MXPA05008871A

MXPA05008871A - Apparatus and method for coal gasification.

Info

Publication number: MXPA05008871A
Application number: MXPA05008871A
Authority: MX
Inventors: Fredrico Van Zyl
Original assignee: Cogas Llc
Priority date: 2004-11-17
Filing date: 2005-08-19
Publication date: 2006-05-19
Also published as: CN1782037A; US20060101715A1; AU2005203534A1; CA2521982A1

Abstract

A process and apparatus for converting a coal into a substitute natural gas generates raw gas in a conventional coal gasification unit and passes at least a portion of the raw gas into a partial oxidation unit to convert the at least portion of the raw gas into a secondary raw synthesis gas substantially devoid of higher hydrocarbons. Optionally, the raw gas is quenched and only the resulting condensate is passed to the partial oxidation unit for conversion to the secondary raw synthesis gas.

Description

APPARATUS AND METHOD FOR THE GASIFICATION OF HULLA BACKGROUND OF THE INVENTION The invention relates to an apparatus and a process for converting hard coal into a synthetic natural gas. More particularly, the invention relates to converting, by non-catalytic partial oxidation, liquid condensates from a primary gasification process to a secondary synthesis gas, resulting in the use of substantially all byproduct streams for gas production additional crude, thereby minimizing the undesirable effluent produced by the gasification process. Coal gasification technology is well known and has been in commercial use, for example, in South Africa for many years. The most common coal fuel used is that developed by Lurgi Kohle und Mineraloeltechnik GmbH. The Lurgi process uses a fixed bed gasogen in which the coal of a selected particle size is fed countercurrent to a stream of steam and oxygen. The coal gasification processes are accompanied by the generation of byproducts essentially comprised of oil, tar and phenolic. The trend of this by-product presents significant environmental and economic problems. Ref. 166058 Therefore, there is appreciated the need in the art for an apparatus and a process that will essentially utilize all by-product streams from a gasification process for the production of additional raw gas to maximize the synthesis gas produced by the process of gasification. SUMMARY OF THE INVENTION Therefore, a process for converting hard coal to synthetic natural gas begins by placing a coal load in a coal gasification device and causing the gasification of at least a portion of the load by exposing the load to a gasifying agent and heat. The primary raw gas is recovered at an outlet of the coal gasification device and at least a portion of the primary raw gas is transferred into the non-catalytic partial oxidation device where a partial oxidation agent and the temperature is maintained to convert the minus one portion of primary crude gas in a crude gas of secondary synthesis substantially devoid of higher hydrocarbons. In another aspect of the invention, a process for converting hard coal to a synthetic natural gas begins by placing a coal load in a coal gasification device and causing the gasification of at least a portion of the load by exposing the load to a gasifying agent and heat in the coal gasification device. The primary raw gas is recovered at an outlet of the coal gasification device and subjected to rapid cooling to separate the condensable hydrocarbon containing liquid therein. The liquid is then subjected to a partial non-catalytic oxidation in the presence of a partial oxidizing agent at a temperature sufficient to convert the liquid into a crude gas of secondary synthesis substantially devoid of hydrocarbons with the exception of carbon monoxide, carbon dioxide and methane . In another aspect of the invention, the apparatus for converting hard coal into a synthetic natural gas includes a plurality of coal gasification devices, each operable to cause gasification of at least a portion of the coal load fed therein and to producing a primary raw gas at an outlet of the gasification device. A rapid cooling system having an input coupled to each of the outputs of the gasification device receives the primary raw gas thereof and is operative to separate the condensable hydrocarbons in liquid form from the primary raw gas, to deliver the liquid to an outlet for liquid from the rapid cooling system and to deliver cooled raw gas as synthetic natural gas to a gas outlet of the cooling system Quick. A partial oxidation device having an inlet coupled to the liquid outlet of the rapid cooling system is operative to subject