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WO1995019407A1 - Procede de gazeification autonome - Google Patents

Procede de gazeification autonome Download PDF

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Publication number
WO1995019407A1
WO1995019407A1 PCT/US1995/000105 US9500105W WO9519407A1 WO 1995019407 A1 WO1995019407 A1 WO 1995019407A1 US 9500105 W US9500105 W US 9500105W WO 9519407 A1 WO9519407 A1 WO 9519407A1
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WIPO (PCT)
Prior art keywords
gasifier
gas stream
pressure
carbonaceous feedstock
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US1995/000105
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English (en)
Inventor
John P. Whitney
Robert E. Lea
William J. Vanderwilt
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Rineco Chemical Industries Inc
Rineco Chemical Ind Inc
Original Assignee
Rineco Chemical Industries Inc
Rineco Chemical Ind Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rineco Chemical Industries Inc, Rineco Chemical Ind Inc filed Critical Rineco Chemical Industries Inc
Priority to AU15586/95A priority Critical patent/AU1558695A/en
Publication of WO1995019407A1 publication Critical patent/WO1995019407A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
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    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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    • C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
    • C10K1/122—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing only carbonates, bicarbonates, hydroxides or oxides of alkali-metals (including Mg)
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    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
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    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
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    • C10J2200/00—Details of gasification apparatus
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    • C10J2300/0959—Oxygen
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    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam

Definitions

  • the invention relates to gasification processes, and particularly to a self-contained process for gasifying carbonaceous fuels, such as hazardous waste-derived feedstocks, without emitting gases to the environment.
  • the invention also relates to a self-contained gasification process for producing useful products from carbonaceous feedstocks such as hazardous wastes.
  • Hazardous wastes are conventionally disposed of by combusting them in incinerators, cement kilns, boilers or industrial furnaces. These disposal techniques are unsatisfactory for at least two reasons. First, fossil fuels such as natural gas are combusted with the hazardous waste materials. This is expensive and consumes a valuable natural resource. Second, combusting the wastes creates a combustion gas stream that is subsequently released into the environment. Because of the potential environmental harm caused by releasing combustion gas streams to the environment, practice of such processes is subject to issuance of permits from various federal and state regulatory agencies.. The time and expense needed to assure continual compliance with environmental regulations, such as the federal Resource Conservation and Recovery Act, makes hazardous waste combustion operations commercially unattractive.
  • U.S. Patent No. 4,950,309 to Schulz discloses a process for converting toxic organic waste to useful materials.
  • a combustible stream of toxic organic waste is gasified with steam at a temperature of 2500°-3500°F.
  • the gasifier is operated at a pressure of 15-1500 psig, preferably 150-450 psig (col. 4, lines 55-57) .
  • Oxygen, oxygen-enriched air, or preheated air converts the waste into a reducing stream containing carbon monoxide, hydrogen, and methane. These products can be used as a fuel or synthesis gas (col. 1, lines 42-44) .
  • the effluent may be scrubbed to remove carbon dioxide and other gases (col. 5, lines 58-64).
  • the carbon monoxide product is reacted with steam in a water gas shift reactor to produce hydrogen and carbon dioxide (col. 6, lines 4-23) .
  • U.S. Patent No. 4,631,183 to Lalancette et al. discloses a process for decomposing toxic organic halogenated substances. The process involves first heating a mixture of a toxic organic halogenated substance, carbon and carbonate or bicarbonate of an alkali metal at 1000°-1600°C in a reaction chamber under a reducing atmosphere. Second, the carbon monoxide exit gas is oxidized into carbon dioxide. Lalancette suggests that advantages are obtained by the absence of oxygen from the process (col. 5, lines 25-26) .
  • U.S. Patent No. 3,528,930 to Schlinger discloses a process for generating synthesis gas (such as carbon monoxide and hydrogen) by reacting hydrocarbons with oxygen and steam at 1800°-3000°F.
  • synthesis gas such as carbon monoxide and hydrogen
  • the product gas stream contains small amounts of carbon dioxide.
  • the reaction zone is maintained at a pressure of 600-1000 psig (col. 1, lines 58-60) .
  • the invention provides a self-contained gasification process for producing a clean gas, comprising: (a) gasifying a carbonaceous feedstock in a gasifier maintained at a temperature of from about 1650°F to about 1900°F and a pressure lower than atmospheric pressure, while maintaining excess carbon in the gasifier, to produce a gas stream; and (b) quenching and scrubbing the gas stream to provide a clean gas.
  • the process is completely self-contained and does not release any gases to the environment.
