Abstract:
A method and device for the gasification of solid fuels such as bituminous coal, lignite coal, and petroleum coke in the flue stream, with an oxidizing medium containing free oxygen by partial oxidation at pressures between atmospheric pressure and 80 bar, and at temperatures between 1200 and 1900° C., consisting of the process steps of pneumatic metering for pulverized fuel, gasification in a flue stream reactor with cooled reaction chamber contour, partial quenching, cooling, crude gas scrubbing, and partial condensation.

Description:
BACKGROUND OF THE INVENTION 
     1. Field of the Invention 
     This invention relates to a gasification method consisting of the process steps of fuel infeed, gasification reaction, partial quenching, waste heat recovery, gas scrubbing, and partial condensation, to produce gases containing CO and H 2  by partial oxidation of pulverized fuels containing ash with a gasification medium containing free oxygen, at high temperatures and elevated pressure. 
     To achieve long operating times, the pressurized jacket of the gasification reactor has to be protected reliably against the action of crude gas and against the high gasification temperatures of 1200-1900° C. This is done by confining the reaction or gasification chamber with a cooled tubular shield that is hung in the pressurized jacket. The annular gap between tubular shield and pressurized jacket is flushed. 
     The fuel is fed to the head of the reactor through burners, using a pneumatic system following the flow transport principle. One or more fuels or varieties of coal can be gasified at the same time. The crude gas leaves the gasification chamber together with the liquefied slag at the bottom of the reactor and is then partially cooled to 700° C. to 1100° C. by injecting water, and is freed of entrained fine after recovering the waste heat. The scrubbed crude gas is then fed to further treatment steps. 
     2. The Prior Art 
     The autothermic entrained flow gasification of solid, liquid, and gaseous fuels has been known in the technology of gas production for years. 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 für 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 A1. Either systems with refractory linings or cooled systems are used for the internal confinement of the reaction chamber structure of the gasification system; see German Patent No. DE 4446 803 A1. 
     European Patent No. EP 0677 567 B1 and PCT International Publication NO. 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. Feeding in the fuel as a coal-water slurry causes considerable losses of efficiency; 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. 
     German Patent No. DE 3534015 A1 shows a method in which the gasification media, powdered coal and oxidizing medium containing oxygen, are introduced into the reaction chamber through multiple burners in such a way that the flames are mutually deflected. 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 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; in particular, 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. 
     Chinese Patent No. 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. 
     SUMMARY OF THE INVENTION 
     It is therefore an object of the invention, to provide a process that takes into account the different ash contents of fuels and has high availability, with reliable operation. 
     The method according to the invention provides for gasification of solid fuels containing ash with an oxidizing medium containing oxygen, in a gasification chamber designed as an entrained flow reactor, at pressures between atmospheric pressure and 80 bar, in which the reaction chamber contour is confined by a cooling system, with the pressure in the cooling system always being kept higher than the pressure in the reaction chamber. 
     In the method, the fuel, e.g. bituminous coal or lignite coke, or mixtures of different coals, is dried and pulverized to a grain size of &lt;200 μm, and is fed through an operational bunker to a pressurized sluice, in which the pulverized fuel is brought to the desired gasification pressure by feeding in a non-condensing gas such as N 2  or CO 2 . Different fuels can be used at the same time. By using more than one of these pressurized sluices, they can be filled and pressurized alternately. The pressurized powder is then sent to a metering tank, in the bottom of which a very dense fluidized bed is produced by likewise feeding in a non-condensing gas; one or more transport pipes are immersed in the bed and open into the burner of the gasification reactor. One or more burners can be used. The fluidized powder flows through these lines from the metering tank to the burners by applying a pressure differential. The amount of flowing pulverized fuel is measured, regulated, and monitored by measurement devices and monitors. There is also the capability of mixing the pulverized fuel with water or oil and feeding it to the burner of the gasification reactor as a slurry. An oxidizing medium containing free oxygen is fed to the burner at the same time, and the pulverized fuel is converted to a crude synthesis gas by partial oxidation. The gasification takes place at temperatures between 1,200 and 1,900° C. at pressures up to 80 bar. The reactor is equipped with a cooling shield that consists of water-cooled tubes welded gas-tight. 
     The hot crude gas leaves the gasification reactor together with the liquid slag formed from the fuel ash, and arrives at a chamber perpendicularly under it, in which partial quenching occurs by injecting water or by feeding in a cold gas and cooling to temperatures between 700° C. and 1,100° C. At this temperature, the entrained liquid slag has been cooled to the extent that it can no longer adhere to surfaces. The crude gas cooled to temperatures of 700° C. and 1,100° C. then arrives at a waste heat boiler together with the likewise cooled solid slag, to utilize the heat for steam production. This partial quenching or partial cooling prevents or sharply reduces the risk of slag caking on the waste heat cooling pipes. The water or recycled gas condensate needed for the partial quenching is fed in through nozzles that are located directly on the jacket. The cooled slag is collected in a water bath located at the bottom of the waste heat boiler. The crude gas, cooled to 200-300° C., leaves the waste heat boiler at the side and reaches a crude gas scrubber, preferably a Venturi scrubber. 
     The entrained dust is thereby removed down to a grain size of about 20 μm. This degree of purity is still inadequate for carrying out subsequent catalytic processes, for example crude gas conversion. It also has to be considered that salt mists are also 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 fine dust &lt;20 μm and the salt mists, the scrubbed crude gas is fed to a condensation step in which the crude gas is chilled indirectly by 5° C. to 10° C. Water is thereby condensed from the crude gas saturated with steam, which takes up the described fine dust and salt particles. The condensed water containing the dust and salt particles is separated in a following separator. The crude gas purified in this way can then be fed directly, for example, to a desulfurization system. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       Other objects and features of the present invention 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 invention. 
       In the drawings, wherein similar reference characters denote similar elements throughout the several views: 
         FIG. 1  shows a block diagram of the technology according to the invention; 
         FIG. 2  shows a metering system for fluidized fuel; 
         FIG. 3  shows a gasification reactor with partial quenching and perpendicularly arranged waste heat boiler; and 
         FIG. 4  shows a gasification reactor with partial quenching and adjacent waste heat boiler. 
     