the received liquid hydrocarbons to partial oxidation at a temperature sufficient to convert the liquid hydrocarbons to a crude gas of secondary synthesis substantially devoid of hydrocarbons in a gas outlet of the partial oxidation device. BRIEF DESCRIPTION OF THE FIGURES The objects and characteristics of the invention will become evident by reading a detailed description, taken together with the figures, in which: Figure 1 is a schematic diagram of a coal gasification system ordered according to the principles of the invention; Figure 2 is a schematic diagram showing a primary gasification device and a partial oxidation device coupled by an optional rapid cooling system; and Figure 3 is a schematic diagram of an illustrative gasification plant using a simple partial oxidation device with four primary coal gasification devices and a multi-stage rapid cooling system, arranged according to the principles of the invention. DETAILED DESCRIPTION OF THE INVENTION As used herein, the term "higher hydrocarbons" refers to hydrocarbons having a composition CnHm, where n and m are integers and n is 2 6 greater. With reference to Figure 1, a basic schematic diagram showing the optional arrangements of the invention is displayed. The primary gasogen 102 directs raw gas at its outlet 110 to any liquor separation and rapid cooling device 106 by path 110A or by path 110B to a non-catalytic partial oxidizing device 104. If path 110B is used, then the Entry to the partial oxidant 104 is basically in gaseous form. If the liquor separation and quick cooling device 106 is used, then the inlet 116 for the partial oxidation device 104 is in liquid form, the condensate being generated by the cooling process occurring in the device 106. It will be evident to those skilled in the art. in the art, that only a portion of the raw gas 110 can be fed via an optional path 110B to the partial oxidant device 104. When the raw gas 110 is subjected to rapid cooling down the path 110A before feeding the partial oxidant 104, the gas generated secondary synthesis resulting in the output 114 would then be directed by the path 114A back to an input of the rapid cooling system 106 for additional cooling. Otherwise, if rapid cooling is not performed prior to partial oxidation, the secondary synthesis raw gas at 114 may be directed to the output of system 112 by path 114B. What differentiates the instant invention from the known gasification processes is the inclusion of a non-catalytic partial oxidation device 104. The device 104 produces additional synthesis crude gas from the tars and oils present in the crude gas stream. in gaseous form or in the inlet 116 in liquid form. Hence, all by-product streams are used for the production of crude oil, minimizing the effluent produced from the process. The partial oxidant 104 converts the higher hydrocarbons to carbon monoxide and hydrogen and a little unnoticed carbon dioxide. This is completed in very high temperatures by using direct contact with a hot flame burner in an atmosphere of substoichiometric oxygen that prevents the vast majority of the carbon monoxide generated from becoming carbon dioxide. The direct feed of crude gas 110 through path 110B makes sense in those applications where methane is not desired in the final product of the final synthetic natural gas. However, by using the liquor separation and rapid cooling system 106, only the derived liquor is transferred to the partial oxidant and not the crude gas leaving to the path 110. In this type of application, methane is normally a desirable component. of the synthetic crude gas at the outlet of the system 112 and will be transferred directly thereto via the system 106 without addressing the partial oxidant 104. With reference to Figure 2, a basic arrangement of the primary gasogen, a non-catalytic partial oxidant and a system Optional quick cooling 212 are described. A coal feed tank 204 is a pressure vessel and allows gas generator 206 to be fed in a mixing operation. The coal feed tank 204 has a closure device in the bottom and on the surface which are hydraulically operable. The coal flows through an evacuation chute 202 in the coal feed tank 204 when the coal feed tank 204 is at atmospheric pressure (with the lower cone enclosed and the upper cone open). After the coal feed tank 204 is full, the upper cone is closed and the coal feed tank 204 is pressurized with a crude gas taken downstream from the gas cooling device. The final pressurization is made by a direct line from the upper section of the gasogen 206 to the coal feed tank 204.

