MXPA99000650A - Method for minimizing corrosion by halide dehydrogen in a parc oxidation process - Google Patents

Abstract

The present invention relates to a method for minimizing hydrogen halide corrosion in a cooling gasifier during the non-catalytic partial oxidation reaction of a halogen-containing hydrocarbonaceous filler, to produce a synthesis gas containing hydrogen halide, solids particulates finely divided and non-toxic slag. The synthesis gas containing hydrogen halide is brought into contact with the water within the cooling zone (14) of the gasifier (10). The cooling water contains a neutralizing agent, in excess of the amount necessary to neutralize the hydrogen halide acids present therein, and in this way the halide salts are formed. The cooling water containing halide salts is purified to recover the halide salts. Free water salt is essentially non-toxic environmentally and can be recycled into the process or disposed of in accordance with environmental regulations

Description

METHOD FOR MINIMIZING CORROSION BY HYDROGEN HALIDE IN A PARTIAL OXIDATION PROCESS This application claims the benefits of Provisional Applications Nos. 60 / 021,880; 60 / 021,882; 60 / 021,886; 60 / 021,881 and 60 / 021,891 all filed July 17, 1996. BACKGROUND OF THE INVENTION 1. Field of the Invention This invention relates to a method for minimizing corrosion by hydrogen halides in a partial oxidation cooling gasifier, and dragged flow. 2. Description of Previous Technology Oil, coal and other natural resources are used as fuels, for transportation, heating and power generation, and also as a charge for partial oxidation gasifiers for the manufacture of various industrial chemicals. This includes gaseous, liquid and solid hydrocarbons. Almost any combustible material containing carbon and hydrogen can serve as a charge for the gasification process by partial oxidation, such as natural gas, methane, crude oil, shale oil, bitumen, heavy residual oil, coal, petroleum coke, silt drainage, light hydrocarbon fuel, various carbons including anthracite, bituminous, subituminous and lignite, and various mixtures thereof. Also useful as a filler for the gasification process by partial oxidation are several mixtures of silts of the aforementioned, using, among other things, hydrocarbons or other gaseous or liquid materials to form a pumpable silt. The decrease in natural resources as well as economic considerations have led to an increase in the use of organic loads that come from impure sources, such as waste or plastic waste containing relatively high levels of pollutants. The plastic waste is used as a hydrocarbonaceous filler in a partial oxidation reaction to produce mixtures of hydrogen and carbon monoxide, referred to as synthesis gas or simply "syngas". The singas can be used to make other useful organic compounds or as fuel to produce energy; Waste or plastic waste materials are often composed of at least one carbonaceous thermoplastic solid and / or thermosetting material - which may or may not contain inorganic matter, such as fillers and reinforcement. These materials can be derived from obsolete equipment, containers of household goods, packaging, industrial sources, recycling centers and discarded cars. The plastic waste is composed of organic polymers derived from plates, films, extruded forms, moldings, reinforced plastics, laminated plastics and foamed. The mixture of plastic waste varies with the source and with the presence of non-combustible inorganic material incorporated in the plastic, such as fillers, catalysts, pigments and reinforcement. The inorganic matter may also include dyes and pigments such as the compounds of cadmium, chromium, cobalt and copper; non-ferrous metals such as aluminum and copper in plastic coated wire cuttings; metal films; woven and nonwoven fiberglass, graphite and boron reinforcing agents; metal inserts made of steel, brass and nickel; and lead compounds from automotive plastic batteries. Heavy metals are also present, such as, for example, cadmium, arsenic, barium, chromium, selenium, and mercury. The inorganic constituents may be present in the solid hydrocarbonaceous material containing plastic in an amount ranging from one trace to about 30 weight percent of this plastic-containing material. Solid hydrocarbonaceous plastic waste typically consists of polyethylene, polyethylene terephthalate, polypropylene polyesters, polyurethanes, polyamides, polyvinylchloride, polystyrene, cellulose acetate and mixtures thereof. Also found, polyurea, polycarbonate, cellulose, acrylonitrile-butadiene-styrene (ABS), acrylics, alkyds, epoxy resins, nylon, phenolic plastics, polyacetals, alloy-based polyethylene, styrene, acrylonitrile, thermoplastic elastomers, fluoride polymers, sheets of rubber, urea and melamine. Due to the reduced conditions that exist during the partial