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT 
     320 tons/hour of bituminous coal with a composition of 
                                                     C   71.5   wt. %           H   4.2   wt. %           O   9.1   wt. %           N   0.7   wt. %           S   1.5   wt. %           Cl   0.03   wt. %,                        
an ash content of 11.5 wt. %, and a moisture content of 7.8 wt. %, is to be gasified at a pressure of 40 bar. The calorific value of the coal is 25,600 kJ/kg. The gasification takes place at 1,450° C. 215,000 m 3  I.H./h of oxygen is needed for the gasification. The coal is first fed to a state-of-the-art drier and grinder in which its water content is reduced to &lt;2 wt. %. The grain size range of the pulverized fuel prepared from the coal present after the grinding is between 0 and 200 μm, and the amount of dried and ground pulverized fuel is 300 tons/hour. The ground pulverized fuel according to  FIG. 1  is then fed to the metering system that is described in  FIG. 2 . The pulverized fuel then is sent through the transport line  1 . 5  to the supply bunker  1 . 1  and is supplied alternately to the pressurized sluices  1 . 2 . Suspension is carried out with an inert gas such as nitrogen, for example, that is fed in through the line  1 . 6 . After suspension, the pressurized pulverized fuel is fed to the metering tank  1 . 3 . The pressurized sluice  1 . 2  is depressurized through the line  1 . 7  and can again be filled with pulverized fuel. There are three pressurized sluices in place, which are filled and depressurized alternately. For the gasification of 300 tons/hour of pulverized fuel, there are three gasification reactors according to  FIG. 3 , each with a metering system. A dense fluidized bed is produced in the bottom of the metering tank  1 . 3  by feeding in 40,000 m 3  i.H./h of a dry inert gas serving as transport gas, likewise nitrogen, for example, through the line  1 . 8 ; one or more dust transport lines  1 . 4  are immersed in the fluidized fuel bed. In this example, three transport lines  1 . 4  are provided in each case. The amount of pulverized fuel flowing in the transport line  1 . 4  is monitored, measured, and regulated in the system  1 . 9 , and is fed to the burner of the gasification reactor  2  according to  FIG. 1 . The loaded density is 250-420 kg/m 3 . The gasification reactor is explained in further detail in  FIG. 3 . The 300 t/h of pulverized fuel flowing into the gasification reactor through the transport lines  1 . 4  is subjected to partial oxidation at 1,450° C. together with the 215,000 m 3  i.H./h of oxygen flowing into the gasification chamber  2 . 3  through the line  2 . 1 , whereby 596,000 m 3  i.H./h of crude gas is formed, with the following composition:
 
     
       
         
               
               
               
               
             
           
               
                   
                   
               
             
             
               
                   
                 H 2   
                 20.8 
                 vol. % 
               
               
                   
                 CO 
                 71.0 
                 vol. % 
               
               
                   
                 CO 2   
                 5.6 
                 vol. % 
               
               
                   
                 N 2   
                 2.3 
                 vol. % 
               
               
                   
                 NH 3   
                 0.003 
                 vol. % 
               
               
                   
                 HCN 
                 0.002 
                 vol. % 
               
               
                   
                 H 2 S 
                 0.5 
                 vol. % 
               
               
                   
                 COS 
                 0.07 
                 vol. %. 
               
