INNOVATIVE INCINERATION SYSTEM FOR REFUSE-DERIVED FUELS, COAL AND PETROLEUM COKE, OR CHLORINATED HYDROCARBONS

Abstract: Incineration systems, particularly those using municipal garbage and waste, refuse-derived fuels, coal and petroleum coke, and/or chlorinated hydrocarbons without the release of toxic pollutants such as dioxins. One preferred embodiment relates to a non-polluting method for burning fuel derived from typical municipal garbage and waste, thus eliminating, or at least significantly reducing, the need for the landfill disposal of such waste materials. In an alternative application, air, water, coal and/or petroleum coke are used to produce electricity, urea, and methanol in a non-polluting manner.

Description: Innovative Incineration System for Refuse-Derived Fuels, Coal and Petroleum Coke, or Chlorinated Hydrocarbons FIELD OF THE INVENTION The present invention relates to incineration systems, particularly those using municipal garbage and waste, refuse-derived fuels, coal and petroleum coke, and/or chlorinated hydrocarbons without the release of toxic pollutants such as dioxins. One preferred embodiment relates to a non-polluting method for burning fuel derived from typical municipal garbage and waste, thus eliminating, or at least significantly reducing, the need for the landfill disposal of such waste materials. In an alternative application, air, water, coal and/or petroleum coke are used to produce electricity, urea, and methanol in a non-polluting manner. BACKGROUND OF THE INVENTION Coping with garbage generated by modern living is a serious global problem. In the United States, municipal garbage is disposed of mainly into landfills that uses up valuable land at a disturbing rate. The property value of land used in this manner depreciates tremendously, and the land becomes practically useless. Furthermore, landfills are often criticized as being a health and environmental menace to citizens who live near them. Much of the garbage taken to landfills is combustible and can be used to produce refuse- derived fuel (RDF). However, if certain types of materials, such as chlorinated plastics, normally present in municipal waste, are not removed from, then toxic materials, such as dioxins, will be formed and released to the environment if the RDF is burned in conventional waste-incinerating systems. This is a major reason for sending municipal waste to a landfill rather than converting it to RDF to serve as fuel for producing electricity. A practical and affordable method that will permit clean, non-polluting combustion of fuel derived from typical municipal waste is desperately needed. A significant portion of the world's electricity is produced by burning coal. Also, large amounts of petroleum coke are burned to produce electricity. In North America, coal reserves are abundant and in North, Central and South America, the production of petroleum coke continues to grow. Yet the U. S. continues to increase its crude oil imports. Presently, greater than fifty (50%) percent of the U. S.'s oil consumption is imported, and much of that is used as fuel oil. The technologies in use today to produce electricity, fuel and petrochemicals from coal and petroleum create serious environmental problems. The burning of coal releases more of the greenhouse gas, carbon dioxide (CO 2 ), into the atmosphere per unit of electricity produced than any other method for producing electricity. Burning coal to produce electricity also releases vast amounts of nitrogen oxides (NO x ) into the atmosphere. New, affordable technology that will permit the burning of coal without releasing so much C0 2 and NO x into the atmosphere is desperately needed. Applicant's co-pending U. S. patent application No. 09/193,000, filed November 1 1, 1998, and incorporated herein by reference, teaches new and novel techniques for the high temperature oxidation of chlorinated hydrocarbon waste materials, with essentially zero release of CO 2 and zero release of NO x and other pollutants such as dioxins. Some of these new and novel techniques can be incorporated, for example, into the design of processing units that will permit the burning of fuel derived from typical municipal wastes, or the burning of coal and petroleum coke, without releasing NO x , or other pollutants, such as dioxins into the atmosphere. Summary of the Invention As noted above, the present invention relates to incineration systems, particularly those using municipal waste, refuse-derived fuels, coal and petroleum coke, and/or chlorinated hydrocarbons, and, more particularly, in one application, to a non-polluting method for burning fuel derived from typical municipal garbage and waste, thus eliminating or at least significantly reducing the need for the landfill disposal