When the coal feed tank 204 is at the pressure of the gasogen, a lower cone opens and the coal begins to flow into the gasogen 206 through a distributor 208, preferably comprised of a cyclonic skirt. When the coal feed tank 204 is empty, the lower cone is closed and ready for recycling. The gasogen 206 is a double-walled pressure vessel. The feed water of the high-pressure boiler is maintained in the cover formed by the double wall to limit the temperatures of the gas-generator wall and the cover. The feed water from the high-pressure boiler circulates through the cover through lowering pipes. During the operation, a considerable amount of heat is transferred from the fuel bed to the cover. The vapor from the cover is added to the high pressure steam and the total steam is mixed with oxygen at a rate of approximately 0.4 pounds of steam per oxygen SCF. This gasifying agent is directed by means of a rotating grid 209 in the fuel bed of the -gasogen. As a consequence, the grid 209 is cooled by the gasifying agent, the grid 209 is driven by alternating current units and serves first to enable the distribution of the gasifying agent in the cross section of the gas generator 206 through the ring grooves of the gasifying agent. The distribution is completed in the combustion waste bed.

Secondarily, the grate 206 conveys the combustion residues to the feed tank of the combustion residues 210, which helps disintegrate the agglomerates of combustion residues and crush the pieces of the combustion residues to a maximum size to avoid obstacles in the combustion. the feeding cones of the combustion residues. Finally, grid 209 keeps the fuel bed in motion. The grid 209 is automatically a speed controlled by the flow of oxygen to adapt the formation of combustion residues to the production of combustion residues. Manual corrections of grid speed are also possible. The drainage capacity of the grid 209 is determined by the number of grilles installed below the grid and by the speed of the grid 209. The grid 209 operates continuously and stops only for short periods when the waste feed tank cycle of combustion 210 starts. The gasifying agent, for example, a mixture of oxygen in line 233 and steam in line 231, is transferred through the following reaction zones in vessel 206. In the waste bed of combustion 206A, the gasifying agent is super-heated through combustion zone 206B that leaves combustion residues at a temperature of approximately 2730 ° F. Under the assumption that a sufficient bed of combustion residues 206A is established, the combustion residue is cooled to a temperature higher than that of the gasifying agent while the gasifying agent is heated at the inlet of vessel 206. In a combustion zone 206B , carbon and oxygen are converted to carbon dioxide and heat. The temperatures of the gas flow are increasing and the combustion residue (which has a carbon content of approximately 2%) decreases, increasing to almost 2700 ° F. The gas running upwardly from the combustion zone 206B consists mainly of carbon dioxide and steam and reacts in the gasification zone 206C at an average temperature of about 1560 ° F. The dominant reaction in the 206C gasification zone is the conversion of carbon and water to carbon monoxide, hydrogen and heat. A methanization reaction has a minor influence on the composition of the gas leaving the 206C gasification zone. In a 206D carbonization zone, the volatiles in the coal are expelled. The carbonization reaction is a consumption of heat. As a consequence, the raw gasification gas flowing upward from the 206C gasification zone must heat the coal that flows downward and must deliver heat for carbonization.

Additionally, in the 206D carbonization zone, the recycled dusty tar is cracked to oil and coke. The combustion waste feed tank 210 is a pressure vessel having lower and upper closures that are operated hydraulically. The combustion waste feed tank 210 serves to remove the combustion residues of the gas engine 206 and is operated in cycles, each having the following steps. The continuous operating grid 209 deflects the combustion residues out of the gasogen 206 by means of an upper cone which acts hydraulically in the combustion waste feed tank 210 with its lower cone closed in the gasogen pressure. As soon as the combustion waste feed tank 210 is full, the grid 209 stops. After the upper cone of the combustion waste feed tank is closed and sealed, the grate 209 is reset. The combustion waste feed tank 210 is then reduced to atmospheric pressure, the lower cone of the combustion waste feed tank 210 is opened and the combustion residue flows out of the combustion waste feed tank 210 in a combustion channel 210. evacuation 253 where it is cooled quickly and is hydraulically taken to a combustion waste plant.

The raw gas generated by the fuel device 206 exits in the conduit 235 and is directed to an optional rapid cooling system 212 whose outlet 237 contains liquid condensates from the rapid cooling process. Alternatively, in a direct feed system the rapid cooling system 212 is not used and the raw gas is fed to a partial oxidizing device 266. In the optional cooling / washing apparatus 212, the excess water, certain condensable hydrocarbons and a small amount of solids are separated from the crude gas stream in conduit 235. The liquid stream in conduit 237 serves as raw material for partial oxidation device 216. In the non-catalytic partial oxidation device 216 the raw material reacts with oxygen in the presence of steam as a moderator for the crude synthesis gas. The hot raw gas is cooled by direct injection of water into the quench tube 218 and into the quench flask 220. A quench vessel 222 carries the combustion residues to its outlet 249. The partial non-catalytic oxidation device 216 partially oxidizes the heavy fragments at a temperature of about 2500 ° F. and at a pressure close to 435 psig. Oxygen in conduit 239 and vapor in conduit 241 are added to incoming raw material in conduit 237 by a partial oxidation burner device 214. Burner 214 ensures intensive mixing of the feed, which is necessary for a conversion higher in the desired synthesis crude gas. In an injection zone of the reactor 216, the feed is partly oxidized in the flame of the burner 214. The raw reactions in the device 216 essentially convert higher hydrocarbons to carbon monoxide and hydrogen in two phases. In a first heating and cracking phase, the feed and oxygen leave the burner 214 at the respective preheating temperatures. Before the current combustion, the reactants are further heated by the reflected heat of the flame and the burning brickwork of the vessel 216. The higher hydrocarbons in the feed cradle the radicals. Then, in a reaction phase, at an igniting temperature that reaches, -a portion of the hydrocarbons reacts with the oxygen in an exothermic reaction that forms carbon dioxide and water. Practically, all available oxygen is consumed in this phase. The non-oxidized portion of the hydrocarbons reacts with steam and the products of the reaction are mainly carbon monoxide and hydrogen. As mentioned earlier, the raw material, oxygen and vapor enter the reactor 216 by the burner 214, which is mounted in an upper portion of the reactor 216. The burner 214 preferably has a four-nozzle design with a central simulated tube that lifts to the burner start. At startup, the central tube supports the ignition and start burner, which is equipped with a sensor for flame control. In order to heat the reactor 216, the air plant and the heating gas are fed by the start burner into the duct 243. At higher temperatures, when the higher heat supply is required, the air and the heating gas are also powered by four burner spears. At a good reactor temperature above the auto-ignition temperature of the heating gas, usually close to 1470 ° F, the ignition burner is removed and replaced by a simulated steam purge. During the final heating to approximately 2200 ° F, the heating gas and air are fed through the four burner nozzles. To maximize the volumetric capacity of the partial oxidation reactor 216, the fine coal may optionally be added to the liquid raw material by the lance burner 214. The burner 214 is cooled with water and by means passing through it. The reactor outlet for the quench tube 218 is also cooled to minimize refractory wear at this point.