oxidation reaction, the halogen content of the halogenated organic material is converted to hydrogen halide or ammonium halide. The free halogens that are formed during a complete combustion of halogenated organic materials are not formed under the conditions in the partial oxidation gas reactor. Other halogen compounds such as phosgene (C0C12), cyanogen chloride (CNC1), volatile halide compounds such as AICI3, Cl4 and POCI3 are not formed during the partial oxidation reaction although aluminum, vanadium or phosphorus They may be present in the cargo. A cooling gasifier is used to drive the partial oxidation reactions and capture most of the acidic components of the singas in the chilled water. The partial oxidation reaction is carried out in a non-catalytic cooling gasifier without free-flowing packing. The reaction temperature is from about 1800 ° F to 3000 ° F and the reaction pressure is from about 1 to about 100 atmospheres, preferably from about 24 to about 80 atmospheres. Under these high temperatures and pressures, substantially all halogenated organic materials are rapidly converted to hydrogen halide, carbon dioxide, carbon monoxide, hydrogen cyanide, ammonia, carbonyl sulphide, hydrogen and trace amounts of other gases and small amounts of carbon. The presence of halogens in plastic waste can be in the range from trace amounts to as much as 10% by weight or more, and can cause severe corrosion problems. - During the non-catalytic partial oxidation reactions, the halogen content of the hydrocarbonaceous plastic waste feed is first converted to hydrogen halides. At high temperatures, these acidic halides make the heat recovery of the resulting syngas impractical due to corrosion problems prior to the removal of the acidic component. This problem is compounded when the halogen content is highly variable and can not be easily measured, as is the case with any waste material, particularly plastics, thus making the implementation of counter-corrective measures very difficult. The extent of corrosion in the cooling portion of the reactor and in the downstream equipment is reduced by adding a base to control the pH. A second problem arises from the variable nature of the halide content in the charge. If the pH in the water system becomes very high, depending on the base used, the salts can be precipitated in parts of the water process system causing blockage and / or clogging. It is difficult to control the addition rate of the base to equalize the halide loading rate because the pH control of the hot, pressurized process water or the advance charge control based on the halide analysis of the charge It is not reliable. In the gasification of well-defined charges containing low amounts of halides, in the order of about 0.05% by weight to about 2% by weight, the addition of a base to neutralize the acidic halide content of the gasification water flows they are based on stoichiometric quantities of the base for the average amount of acid produced in the gasifier. Since the polishing capacity of the process water is typically higher than the variations in acid generated by the components in the load, the pH of the process water can be measured autonomously and the addition rates of the base adjusted as needed. However, when the amount of halides in the load can far exceed the natural polishing capacity of the process water, and where this amount can change rapidly, this system will not be able to prevent severe corrosion. This can occur when there is less than about 0.5% by weight of halide in the charge, and normal or low amounts of nitrogen or alkali metals in the charge, where "normal" is defined as the amounts typically found in oil residues, coal or petroleum coke. The U.S. Patent No. 4,468,376 to Suggitt discloses a method for disposing of the fixed amounts of halogenated organic material produced during a partial oxidation reaction. For example, the cooling zone of the gasifier is maintained at a pH above 7 with ammonia to ensure that there is sufficient ammonia to react with the hydrogen halide in the flow of synthesis gas. Thus, the Suggitt patent reveals how to avoid contamination of the synthesis gas with acid, but does not reveal how to avoid corrosion in the process water system. The Suggitt patent does not explain how to control the addition of ammonia when the charge to the gasifier contains varying amounts of halide, which is the situation encountered when plastic waste materials are used as a filler. If an excessive amount of ammonia or other equivalent base is added to the cooling water in such a way that the pH rises to about 10, the solid salts of ammonium carbonate will precipitate as a result of the reaction of NH3 or the cationic portion. of another equivalent base with dissolved carbon dioxide in any water that comes in contact with or condenses from the syngas. This can cause