of such waste materials. In an alternative application, air, water, coal and petroleum coke are used to produce electricity, urea, and methanol in a non- polluting manner. In a final, exemplary embodiment a valorization of chlorinated residuals process (VCR) system is used. The present invention is directed to achieving substantially zero emission of such pollutants as dioxins, and, in the most preferred embodiments of the invention, also zero emission of NO x , and greatly reduced emission of the greenhouse gas C0 2 An important aspect of the inventions, in which at least one and preferably two, sorbent clean-up beds are used, is the routing of the hot reactivation gases exiting at least one of the sorbent beds back into the combustor or reactor, which is operating at a high temperature (e. g. about 1,000°C to about 1,500°C), where the toxic pollutants stripped from the sorbent beds during reactivation are destructed or decomposed, thus preventing such toxic chemicals from escaping to the atmosphere. The schemes, or approaches, of the below described, exemplary embodiments offer, inter alia, one or more of the following benefits: 1. A practical way to incinerate municipal garbage and other such waste materials without releasing to the atmosphere NO x dioxins and other such pollutants, thus in essence eliminating, or at least significantly reducing, the future need for landfill disposal of such waste materials. 2. A practical way to modify coal-burning electric power generating plants so that such plants can operate with substantially zero NO x emission. 3. A practical way to use coal and/or petroleum coke for efficiently producing electricity, urea and methanol with substantially zero emission of NO x , substantially zero emission of such pollutants as dioxins and greatly reduced emission of the greenhouse gas CO 2 . By using more of America's abundant coal reserves in the non-polluting methods of the present invention, the U. S.'s dependence on imported crude oil can be greatly reduced, while at the same time creating many, and much needed, new jobs in the mining and use of coal, as well as in farming and down-stream farming businesses. 4. A practical low cost way is to modify and/or build new incinerators and valorization of chlorinated residuals process (VCR) systems that are used to destruct chlorinated hydrocarbon materials, such that there will be zero discharge of toxic chemicals such as dioxins to the atmosphere. Additionally, as will become clear from the following detailed description, other highly innovative, unobvious advances and improvements are also disclosed as part of the present invention. BRIEF DESCRIPTION OF THE FIGURES For a further understanding of the nature and objects of the present invention, reference is made to the following detailed description, taken in conjunction with the accompanying drawings, in which like elements are given the same or analogous reference numbers, and wherein: Figure 1 is a schematic, generalized, flow chart view depicting a process scheme for incinerating combustible materials that generate pollutants. Particularly dioxins. The processes results in substantially zero release of NO x and such pollutants as dioxins. The embodiment of this figure shows the blending of oxygen (O 2 ) with carbon dioxide (C0 2 ) produced during the incineration of the combustible material. Figure 2 is a schematic, generalized, flow chart view presenting, as a second, exemplary, preferred embodiment, a practical, low cost method for accomplishing the objective of avoiding the release of such things as dioxins to the atmosphere, while not choosing to curb the release of NO x and C0 2 , in which scheme, air is employed as the source of the 0 2 required for the combustion of polluting combustion materials. Figure 3 is a schematic, generalized, flow chart view representing a scheme whereby air, water, coal and petroleum coke are used to produce electricity, urea and methanol in a non- polluting manner. . Figure 4 is a schematic, generalized, flow chart view illustrating another embodiment of the present invention, wherein, if one chooses to continue releasing C0 2 and NO x into the atmosphere, while destructing chlorinated hydrocarbon waste through high-temperature oxidation, then the embodiment offers a practical, low-cost way for doing so with substantially zero release of dioxins and other such toxic pollutants to the atmosphere. In this embodiment, air is the source of the oxygen required to carry out the oxidation of chlorinated hydrocarbon waste materials, either in conventional chlorinated waste incinerators or in VCR systems. DETAILED DESCRIPTION OF THE INVENTION The Figures hereof present a unique arrangement of various process units, such as combustors, steam and gas