The conversion of hydrocarbons by partial oxidation occurs in the lined refractory reactor 216. The refractory material is selected according to the load of combustion residues and to the properties of the combustion residues of the raw material. The combustion residue must be melted at the operating reactor temperature to ensure the free flow of molten combustion residues from the reactor 216 to the quick-cooling vessel 220 and to prevent blocking of the reactor 216 and the quench tube 218. The raw gas Secondary synthesis hot water from the reactor 216 is directed by the rapid cooling tube 218 to the rapid cooling vessel 220. The secondary synthesis gas is instantaneously cooled from a temperature close to 2470 ° F to an equilibrium temperature of approximately 430 ° F by injection water. The liquid slag that flows with the gas solidifies into particles. The particles could be leached in any acidic or alkaline medium. The gas is separated from the excess quench water and the slag particles below the quench tube 218 and the quench flask 220. The gas is removed by a separate nozzle and the collected slag water is directed by control level to a slag separator 222. The slag is separated from the soot water leaving the rapid cooling vessel through the duct 251 in a slag-like system having the slag separation vessel 222. The heavy particles of the slag they are set from the soot water in the slag separation vessel 222 and collected in a lower cone to be discharged via the conduit 249. The collected soot and the combustion residues can be mixed in a soot pulp and sent to a metal combustion waste recovery system where the soot pulp is ignited at atmospheric pressure in a pulp tank. The pulp is filtered which results in a cake of filtering mass and clean water usable for the fast cooling and washing operation. Figure 3 presents a schematic diagram of a gasification plant using a simple non-catalytic partial oxidation device with four primary coal gasification devices. This type of arrangement takes advantage of the fact that only the products of the pyrolysis of the raw gas generated from the primary gasification devices are partially oxidized. Hence, one only needs the capacity of a simple partial oxidation device for several primary de-gasification fixed-bed devices (more than five).