plugging problems in the water system used in the gasification operation, particularly in the heat exchangers used to cool the still of the cooler and scrubber temperatures to about 350 ° F (175 ° C) to around 600 ° F (315 ° C), up to temperatures around 80 ° F (26 ° C) to around 300 ° F (148 ° C), for additional cleaning or processing. Alternatively, if the amount of ammonia or other equivalent base is insufficient to react with all of the hydrogen halide in the synthesis gas flow rate, rapid and catastrophic acid corrosion of the building materials will occur, such as carbon steel. In addition, the presence of ammonia or any volatile base contaminates the synthesis gas product. Therefore the process has to be adapted to remove the neutralizing base of the synthesis gas and to recover or discard any excess of the base. If a person trained in the technology follows the teachings of the Suggitt patent, it can lead to large amounts of excess water or blockage or blockage in parts of the water system used in the partial oxidation reaction system. The Suggitt patent does not disclose the specific means to ensure that there is always an excess of ammonia, particularly for fillers where the halide content varies widely. Thus, the Suggitt patent does not disclose how to control pH with ammonia, or how to treat charges that have a variable halogen content. In essence, the Suggitt patent does not reveal how to control pH or corrosion while the halide content in the charge varies, nor does it address the problem of ammonia contamination in the synthesis gas. When a charge with a high and variable chloride content is gasified, in the order of about 10% by weight to about 15% by weight, where the addition of ammonia is based on periodic independent analyzes of samples, for example every 30 minutes, a sudden increase in the chloride content of the charge causes the pH of the chiller water to drop to less than 1 in less than 15 minutes. The failure experienced in a carbon steel component of the process water pipeline due to corrosion that caused a hole in the line. The time required for the pH to fall to dangerous levels, if the addition of ammonia is interrupted or inadequate, it may be less than 30 minutes in a gasifier with more than 2% by weight of chloride in the charge. This can cause rapid corrosion on any of the carbon steel components, and can result in the release of hot, pressurized water or gas. In circumstances similar to those cited above, difficulties in adjusting the output of the ammonia addition pump caused the ammonia addition rate to be almost double the amount required for neutralization. This caused a rapid clogging in the synthesis chillers in less than an hour, resulting in the closure of the reactors.

SUMMARY OF THE INVENTION The present invention relates to a method for minimizing the corrosion of hydrogen halide in a coolant gasifier during the non-catalytic partial oxidation reaction of a hydrocarbonaceous filler with a variable halide content, to produce a synthesis gas with content of hydrogen halide or "singas". The synthesis gas with hydrogen halide content makes contact with the cooling water in the cooling zone of the gasifier which contains a neutralizing agent that is in excess of the stoichiometric amount necessary to neutralize the acid gases of the hydrogen halide contained in the synthesis gas. The neutralized hydrogen halide gases form the condensed halide salts in the cooling water. The halide salts can be purified for later use. A portion of the cooling water containing the halide salts is removed and treated to recover the halide salts. The treated cooling water can be recycled into the process or discarded in compliance with environmental regulations. BRIEF DESCRIPTION OF THE DRAWING The drawing that accompanies this is a simplified diagram representation of the operational steps to minimize hydrogen halide corrosion when a variable content of halide in the hydrocarbonaceous load undergoes partial oxidation. DESCRIPTION OF PREFERRED EMBODIMENTS In accordance with the present invention, corrosion control is provided in the cooling gasifier system of the process water, and the cooling and purification operations of the synthesis gas of the gasification system by adding a stoichiometric excess of the neutralizing agent, such as ammonia to the water circulating in the cooling zone of the gasifier, so that there is always a sufficient amount of the neutralizing agent in the cooling water to neutralize the hydrogen halide acids present in the synthesis gas. The added amount is chosen to ensure that the pH of the cooling water existing in the cooling zone of the gasifier is always within the range of about 3.5 to about 9.0. This is because if the pH is lower, rapid and catastrophic corrosion occurs, while a higher pH can cause the cooling system to clog with ammonium carbonate.