turbines, sorption beds, and scrubbers and strippers. These process units represent conventional units known in the art, thus a detailed description of each unit is not necessary. Figure 1 depicts a process scheme for burning combustible material, preferably those selected from the group consisting of municipal solid waste, refuse derived fuel, coal, and petroleum coke. The processes of the present invention are conducted in the substantial absence of pollutants, particularly NO x and dioxins. The process of this figure involves the blending of oxygen (0 2 ) via line 10 with carbon dioxide (CO 2 ) via line 12 produced in the combustion of the polluting combustible material with or without an additional solid fuel, such as coal and petroleum coke. The oxygen can be obtained from an upstream air separation plant. The combustible material to be incinerated is fed to combustor R-l via line 8. It is understood that the combustor can be any suitable process unit for burning such combustible materials. For example, the combustor can be a conventional chlorinated waste incinerator, a valorization of chlorinated residuals process unit, and the like. Combustor R-l, which will typically be an incinerator, can be a unit designed to burn garbage and/or RDF alone or a unit that can burn a mixture of garbage and/or RDF and coal, a mixture of garbage and/or RDF and petroleum coke, or a mixture of garbage and/or RDF, coal and petroleum coke. Fluid bed combustors are preferred combustion units for burning such mixtures. Slag is removed from combustor R-l via line 9. The scheme includes a heat exchanger E-l, where steam is preferably produced from the heat generated in combustor R-l in water/steam loop 14/16 . The steam preferably is used to produce useful output, for example, to drive a steam turbine ST-1, which is connected to, for example, a generator G-l, for producing electricity. Make-up water can be added to the system via line 17. Also, condenser CN-1 is provided within the water/steam loop. Compared to the reactor's (R-l) combustion temperature of approximately 1,000°C and higher, the exhaust gases, which are comprised primarily of C0 2 with some 0 2 and water, exiting the heat exchanger E-l via line 11 are at a significantly lowered temperature (about 500°C or less) and are preferably sent to a solids/gas separation zone P-l wherein particulate matter is removed via line 15, and then through a second heat exchanger E-2 via line 22, where the exhaust gases are further cooled. Low pressure steam is produced in the heat exchanger E-2, which is preferably also fed into the steam turbine ST-1 preferably to be used for producing electricity via water/steam loop 14/20. The exhaust gas steam exiting heat exchanger E-2 enters the recycle compressor C-l via line 23. Since no air (which is comprised mostly of nitrogen N 2 ) is fed into the combustor R-l, there will be substantially no NO x present in the exhaust gas stream entering or exiting the compressor C-l. Combustor R-l, is thus isolated from the air during combustion, with another source of O 2 being provided to support combustion for rapid oxidation. The desired portion of exhaust gases, that are comprised primarily of the CO exiting the compressor C-l is routed via lines 24 and 12 into a mixing unit M-l, where the desired mixture of O 2 and CO 2 is formulated for feeding into the combustor R-l via line 13. A remaining portion of the C0 2 -containing exhaust gas discharged from the compressor C-l, an amount preferably equivalent to the rate at which C0 2 is generated in the combustor R- 1, is routed via line 26 through scrubber S-1, where it passes countercurrent to down-flowing aqueous alkaline solution via line 30. It is preferred that the alkaline solution be a relatively weak solution, to remove (neutralize) any trace quantities of acid components that may be in the exhaust stream. The alkaline solution can be any suitable basic solution that is conventionally used to neutralize such streams. Non-limiting examples of such streams include those based on sodium hydroxide, potassium hydroxide, calcium hydroxide, as well as their corresponding carbonate solutions. The alkaline solution, after contacting the up-flowing exhaust gas stream will contain salts of those acids that were in the gaseous stream. At least a portion of this alkaline solution can be recycled to the scrubber S-1 via lines 32, 34, and 30. It is preferred that this salt-containing alkaline solution be passed via line 36 to a suitable conventional separation unit for removal of the salts. The scrubbed exhaust gas stream exiting scrubber S-1 via line 28 is comprised primarily of CO 2 , with minor amounts of 0 2 . This stream is routed via lines 28, 38, and 40 through one or more, preferably one of two sorption (clean-up) beds B-l and B-2. Clean-up beds B-l and B-2 contain a conventional absorbent material capable of removing at least a portion, preferably substantially all of any pollutants, particularly dioxins, from the C0 2 containing stream. Any sorbent material suitable for such use may be used. Non- limiting examples of suitable sorbents include activated carbon, molecular sieves (zeolitic materials), aluminas, and silicas, with activated carbon being the most preferred. The terms sorbent, adsorbent and absorbent are sometimes used interchangeably herein. The important aspect is that the sorbent be able to remove (sorb) the pollutants from the CO 2 containing stream, either by adsorption or by absorption. When either bed, B-l or B-2, needs to be reactivated, carbon dioxide (C0 2 ) with some oxygen (O 2 ) via line 42 can be routed through a heat exchanger E-3, where the mixture is heated by steam or other suitable means to raise the temperature to a level satisfactory for reactivating the bed. If the bed's sorbent material is composed of activated carbon, then the reactivation gas stream can be enriched with O 2 and the heated only to the temperature required to initiate an exothermic reaction between the O 2 and the carbon sorbent material, such as, for example, a temperature of about 120°C or greater. The flow rate and O content of the reactivation gas stream preferably are controlled to achieve the required temperature for properly reactivating the bed. The gases exiting the beds B-l and B-2 via line 44 and 46 during reactivation preferably are routed back into the combustor R-l via line 48. This assures that all pollutants stripped from the absorbent beds during reactivation are subjected to high temperature combustion (decomposition) and thus are converted to harmless compounds. Likewise, if the sorbent material in beds B-l and B-2 is activated carbon, then a portion of the carbon will be converted to CO during each reactivation. Therefore, make-up carbon (not shown) will periodically added to beds B-l and B-2. The substantially pollutant-free C0 2 stream exiting absorbent beds B-l or B-2 via line 50 typically will contain a minor quantity of 0 2 . This stream can be either vented to the atmosphere or it can used to react with, for example, ammonia to produce urea, or to react with hydrogen to produce methanol. However, the main purpose of the scheme presented in Figure 1 is to provide a non- polluting method for burning municipal waste or fuel derived from typical municipal garbage and waste, thus eliminating, or at least substantially reducing, the need for the landfill disposal of such waste materials. If one chooses only to avoid the release of such things as dioxins to the atmosphere, but does not choose to also curb the release of NO x and C0 2 , as achieved in the embodiment of this Figure 1, then Figure 2 represents a practical, low cost method for accomplishing this alternative objective. In Figure 2, those objects that were previously discussed for Figure 1 are numbered in a similar way except they are a numbered 100 higher than those of Figure 1. In this scheme, air is employed via line 110 as the source of the O 2 required for the combustion of the combustible material that is introduced in combustor R-101 via line 108. When the products of combustion exit the scrubber S-101 via line 128, the stream primarily comprises C0 2, N 2 , 0 2 and water vapor and possibly trace quantities of such toxic pollutants as dioxins. This scrubbed gaseous stream is routed into and through either or both sorbent beds B-101 and B-102. Each bed contains a sorbent material preferably capable of removing from the stream substantially all of the pollutants, such as dioxins, from the stream. The gas exiting the sorbent bed that is in service removing the pollutants, can be discharged to the atmosphere via line 150, which gas will be substantially free of toxic compounds, such as dioxins. The vented stream primarily comprises N 2 , C0 , and O 2 , along with trace amounts of NO x . When the pollutant sorption capability of the bed in service nears exhaustion, flow can be diverted through the other bed using appropriate piping (details of the valves, pipe lines, etc., being well known to those of ordinary skill in the art), taking the bed off-line, and the exhausted bed can then be reactivated. Reactivation preferably is accomplished by passing compressed air via line 160 through the heat exchanger E-103 to increase its temperature to a suitable deactivation temperature. If the clean-up beds contain absorbent material other than activated carbon, the source of heat for the heat exchanger E-103 could be, for example, fired natural gas of fired fuel oil, in order to heat the reactivation air to a high enough temperature to drive