As seen in Figure 3, the sources of coal to be gassed 301a-d are respectively fed to an evacuation chute 350 of each of the four fixed-bed gasogen devices 302a-302d. From the entrance of the trough 350 the coal is transferred to the inlet of the feed tank 352 which is coupled to the processing vessel. Near the surface at the entrance to the processing vessel a cyclonic skirt 354 helps to distribute the coal load flowing down through the countercurrent of the vessel to the flow of the gasification agent supplied to the respective inlets of the containers 302a-d from the oxygen source 305 and from the steam source 307. A rotating grid 356 distributes the gasifying agent and processes the combustion residues within the systems as described above with respect to Figure 2. The raw gas from the process is collected in the outlets 303a-d which are coupled together in conduit 313 as a gaseous outlet for rapid cooling system 306. As mentioned above, the gasifying agent is a mixture of oxygen and vapor. The rapid cooling system 306 is comprised of a serial connection of five heat exchange devices 308, 310, 312, 314 and 316. The initial stages 308 and 310 receive an inlet for relatively high temperature gas and generate high pressure steam from the heat exchange process. The condensates 308 and 310 remove the devices at the liquid outlets 309a and 309b and are comprised primarily of thick tars and combustion residues. The subsequent steps of the rapid cooling system 306 result in the generation of medium pressure steam and in the condensation of light oils. As seen in Figure 3, the gas outlet of each of the stages is connected to the gas inlet of a subsequent upper stage until the final stage 316 whose outlet 311 forms the outlet of the primary system that transports the crude natural gas Synthetic cooled. Hence, the gaseous outlet 317 is coupled to an inlet of the heat exchanger .310 whose gaseous output 319 is in turn coupled to the inlet of the heat exchanger 312. The gaseous output 321 of the device 312 is connected to the input of the device. 313 and the output 323 of the device 314 is coupled to an input of the final stage of the heat exchanger device 316. The outlets for the liquid 309a-e are coupled together to a primary liquid outlet of the rapid cooling system 309. The Liquid hydrocarbons in the conduit 309 are coupled to an input of the non-catalytic partial oxidation device 304. The oxygen source 305 and the steam source 307 are further coupled to the input of the device 304 and the secondary synthesis raw gas comprised primarily of hydrogen and carbon monoxide leaves the device 304 through line 315 and is directed back to an inlet 313 of the system 306 rapid cooling for additional cooling. The outlet of the plant 311, therefore, contains crude synthetic natural gas cooled rapidly to about 392 ° F which is essentially free of the pyrolysis products generated in the primary gasogens 302a-d.

EXAMPLE Unreactive coal (ie coal containing more than about 30% non-combustible contaminants) having a combustion residue content greater than about 50 weight /% is fed to a primary gasogen accommodated as shown in Figures 2 or 3 and a primary raw gas is produced at the primary gas source outlet that has a volume percentage composition of 28.2% carbon dioxide, 0.05% hydrogen sulfide, 0.69% higher hydrocarbons, 22.66% monoxide of carbon, 38.51% of hydrogen, 9.5% of methane and 0.39% of nitrogen. The raw gas as previously produced is directed to a rapid cooling system where the pyrolysis products and other liquids are condensed out of the gas stream and transferred to the input of the non-catalytic partial oxidation device that is run at a reaction temperature of about 2578 ° F. The crude gas of the gasogen is then reformed in the partial oxidation device, cracked and idolyzed, and the process established under the gasification reaction conditions results in the following typical gas components at the output of the partial oxidation device expressed by the percentage of volume: 1.9% carbon dioxide, 0.08% hydrogen sulfide, 52% carbon monoxide, 45.1% hydrogen, 0.3% methane and 0.62% nitrogen. The request has been described with respect to a specific modality as an example-only reason. The scope and spirit of the invention are to be determined - of the appropriately interpreted claims. It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Claims

CLAIMS Having described the invention as above, the content of the following claims is claimed as property:

1. A process for converting hard coal into a synthetic natural gas characterized in that it comprises: placing a coal load in the coal gasification device; causing the gasification of at least a portion of the charge by exposing the charge to a gasifying agent and to heat in the coal gasification device; recover primary raw gas at an outlet of the coal gasification device; and passing at least a portion of the primary crude gas in the non-catalytic partial oxidation device, adding a partial oxidation agent, and maintaining an effective temperature to convert the at least a portion of the primary raw gas into a secondary synthesis crude gas substantially devoid of superior hydrocarbons.

2. The process according to claim 1, characterized in that it also comprises the addition of the crude gas of secondary synthesis to the primary raw gas.

3. The process according to claim 1, characterized in that the at least a portion of the primary raw gas is subjected to rapid cooling to separate the condensable hydrocarbons therefrom by transmission to a non-catalytic partial oxidation device to convert the hydrocarbons condensables to a crude gas of secondary synthesis substantially devoid of superior hydrocarbons.