               
                   
                   
               
             
          
         
       
     
     Gasification chamber  2 . 3  is confined by a cooling shield  2 . 4  that consists of a water-cooled tube system welded gas-tight. The crude gas together with the liquid slag flows through outlet opening  2 . 5  into chamber  3 . 1  for partial quenching/partial cooling of the crude gas to temperatures of 700° C.-1,100° C. At this temperature, along with the crude gas, the slag is also cooled to such an extent that it cannot be deposited in tubes  4 . 1  of the waste heat boiler that follows according to  FIG. 1 . The steam generated in waste heat boiler  4  is utilized in the process to preheat the oxidizing medium containing oxygen or as a gasification moderator, or otherwise. The slag is collected in a water bath  4 . 2  located at the bottom of the waste heat boiler and is discharged through  4 . 3 . The crude gas leaves the waste heat boiler through  4 . 4  and arrives at the crude gas scrubber  5  according to  FIG. 1 . Waste heat boiler  4 , however, can be located according to  FIG. 3  directly beneath gasification reactor  2  and partial quencher  3 , but also, as shown in  FIG. 4 , beside it. In this case, there is a slag discharge  4 . 3  beneath partial quencher  3  and also one below waste heat boiler  4 . 6 . The crude gas leaving waste heat boiler  4  through outlet  4 . 4  then arrives at crude gas scrubber  5  according to  FIG. 1 , which is an adjustable Venturi scrubber to which is fed about 100 m 3 /h of wash water. The wash water is freed of absorbed solids in the usual way and is fed again to the Venturi scrubber. The wash water can be preheated in order to wet the crude gas further at the same time as the washing. To remove fine dust &lt;20° m in size and salt mists not separated in the Venturi scrubber, the water-washed crude gas is subjected to partial condensation  6  according to  FIG. 1 , with the crude gas being chilled indirectly from 220° C. to 210° C. The finest dust and salt particles are taken up by the steam condensing during the chilling and are thus removed from the crude gas. The crude gas cleansed of solids then has the following composition: 
     
       
         
               
               
               
               
             
           
               
                   
                   
               
             
             
               
                   
                 H 2   
                 9.5 
                 vol. % 
               
               
                   
                 CO 
                 31.2 
                 vol. % 
               
               
                   
                 CO 2   
                 2.6 
                 vol. % 
               
               
                   
                 N 2   
                 1.1 
                 vol. % 
               
               
                   
                 NH 3   
                 0.001 
                 vol. % 
               
               
                   
                 HCN 
                 0.001 
                 vol. % 
               
               
                   
                 H 2 S 
                 0.200 
                 vol. % 
               
               
                   
                 COS 
                 0.03 
                 vol. % 
               
               
                   
                 H 2 O 
                 54.60 
                 vol. % 
               
               
                   
                   
               
             
          
         
       
     
     The purified, wet crude gas amounts to 1,320,000 m 3  NTP/hour. It can be directly sent to a crude gas converter or to other treatment steps. 
     Accordingly, while only a few embodiments of the present invention have been shown and described, it is obvious that many changes and modifications may be made thereunto without departing from the spirit and scope of the invention. 
     LIST OF REFERENCE SYMBOLS USED 
     
         
           1  Pneumatic metering system for pulverized fuel 
           1 . 1  Bunker 
           1 . 2  Pressurized sluice 
           1 . 3  Metering tank 
           1 . 4  Transport line 
           1 . 5  Transport line for pulverized fuel 
           1 . 6  Line of inert gas into  1 . 2   
           1 . 7  Depressurization line 
           1 . 8  Line for inert gas into  1 . 3   
           1 . 9  Monitoring system 
           2  Reactor 
           2 . 1  Line for oxygen 
           2 . 2  Burner 
           2 . 3  Gasification chamber 
           2 . 4  Cooling shield 
           2 . 5  Outlet opening 
           3  Quenching cooler 
           3 . 1  Quenching chamber 
           3 . 2  Nozzle in  3   
           3 . 3  Outlet from  3 . 1   
           4  Waste heat boiler 
           4 . 1  Cooling pipe 
           4 . 2  Slag 
           4 . 3  Outlet from  3   
           4 . 4  Opening from  4  to the crude gas scrubber  5   
           4 . 5  Slag in  4   
           4 . 6  Slag opening in  4   
           5  Crude gas scrubber 
           6  Condenser, partial condensation