the dioxins and other such pollutants out of the absorbent beds. If activated carbon is used as the absorbent material, then the reactivation air, as it passes through heat exchanger E-103, only has to be heated with steam or electricity to a high enough temperature, such as, for example, a temperature of about 120°C, to initiate a reaction between the O 2 in the heated reactivation air stream and the activated carbon itself. This reaction is exothermic, and the desired reactivation temperature of the bed can be achieved simply by controlling the rate of flow of the reactivation air. This approach preferably uses a periodic, alternate recharging of the clean-up beds with necessary amounts of activated carbon. This description of the clean-up bed is suitable for all figures hereof. An important, novel and unique aspect of this scheme is the routing of the reactivation gases exiting either of the sorbent beds back into the combustor R-101 via line 148, wherein the toxic pollutants stripped from the sorbent beds during reactivation are destructed in the combustor, thus preventing such toxic chemicals from escaping to the atmosphere. The scheme of Figure 2 also shows a supply of nitrogen via line 162 that can be passed through the sorbent bed to cool it down immediately after reactivation. During the cooling procedure, the N 2 exiting the bed being cooled preferably is diverted to the atmosphere via lines 148 and 152. Before putting the reactivated bed back into service, it is preferably cooled to about ambient temperature. Figure 3 represents an alternative embodiment of the present invention whereby air, water, coal and petroleum coke are used to produce electricity, urea, and methanol in a non- polluting manner. The first step in the process is to introduce air via line 210 into process plant Plt-1, which is a conventional air separation plant to produce an oxygen (O 2 ) stream via line 212, a nitrogen (N 2 ) stream via line 226, and a stream containing the minor components of air, such as argon via line 205. A portion of the nitrogen can be vented via line 207 if necessary. A portion of the 0 2 produced in plant Plt-1 is fed via line 212 and 214 to a second plant Plt-2, where it is reacted with coal and/or petroleum coke introduced via line 216 and water via line 218 to produce hydrogen (H 2 ) and carbon monoxide (CO). A second portion of the 0 produced in plant Plt-1 if passed via lines 212, 240, and 250 to gas turbine GT-201. A third portion of this 0 2 stream is passed to combustion plant Plt-5 via lines 212, 240, 230, and 267. A fourth portion of this O 2 stream can be passed via lines 212 and to the reactivation system of sorbent beds B-201 and B-202. The H 2 /CO stream that is produced in second plant Plt-2 is passed via line 220 to third processing plant Plt-3, which is a conventional gas/gas separation plant wherein the H 2 and CO are separated from each other, thus producing a substantially pure stream of H 2 via line 222 and a pure stream of CO via line 224. In a fourth processing plant Plt-4, pure nitrogen (N 2 ) via line 226 that is produced in the first plant Plt-1 is reacted with the H 2 via line 222 produced in the third plant Plt-3 to produce ammonia (NH 3 ). In a fifth, processing plant Plt-5, coal and/or petroleum coke via line 228 are combusted with a mixture of O 2 / CO 2 via line 230 to produce high pressure steam, that is then used, for example, to generate electricity with generator G-201, which is driven by the steam turbine ST-201. Lines 232, 234, and 236 represent the steam/water lines for transferring heat from the heat exchanger to the turbine and generator. Slag can be removed via line 209. The exhaust gases exiting the fifth plant Plt-5, which primarily comprises C0 2 and a minor amount of O 2 , are passed via line 240 to particulate matter removal unit P-201 to remove particulate matter via line 215. The stream is then routed via line 242 through heat exchanger E- 201 for cooling. Steam is produced in the heat exchanger E-201 and preferably is routed into the steam turbine ST-201 for generating electricity. Upon exiting heat exchanger E-201, the CO 2 /0 2 exhaust stream enters compressor C-201 via line 244. A portion of the C0 2 /0 2 exhaust gas stream exits compressor C-201 via line 246 is preferably blended with the 0 2 of line 230 via line 240 produced in the first plant Plt-1 and fed into the combustion chamber of fifth process plant Plt-5 via line 267. Another portion of the CO 2 /O 2 exhaust stream from the compressor C-201 is preferably fed into the gas turbine GT- 201 via lines 246, 240, and 250 where it is blended with the CO produced in the third plant Plt-3 via line 224, thus providing a combustible mixture for driving the gas turbine GT-201. Generator G-202 is connected