The inventive process is designed to provide an ammonia content that is always with a stoichiometric excess of the maximum expected amount of halide, and low enough so that the ammonium carbonate does not precipitate in the gasification process system, more specifically, in the singas coolers. While acid gases such as carbon dioxide, hydrogen sulfide and hydrogen cyanide are formed during the partial oxidation reaction, the cooling of the synthesis gas cooler and the subsequent purification water cause the hydrogen halide gaseous reaction preferably with ammonia. Format ions (HCOO ") are formed in the cooling water, and since they are not volatile, they remain in the water.Some gases of carbon dioxide and hydrogen sulfide are solubilized in the water, but most remain in the water. Since hydrogen halides and ammonia are very soluble, all halides will be absorbed into the water.If there is an excess of ammonia in the water, an ionization will occur to form the chloride ions (Cl "). ammonium (NH4 +) in the solution. The hydrogen halide contained in the synthesis gas is passed from the reaction zone of the gasifier to the cooling zone where it makes contact with the cooling water containing the neutralizing agent that is always in a stoichiometric excess of the minimum amount necessary to neutralize the hydrogen halide acids present in the synthesis gas, so that the corresponding halide salts are formed in the cooling water. The synthesis gas substantially free of halogen is then passed to the purification operation where the synthesis gas is purified with water to remove any particulate solid finely divided, entrained. The neutralizing agent is preferably added in an amount such that the cooling water existing in the cooling zone of the gasifier has a pH from about 3.5 to about 9.0, preferably from about 4.5 to about 8.5. The scrubber water in the scrubber is also maintained at a pH from about 3.5 to about 9.0, preferably from about 4.5 to about 8.5. A pH below 3.5 can cause catastrophic and rapid corrosion by halides. A higher pH can cause a plugging of the cooling system by ammonium carbonate. The use of a volatile base such as ammonia as a neutralizing agent is preferred because the vapor spaces in the cooling chamber, the scrubber and the heat exchangers used to cool the synthesis gas could not be properly protected otherwise. This is due to the volatility of the halogen acids. When a non-volatile base is used, acidic condensates may be present. However, when a volatile and highly soluble base such as ammonia is used, there will always be ammonia present in both the liquid and vapor phases, should any of these phases be present an excess amount of ammonia. halides. Since the stoichiometric amount of the neutralizing agent is always greater than the amount of halides in the hydrocarbonaceous filler, there will always be a sufficient base present in the liquid phase to avoid excessive corrosion. This results in the formation of ammonium chloride with an excess of ammonia, instead of an excess of hydrogen chloride, and ensures that there is always very little or no acidic condensate, and a non-corrosive pH from about 6 to about of 10.5 in any condensate. Thus, any condensate of the synthesis gas existing in the cooling portion of the gasifier will consequently not be corrosive. To remove the halides from the gasification system, a halide-containing aqueous stream is purged or removed in such a way that the halide content in the hydrocarbonaceous filler can be discharged from the general process. This is done in the purification step where the halide salts are recovered for later use or disposed of according to environmental standards. All or a portion of the purified water can be returned to the process, as needed, or it can be discarded. As a secondary consideration, it is generally desirable to minimize the amount of water added or removed from the general gasification system of the process water. The composition of the hydrocarbonaceous load controls the water produced or consumed during the gasification process. With reference to the FIGURE, a hydrocarbonaceous filler 2 with halogen content, and any water necessary or associated with the charge, and a free oxygen contained in the gas flow 4 are fed to the reaction zone 12 of the cooling gasifier 10. Where the charge suffers from partial oxidation to form a crude syngas and a slag by-product which passes from the cooling zone 14 of the gasifier 10. The syngas and the slag make contact in the cooling zone 14 with cooling water 32 which contains a neutralizing agent such as ammonia in excess of the stoichiometric amount necessary to neutralize the maximum expected halide content in the stream 2. The non-toxic slag 6 leaves the cooling zone 14 to be discarded or to be used as construction material. The flow