the accompanying drawings and examples. S:P59914 2334953_2 (GHMatters) P59114 AU