to gas turbine GT-201 and thus is used to generate electricity. The hot exhaust gaseous stream exiting gas turbine GT-201 preferably is routed via line 252 to the combustion chamber of the fifth plant Plt-5, where the BTU content of the stream preferably is captured to produce high pressure steam. The remaining portion of the C0 2 /0 2 stream being discharged from the compressor C- 201 is preferably passed via line 254 to scrubber, or neutralizer, S-201. Scrubber S-201 is the same as that of Figures 1 and 2 hereof and will not be discussed in further detail. Lines 256 to 262 correspond in function to those of 30 to 36 of Figure 1 hereof. The scrubbed stream is passed to sorption or clean-up beds B-201 or B-202 for the removal, by sorption, of toxic impurities and the beds that are operated in accordance with the discussion of the sorption beds of Figures 1 and 2 hereof. Upon capturing the toxic impurities, the beds B-201 and B-202 can be regenerated, or reactivated, in the same manner as previously described. The gases exiting the sorbent beds during reactivation, which gases will contain pollutants, such as dioxins, are routed via line 267 to the combustor at Plt-5. The clean stream exiting sorption beds B-201 and/or B-202 via line 266 are primarily comprised of CO and a relatively small quantity of 0 2 , which stream can be rendered into substantially pure CO The purified C0 2 stream via line 268 is preferably then reacted with the ammonia via line 270 produced in the fourth plant Plt-4 to produce urea (NH CONH 2 ) via line 271, as shown in a sixth chemical processing plant, Plt-6. Also, the purified C0 2 stream can be reacted with H 2 via line 272 produced in the second Plt-2 to produce methanol (CH 3 OH), as shown in a seventh chemical processing plant, Plt-7; or, the purified C0 2 can be vented via line 274, if necessary or desired. With the integrated scheme shown in Figure 3 hereof, solid fuels such as coal and petroleum coke can be used to produce electricity, urea and methanol with no NO x , with no pollutants and no greenhouse gases escaping to the atmosphere. The urea that is produced can be used as a fertilizer to significantly increase the production of grains, such as corn, from which, for example, ethanol can be produced. Also, utilizing urea as a fertilizer for rapidly growing trees, such as the Southern pine, could lead to massive tree farming for providing fuel and energy for the future. Also, urea can be used as a chemical feedstock for producing such things as ureaformaldehyde, sulfamic acid, and melamine. Urea is also used in the formulation of certain animal feeds. There are multiple chemical feedstock uses for methanol. Also, internal combustion engines could be designed and built to operate with methanol and methanol blends serving as the fuel. Gas turbines also could be designed to use methanol-blends as fuel. By producing methanol as taught in this integrated processing scheme, methanol could conceivably achieve a significant position as a fuel in the transportation industry. If one chooses to continue releasing C0 and NO x into the atmosphere, while destructing chlorinated hydrocarbon waste through high-temperature oxidation, then the scheme presented in Figure 4 hereof offers a practical, low-cost way for doing so with zero release of dioxins and other such toxic pollutants to the atmosphere. In this scheme, air is the source of the oxygen required to carry out the oxidation of chlorinated hydrocarbon waste materials that is introduced into combustor R-301 via lines 310 and 312. The combustor can be a valorization of chlorinated residuals process unit or a conventional waste incinerator typically used for chlorinated waste materials. Both liquid and gaseous chlorinated materials are fed via lines 314 and 312 into combustor R-301 wherein they are oxidized by combustion. The product stream from combustor R-301 which will typically be comprised of HC1, N 2 , CO 2 , H 2 0, and O 2 is passed to sorption/stripper SS-301 via line 316 where at least a portion of the HC1 and at least a portion of the H 2 0 are removed. The water is collected via line 318 and the HC1 is collected via line 320. The stripped gaseous product stream is then passed via line 322 to scrubber S-301 where it is contacted with a countercurrent downward flowing stream of aqueous alkaline solution introduced via line 324. As previously described with the respect to Figures 1 and 2 hereof the aqueous alkaline solution will remove trace acid components and produce salts thereof. At least a portion of the aqueous solution containing salts of the stripped acid(s) is collected from S-301 via line 326. Another portion, if desired, can be recycled via line 328. The stripped product stream from stripper S-301 is passed to