rate of substantially free of halogen with an excess of ammonia 8 leaves the cooling zone 14 and enters the scrubber 16 where it makes contact with the cooling water., which removes the finely divided particulate solid material entrained. The clean flow of singas saturated with steam at the operating pressure of the system and containing an excess of ammonia in the flow rate of the gas that is or is almost in equilibrium with the amount of ammonia in the water, comes out of the scrubber 16. and enters the cooler 22 where water vapor and ammonia condense upon cooling to a temperature below the dew point. A dry and clean flow of singles 24, substantially free of hydrogen halide content and only trace quantities of ammonia leave the cooler 22 for later use. The flow rate of condensed water 26 with the ammonia leaves the cooler 22 and is divided into flow rates 18 and 28. The flow rate of water 18 with ammonia content is fed to the scrubber 16 to serve as the scrubbing medium for the flow rate of synthesis fas 8. The ammonia content water stream 28 enters the ammonia separator 30, and comes out as a flow of water rich in ammonia 32 and a flow rate of water poor in ammonia 36. The flow rate of water rich in ammonia 32, also referred to as the "evaporation separator" is combined with additional ammonia from the stream 64, as necessary, to provide sufficient ammonia in excess of the stoichiometric amount necessary to neutralize the maximum expected halide content of the hydrocarbonaceous filler 2. The flow rate of water poor in ammonia 26 existing in the ammonia separator 30 is divided into ammonia-poor water streams 38 and 40. The ammonia-poor water flow rate 38 can be discharged if the ammonia is discharged. Local regulations allow or may be subject to an additional purification treatment of waste water is necessary before disposal. The ammonia-poor water flow rate 40 is fed to the cooler 22 to condense water vapor and ammonia from the syngas. Alternatively, all or a portion of the water flow 38 can be recycled to the cooling zone 14 or to the scrubber 16, or to a portion of both. Since carbon dioxide is present in the synthesis gas at concentrations much higher than ammonia under the conditions of cooler 22, carbon dioxide is essentially equimolar to ammonia and is also absorbed by stream 26. It is thus , the excess ammonia in the flow rate 20 has to be limited to the solubility limit of ammonium carbonate in the flow rate 26, and therefore the maximum pH of 9.0 in the flow rate 44. The cooling water 42 at a pH of about 3.5 to 9.0 leaves the cooling zone 14 of the gasifier 10 and contains the neutralized condensed halide salts of the syngas. The flow of cooling water 42 is combined with the flow rate of the scrubbing water 44 which leaves the scrubber 16 with a pH from about 3.5 to 9.0 to form the combined water flow rate 46 which is charged with the particulate matter removed from the water. syngas and the halide salts which have been neutralized and condensed from the acid halide vapors that were present in the syngas. The halide salts are first generally chloride salts. The flow of water 46 enters the separator 48 where the particulate solids composed of carbon, ash and some precipitated salts are separated and exited as flow rate 50 for further treatment and discarded in accordance with environmental regulations. This flow of water rich in halide salt free of particles containing dissolved halide salts leaves the separator 48 as a flow rate 532 and enters the purifier 54 where the halide salts 56 are separated and recovered for later use, including their commercialization. A portion of the water 58 free of halide salts leaves the purifier 54 and is combined with the flow rate of particle-free water 60 which leaves the separator 48 to form a combined water flow 62. All or part of the water flow 62 can be recycled to the cooling zone 14 of the gasifier 10. Alternatively, all or part of the water flow 62 can be recycled to the scrubber 16 to serve as an additional source of scrubbing water. Finally, all or part of the water flow 62 can be introduced to the flow of crude syngas 8 to improve the debugging operation before the syngas enters the scrubber 16. The water flow 68 leaves the purifier 54 to make contact with the load hydrocarbonaceous with halogen content 2 entering the gasifier 10 where it serves as a temperature moderator in the reaction zone 12. Ammonia in excess of the actual amount necessary to neutralize the halide content present in the hydrocarbonaceous filler 2 occasionally accumulates in the flow 68 which is combined with the charge 2 or is introduced separately to the reaction zone 12, where the ammonia is substantially destroyed by decomposition. Thus, the excess ammonia can be fed to the reaction zone 12 of the gasifier 10 without accumulating