  • the control advantages realized by maintaining a reservoir of carbon in the gasifier enable gasification to be carried out efficiently at lower temperatures and pressures than known gasification processes, decreasing cost and improving safety.
  • the process does not create the problems addressed by various federal and state permit requirements, and may be exempt from those requirements.
  • the process is less expensive than conventional combustion processes, which consume fossil fuels.
  • FIG. 1 is a schematic diagram showing apparatus used to carry out a process of the invention. DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
  • the invention provides a self-contained gasification process for producing a clean gas.
  • the process involves: (a) gasifying a carbonaceous feedstock in a gasifier maintained at a temperature of from about 1650°F to about 1900°F and a pressure lower than atmospheric pressure, while maintaining excess carbon in the gasifier, to produce a gas stream; and (b) quenching and scrubbing the gas stream to provide a clean gas.
  • Suitable feedstocks that may be treated according to the disclosed process include any carbonaceous feedstocks having a sufficiently high carbon content to make the process commercially efficient.
  • the carbonaceous feedstock may be any solid or liquid hydrocarbon material such as hydrocarbon wastes, adhesives, resins, inks, petroleum by-products, paints, production debris, medical wastes, municipal sewage wastes and biochemical wastes.
  • the process is especially useful for treating hazardous wastes containing toxic organic substances. Examples of toxic materials include but are not limited to benzene, toluene, xylene, other organic solvents, and byproducts from the manufacture of plastics and coatings.
  • the carbonaceous feedstock is a waste-derived mixture prepared by waste blending.
  • various waste materials are combined so that the resulting blend has a carbon content sufficient to run the gasification process while maintain ⁇ ing excess carbon.
  • the carbonaceous feedstock will be carefully monitored to assure that no contaminants are present in the feedstock at levels that will prevent the economical production of useful products that meet industry specifi ⁇ cations.
  • feedstock blending eliminates the need to add fossil fuels such as natural gas or fuel oil to the carbonaceous feedstock. This conserves energy and reduces costs.
  • a particularly useful carbonaceous feedstock may be prepared by blending materials to provide the following feedstock composition: Feedstock Component Amount (mass fraction percent) Carbon 55 - 100%
  • a carbonaceous feedstock such as a hazardous waste-derived feedstock that has a composition within the composition limits shown above, may be gasified (in the presence of excess carbon) , quenched and scrubbed to form a clean gas without the need to vent any gases into the environment.
  • This is achieved by gasifying the carbonaceous feedstock in a gasifier maintained at a temperature of from about 1650°F to about 1900°F, preferably about 1800°F, while maintaining the gasifier chamber under a slight vacuum.
  • the temperature at which gasification is carried out affects several production variables: Production Efficiency At a temperature of about 1850°F (1000°C) , the gasification r.rocess yields maximum amounts of CO (carbon monoxide) and H 2 (hydrogen) , while the amounts of H 2 0 (water) , C0 2 (carbon dioxide) and CH 4 (methane) produced approach zero asymptotically at this temperature. Nitrogen Side Reactions
  • the bulk of the nitrogen entering t 1 - - gasifier is converted to molecular nitrogen, because of s stability.
  • Other species such as NH 3 (ammonia) and HCN (hydrogen cyanide) could be formed, however, which may cause difficulties in processing and purifying the gas stream.
  • HCN formation could be a problem, for instance, because with its high water solubility it may contaminate scrubbers.
  • NH 3 ammonia
  • HCN hydrogen cyanide
  • Chlorine Side Reactions The production of several reactive, toxic chlorine compounds such as C1CN (cyanogen chloride) , Cl 2 (chlorine) , SCI (sulfur chloride) and CH 2 Cl 2 (dichloromethane) increases exponentially at gasification temperatures above about 1742°F (950°C) . Reactive chlorine species may chlorinate residual organics during quenching to produce chlorinated organics, which must be removed in later steps.
  • C1CN cyanogen chloride
  • Cl 2 chlorine
  • SCI sulfur chloride
  • CH 2 Cl 2 dichloromethane
  • Acetylene C 2 H 2
  • Acetylene production begins just above 1652°F (900°C) and rises exponentially at higher temperatures.
  • the preferred temperature for carrying out the inventive process is about 1650°F-1900°F, most preferably about 1800°F. These temperatures maximize production of useful end-products while minimizing undesirable side reactions and contaminants.
  • the preferred temperature in the gasifier is achieved by beginning the gasification operation using natural gas as the carbonaceous feedstock and combining it in the gasifier with an oxygen feed.
  • the temperature in the gasifier is raised to the preferred level by adjusting from zero the flow rates of the natural gas and oxygen feeds that are injected into the gasifier.