compressor C-301 via line 330. The product stream of oxidation exiting compressor C-301 via line 332 will consist primarily of CO 2 , N 2 , 0 2 , with slight amounts of water vapor and trace quantities of such toxic pollutants as dioxins. The stream exiting compressor C-301 is preferably routed via line 332 and 334 and 333 to either of the clean-up beds B-301 or B-302, each bed containing a conventional sorbent material as previously described that is capable of removing substantially all toxic pollutants, such as dioxins. Preferred sorbents include activated carbon, molecular sieves, alumina, and silica. The most preferred sorbent material is activated carbon. The gaseous stream exiting the sorbent bed that is in service capturing the toxic pollutants can be discharged to the atmosphere via lines 336 and 338. The stream vented to the atmosphere will typically be comprised of N 2 , CO 2 , and 0 2 with the presence of a minute amount of NO x . This stream will be substantially free of dioxins or other such toxic compounds. Nitrogen can be passed via lines 339 and 340 to heat exchanger E-301 and through a sorption bed to cool it down immediately after reactivation. During the cooling procedure the nitrogen exiting the bed being cooled is preferably vented to the atmosphere via lines 336, 337 and 341. When the pollutants sorption capability of the bed (B-301 or B-302) in service nears exhaustion, flow can be diverted through the other bed, and the exhausted bed reactivated. Reactivation can be accomplished by, for example, passing compressed air via lines 335 and 340 through a heat exchanger E-301. If beds B-301 or B-302 contain sorbent material other than activated carbon, the source of heat for the heat exchanger E-301 preferably is, for example fired natural gas in order to heat the reactivation air via line to a temperature high enough to drive dioxins and other such captured pollutants out of the sorbent beds. If activated carbon is used as the absorbent material, then the reactivation air as it passes through the heat exchanger E-301 only has to be heated using steam or electricity to a temperature of, for example, about 120°C, which is high enough to initiate a reaction between the O 2 in the heated reactivation air stream and the activated carbon itself. This reaction is exothermic and the desired reactivation temperature of the bed can be achieved simply by controlling the rate of flow of the reactivation air stream. A unique aspect of this scheme is the routing of the reactivation gases exiting either sorption bed B-301 or B-302 back into the reactor R-301 via lines 336, 337, 342, 310, and 312 where the toxic pollutants, stripped from the sorbent bed during reactivation, are destructed, thus preventing any toxic chemicals from escaping to the atmosphere. As noted above, the schemes or approaches of the above described embodiments offer one or more of the following benefits: 1. A practical way to incinerate municipal garbage and other such waste materials without releasing to the atmosphere NO x , dioxins and other such pollutants, thus in essence eliminating or at least significantly reducing the future need for landfill disposal of such waste materials. 2. A practical way to modify coal-burning electric power generating plants so that such plants can operate with substantially zero NO x emission. 3. A practical way to use coal and/or petroleum coke for efficiently producing electricity, urea and methanol with substantially zero emission of NO x , substantially zero emission of such pollutants as dioxins and greatly reduced emission of the greenhouse gas CO . By using more of America's abundant coal reserves in the none-polluting methods of the present invention, the U.S.'s dependence on imported crude oil can be greatly reduced, while at the same time creating many, and much needed, new jobs in the mining and use of coal, as well as in farming and down-stream farming businesses. 4. A practical low-cost way to modify and/or build new incinerator and VCR systems that are used to destruct chlorinated hydrocarbon materials, such that there will zero discharge of toxic chemicals such as dioxins to the atmosphere. It is noted that the embodiments described herein in detail for exemplary purposes are, of course, subject to many different variations in, for example, structure, design, application, equipment, chemical components and/or methodology. Because many varying and different embodiments may be made within the scope of the inventive concept(s) herein taught, and, because many modifications may be made in the embodiments herein detailed in accordance with the descriptive requirements of the law, it is to be understood that the details herein are to be interpreted as illustrative and not in a limiting sense.