an excess of ammonia in the product of the synthesis gas and eliminating the need for unreliable pH control. It has been found that by controlling the amount of neutralizing agent that is added to the cooling water so that there is always a stoichiometric excess of the maximum halide content of the hydrocarbonaceous filler 2, and by controlling the amount of water in the flow rate 28 that enters to the ammonia separator 30, and controlling the amount if the water in the flow 52 that enters the purifier 54, and determining if sufficient water has been removed from the flow 38 leaving the system to require an addition of water to the system, and if it is added water, select where the water will be added, it can be found that the conditions are such that the pH of the cooling water and the water of purification remains within a non-corrosive range from about 3.5 to about 9.0, and the limit of Ammonium carbonate solubility is not exceeded in the synthesis gas coolers or other parts of the water gasification system, except where the halide salts are precipitated s intentionally in the purifier 54. This is done by taking into consideration that the synthesis gas and water flow through the system, the operating temperatures and pressure, the concentration of soluble species, such as the neutralizer, the halides and the carbon dioxide, and the known equilibrium behavior of these species, that is, the ionization constants, and the vapor pressure against liquid concentrations, and the conduction of a mathematical simulation of the entire system. This process model is well known to those skilled in the art and simulates process conditions for maximum and minimum protection of hydrogen halide from a variable halide hydrocarbonaceous filler. The process conditions are derived from the aforementioned criteria through commercially available simulation packages or a simulation program that can be elaborated directly from known equilibrium relations. In this matter, the process can be controlled in such a way that the maximum expected halide content of the hydrocarbonaceous load, the pH of the cooling water leaving the cooling zone of the gasifier and leaving the purification zone is greater than 3.5 , and in the minimum halide content the pH is less than 9.0. This eliminates the need for online pH control loops. The halogen content of the total hydrocarbonaceous filler to the gasifier may vary from about 0.05% to about 15% by weight, preferably from about 0.1% by weight to about 10% by weight, and more preferably from about 0.2% by weight up to about 5% by weight of the total charge towards the reaction zone. The synthesis gas makes contact with the cooling water, containing ammonia dissolved in it to neutralize and condense the hydrogen halide inside the cooling water. The amount of ammonia in the cooling water is in excess of the stoichiometric amount necessary to completely neutralize the hydrogen halide and other acids that condense in the cooling water. While, ammonia or ammonium salts are the neutralizing agents of preference, any suitable equivalent of the neutralizing agent can also be used. These neutralizing agents include the alkali metal salts, the alkaline earth metal salts, a natural or synthetic mineral or a mineral containing the aforementioned neutralizing agents, and mixtures thereof. The water charge to the cooling zone and to the scrubber generally has a pH of about 7 to about 10. The pH in the cooling zone 14 and the cooling water outlet flow rate 42 are maintained in a desired range to through the addition of liquid or gaseous ammonia in the flow rate 64 in the calculated amount needed. In another embodiment, the cooling and scrubbing water can be maintained at the desired pH level by saturating the charge water with a solid ammonia salt such as ammonium carbonate or ammonium bicarbonate. The saturated solutions of these neutralization agents with a certain pH to ensure that the concentration of ammonia will be sufficient to neutralize any amount of chloride in the charge without online pH measurements or a feedback control. Nitrogen may comprise part of the hydrocarbonaceous filler. Typically about 10% by weight to about 25% by weight of the nitrogen in the hydrocarbonaceous filler is converted to ammonia, and about 0.1% to about 1.5% by weight is converted to hydrogen cyanide (HCN), with the remainder forming molecular nitrogen (N2), which becomes part of the synthesis gas. Additional treatment of residual ammonia is not required and discharge into the atmosphere is avoided, because the excess ammonia is recycled to the gasifier and converted to nitrogen and hydrogen, thus preventing plugging and precipitation of ammonium carbonate. in the system and the contamination of the synthesis gas product with ammonia. The purged water flow rate 28 is concentrated