4. The process according to claim 1, characterized in that the partial oxidation agent comprises a gas mixture containing oxygen and steam. The process according to claim 1, characterized in that substantially all of the higher hydrocarbons present in the at least a portion of the primary raw gas are cracked and hydrolyzed in the non-catalytic partial oxidation device. 6. The process according to claim 3, characterized in that all the higher hydrocarbons present in the condensable liquids separated from the primary raw gas are cracked and hydrolyzed in the non-catalytic partial oxidation device. 7. The process according to claim 1, characterized in that substantially all of the primary raw gas is transferred to the non-catalytic partial oxidation device. The process according to claim 3, characterized in that substantially all of the raw primary gas is subjected to rapid cooling prior to the transmission of the separated condensable hydrocarbons to the non-catalytic partial oxidation device. 9. A process for converting hard coal into a synthetic natural gas characterized in that it comprises: placing a coal load in the coal gasification device; causing the gasification of at least a portion of the charge by exposing the charge to a gasifying agent and to heat in the coal gasification device; recover primary raw gas at an outlet of the coal gasification device; subjecting the primary raw gas to rapid cooling to separate condensable hydrocarbons containing liquid therefrom; and subjecting the liquid to partial non-catalytic oxidation in the presence of a partial oxidizing agent at a temperature sufficient to convert the liquid into a crude secondary synthesis gas substantially devoid of hydrocarbons with the exception of carbon monoxide, carbon dioxide and methane. 10. The process according to claim 9, characterized in that it also comprises the addition of the secondary synthesis crude gas to the primary raw gas. 11. The process according to claim 9, characterized in that - the partial oxidizing agent comprises oxygen and steam. 12. The process according to claim 9, characterized in that the temperature at which the liquid is subjected is sufficient to crack and hydrolyze substantially all of the higher hydrocarbons present in the liquid. 13. The process according to claim 12, characterized in that the liquid is subjected to partial oxidation at a temperature from about 2372 ° F to 2732 ° F. The process according to claim 12, characterized in that the liquid is subjected to partial oxidation at a temperature of about 2578 ° F and a pressure of about 400 psig. 1

5. The process according to claim 9, characterized in that the load is comprised of hard coal having at least about 30% by weight of non-combustible contaminants. The process according to claim 15, characterized in that the primary raw gas comprises about 28% by volume of carbon dioxide less than about 1% by volume of hydrocarbons, about 23% by volume of carbon monoxide, about 38.5% by volume of hydrogen, and approximately 9.5% by volume of methane. The process according to claim 16, characterized in that the secondary synthesis crude gas comprises less than about 2% by volume of carbon dioxide, greater than about 50% by volume of carbon monoxide and greater than about 45% by volume. volume of hydrogen. 18. The process according to claim 9, characterized in that the load is comprised of hard coal having combustion residues and non-combustible contaminants greater than about 50% by weight. 19. The process according to claim 9, characterized in that the load is comprised of hard coal having an oxygen content of more than about 3% by weight. 20. The apparatus for converting coal to synthetic natural gas characterized in that it comprises: a plurality of coal gasification devices, each operable to cause the gasification of at least a portion of a coal charge fed therein and to produce a primary raw gas in an outlet of the gasification device; a rapid cooling system having an inlet coupled to each of the outputs of the gasification device for the reception of primary and operating raw gas to separate the condensable hydrocarbons in liquid form from the primary raw gas, to deliver the liquid to an outlet for liquid from the rapid cooling system and to deliver cooled raw gas as synthetic natural gas to a gas outlet of the rapid cooling system; and a partial oxidation device having an inlet coupled to the liquid outlet of the rapid and operational cooling system for subjecting the received liquid hydrocarbons to partial oxidation and at a temperature sufficient to convert the liquid hydrocarbons to a substantially synthesis secondary crude gas. devoid of higher hydrocarbons in a gas outlet of the partial oxidation device. The apparatus according to claim 20, characterized in that the gas outlet of the partial oxidation device is coupled to the inlet of the rapid cooling system. 22. The apparatus according to claim 20, characterized in that each of the gasification devices comprises a fixed bed gasogen having a feed tank inlet having an inlet engaged for the reception of a coal load and an outlet; a pressure vessel having a coal inlet coupled for receiving the coal from the outlet of the inlet feed tank, a cyclonic skirt for distributing the coal in the vessel fitted to the coal inlet, and a rotating grid placed in a combustion zone of the vessel for combustion in a portion of the coal and for distributing the combustion residues towards an outlet for solid matters from the container, and an inlet for gasification for the reception of a gasifying agent coupled to the rotary grid; and a combustion waste feed tank having an inlet coupled to the outlet for solid matter from the container. The apparatus according to claim 20, characterized in that the rapid cooling system further comprises: a plurality of interconnected heat exchanging devices consecutively, each having an inlet to receive an inlet gas, a condensed outlet to present condensed liquid from the inlet gas, and an outlet for gas having chilled gas by the heat exchanger device, where the outlets for the condensate of the plurality of heat exchanger devices are coupled together to form the outlet for the liquid of the cooling system. rapid cooling, and the gas outlet of each heat exchanger device that is coupled to the inlet to receive gas from a subsequent heat exchanger device, except for the last heat exchanger device in the serial connection, whose gas outlet comprises an outlet for gas in the cooling system r I ask.