Claims: What is claimed is: 1. A process for incinerating combustible material which is capable of producing a waste stream containing pollutants selected from the group consisting of acid gases and toxic gases, which process comprises: a) incinerating said combustible waste material in an incinerator, thereby producing a slag and a gaseous effluent product containing said pollutants; b) collecting said slag; c) passing said gaseous effluent through a heat exchanger thereby reducing its temperature by at least 200°C; d) passing said lowered temperature gaseous effluent to a sorption zone comprised of at least one bed of sorbent capable of sorbing at least a portion of said pollutants from the gaseous effluent; e) collecting or venting the gaseous effluent containing reduced levels of pollutants; e) reactivating said one or more sorbent beds with a reactivating reagent capable of removing said pollutants from said adsorbent beds, thereby resulting in a reactivating reagent stream containing said pollutants; and f) passing said pollutant containing reactivating stream to said incinerator where said pollutants are decomposed by combustion. 2. The process of claim 1 wherein the gaseous effluent stream leaving said heat exchanger contains particulate matter which stream is passed to a solids/gas separation zone wherein at least a portion of said particulate matter is removed from said gaseous effluent stream. 3. The process of claim 1 wherein the incineration is conducted at a temperature from about 1,000°C to about 1,500°C. 4. The process of claim 1 wherein said gaseous effluent stream after it leaves the heat exchanger is passed to a scrubbing zone wherein it is passed countercurrent to an aqueous alkaline solution to remove at least a portion of any acid components in said effluent stream. 5. The process of claim 1 wherein the adsorbent beds are comprised of at least one adsorbent selected from the group consisting of activated carbon, alumina, silica, and molecular sieves. 6. The process of claim 5 wherein said adsorbent is an activated carbon. 7. The process of claim 1 wherein the reactivation reagent is selected from the group consisting of oxygen and air. 8. The process of claim 4 wherein the aqueous alkaline solution exiting the scrubbing zone contains salts of the acids removed from the effluent stream and salt-containing alkaline solution is passed to a separation zone to remove said salts. 9. The process of claim 1 wherein the heat extracted by the heat exchanger of step (c) is used to produce steam for downstream use. 10. The process of claim 9 wherein said steam is used to drive a turbine to produce electrical energy. 1 1. The process of claim 1 wherein the combustible material is selected from the group consisting of coal and petroleum coke and wherei i) air is sent to an air separation plant wherein a stream of oxygen and a stream of nitrogen are produced; and ii) the oxygen stream is conducted to a syngas generation plant wherein a stream of carbon dioxide and hydrogen are produced, which stream of carbon dioxide and hydrogen is sent to a gas separation plant wherein separate streams of carbon dioxide and hydrogen are produced; and iii) a portion of the hydrogen produced is conducted to a methanol plant where is combines with said gaseous effluent containing reduced levels of pollutants to produce methanol. 12. The process of claim 11 wherein a portion of the hydrogen stream is conducted to an ammonia plant along with a stream of nitrogen from the air separation plant to produce a stream of ammonia. 13. The process of claim 12 wherein said stream of ammonia is conducted to a urea plant along with a portion of said gaseous effluent containing reduced levels of pollutants to produce urea. . The process of claim 13 wherein said pollutant containing reactivation stream is conducted said incinerator to decompose said pollutants.

Inventors: TAYLOR TOMMY G, TAYLOR, TOMMY, G.
Applicants: TAYLOR TOMMY G, TAYLOR, TOMMY, G.
Application year: 2000
Main classification: B01D45
IPC codes: B01D53