in the ammonia separator 30 to a flow rate with a high concentration of ammonia 32 which is fed to the cooling zone 14 of the gasifier, and a water flow rate 36 with a low concentration of ammonia. can be recycled to the gas cooler 22. The flow of water with a low concentration of recycled ammonia to the gas coolers helps to avoid salt precipitation and decreases the ammonia concentration of the syngas. A portion of the purge flow 38 can be recycled to the scrubber 16, or discarded according to environmental standards. Preferably, the rate of minimum addition of ammonia to the cooling zone 14 is such that the pH of the water flow rate 42 leaving the cooling zone or the cooling chamber of the gasifier is greater than 3.5 of the maximum concentration of halide in the gas. load. Under these conditions, vapors that condense after leaving the cooling zone will also have a pH higher than 3.5. This property dictates the preference choice of ammonia as a neutralizing agent for hydrogen halide. If a non-volatile base is used, there will be no base in the synthesis gas when it is cooled. So the condensate in the chillers can be acidic due to any low concentration of volatile or entrained acids, and the carbon dioxide in the synthesis gas. The benefit of this invention is that the halide corrosion is substantially reduced or eliminated and less expensive building materials can be used to conduct the process. Environmentally "clean" water can be generated and the clogging of the water system due to carbonate precipitation is avoided. Although this invention has been described in the context of the use of ammonia as the base of preference, other equivalent or suitable bases can also be used.

Claims (9)

1. CLAIMS 1. A method to minimize corrosion by hydrogen halide in an operating system for the production and purification of synthesis gas, where this operating system comprises a cooling gasifier with a reaction zone and a cooling zone, an area of purification and a purification zone, comprising: (a) a hydrocarbonaceous filler that reacts to a variable halogen content in a non-catalytic partial oxidation reaction to produce a synthesis gas containing hydrogen, carbon monoxide, halide vapors, hydrogen, water and carbon dioxide. (b) passing the synthesis gas containing hydrogen halides from the reaction zone to the cooling zone and contacting this synthesis gas with the cooling water containing an ammonia neutralizing agent to neutralize the vapors of hydrogen halide and form ammonium halide salts condensed in the cooling water, where the amount of neutralizing agent contained in the cooling water meets a stoichiometric excess of the maximum amount of halide in the hydrocarbonaceous filler and the pH of the water Cooling salt containing ammonium halide salt leaving the cooling zone is about 3.5 to 9.0, and the synthesis gas leaving the cooling zone is substantially free of halide; (c) the introduction of a substantially halide-free synthesis gas into the purification zone where it is contacted with the purification water to remove any entrained finely divided particulate solid, to produce a particulate-free synthesis gas, and substantially halide-free, and where the pH of the scrubbing water leaving the purification zone is around 3.5 to 9.0; (d) the introduction of cooling water containing halide salt into the purification zone, where the halide salts are separated from the cooling water.
2. 2. The method of Claim 1, wherein all or a portion of the purified cooling water is discarded in accordance with acceptable environmental standards.
3. 3. The method of Claim 1, wherein all or a portion of the purified cooling water is recycled to the cooling zone of the gasifier.
4. 4. The method of Claim 1, wherein all or a portion of the purified cooling water is recycled to the reaction zone of the gasifier.
5. The method of Claim 1, wherein the substantially free halide synthesis gas leaving the purification zone is introduced into a cooling zone to condense the water vapor and ammonia of the synthesis gas and form a flow rate. of water containing ammonia and a clean synthesis gas product, and where there is enough water in the cooling zone to prevent the precipitation of ammonium carbonate in the flow of water containing ammonia.
6. 6. The method of Claim 5, wherein the flow rate of water containing ammonia is introduced into an ammonia separation zone where a flow of water rich in ammonia and a flow rate of water poor in ammonia is produced.
7. The method of Claim 6, wherein all or a portion of the flow rate of ammonia-rich water is recycled to the cooling zone of the gasifier.
8. 8. The method of Claim 6, wherein all or a portion of the flow rate of ammonia-poor water is recycled to the cooling zone.
9. 9. The method of Claim 1, wherein the neutralizing agent is ammonia.