  • these two feeds are added to the gasifier in combustible ratios in the presence of a spark, combustion reactions begin which are exothermic (i.e., they release heat) and which raise the internal temperature of the gasifier.
  • the gasifier temperature approaches the preferred temperature the oxygen feed rate is gradually decreased while the feed rate of natural gas is kept constant. With the substoichiometric conditions that result, generation of carbon monoxide and carbon will begin.
  • the gasifier temperature begins to drop below the desired temperature range, then the steam feed rate is decreased while maintaining a constant feed rate of the carbonaceous feedstock. If the temperature continues to drop below the desired temperature, then the oxygen feed rate is increased.
  • the gasifier temperature begins to rise above the desired temperature range, then the steam feed rate is increased while maintaining a constant feed rate of the carbonaceous feedstock. If the temperature continue-. to rise above the desired temperature, then the oxygen feed rate is decreased. If an extreme upset of high temperature occurs, then the oxygen and carbonaceous feedstock feeds are stopped while the steam feed rate is maintained or increased to sustain the preferred subatmospheric pressur-e in the gasifier. Due to the exothermic nature of the chemical reactions in the gasifier, the gasifier temperature will cease to rise when all of the feed substances in the gasifier are exhausted, causing the gasifier temperature to stabilize and begin to drop.
  • the shutdown procedure is similar to that used in the case of extreme upsets of high temperature.
  • the oxygen and carbonaceous feedstock feeds to the gasifier are stopped while the steam feed rate to the gasifier is maintained or increased to sustain the preferred subatmospheric pressure in the gasifier.
  • the steam feed to the gasifier is gradually reduced to zero while a carbon dioxide purge into the gasifier is started.
  • a gasifier pressure less than atmospheric pressure is used in carrying out the process.
  • the subatmospheric pressure in the gasifier is maintained by equipment on the gas process stream downstream of the gasifier gas outlet.
  • This device a steam jet ejector vacuum pump, sucks the product gases out of the gasifier and can be controlled to maintain the desired subatmospheric pressure in the gasifier.
  • the pressure in the gasifier is from about -1 to -10 inches water column pressure, most preferably about -5 inches water column pressure. If the gasifier chamber is not maintained under a vacuum, the system will not be totally contained and gases may be vented into the environment.
  • the disclosed process is designed so that all gases and vapors either become part of the product or recirculate through the system to prevent gaseous releases. Therefore, the only by-products exiting the system are gasifier residue and metal salts consisting of dry inorganic solids and fixed carbon. These solids may be raked into a totally-enclosed holding vessel for transfer to an appropriate facility. Inorganic solids and/or fixed carbon remaining in the clean gas when it leaves the gasifier are preferably stripped in a venturi scrubber unit and reinserted into the gasifier through the gasifier injection nozzle. A wet scrubber using water and magnesium hydroxide is preferably used to strip the metals and hydrogen chloride in the gasifier effluent. The resulting concentrated brine solution may be blown down and dried in a crystallizer using superheated steam. The metal salts are preferably transferred to an appropriate facility while the saturated steam may be recirculated into the quencher.
  • a shift reactor (described below) is preferably used to convert the gas stream into compressed carbon dioxide and liquid hydrogen.
  • a major commercial use for compressed carbon dioxide is as a supercritical fluid for enhanced oil recovery in the petroleum industry.
  • Liquid hydrogen is used in the petroleum industry in the production of reformulated gasoline and in hydrotreating to reduce the sulfur content of a refined product.
  • equipment other than a shift reactor may be used to convert the gas stream into other products.
  • different types of reactors may be used to convert the gas stream into CH 3 OH (methanol) or NH 3 (ammonia) . Further details and preferred equipment for carrying out embodiments of the process will be described with reference to the accompanying drawing.
  • FIG. 1 a schematic block flow diagram is shown, illustrating an exemplary preferred apparatus and process flows for the gasification process.
  • underlined numbers refer to components while numbers inside diamonds refer to flows described in Tables 1-6.
  • the dashed line boxes encloiu self-contained processes.
  • the preferred apparatus includes gasifier 2, quencher 4, venturi scrubber 6, wet scrubber 8, steam- jacketed evaporator/water-cooled flaker 10, polisher caustic scrubber 12, shift reactor section 14 comprising shift reactor gas-to-gas heat exchanger 16, steam jet ejector 22, shift reactor catalyst first bed 18, and shift reactor catalyst second bed 20, compressor section 24 comprising multistage blower (vacuum pump) 26, turboblower compressor 28 and reciprocating compressor 30, gas separation unit 32 and steam plant 34.
  • gasifier 2 quencher 4
  • venturi scrubber 6 wet scrubber 8
  • steam- jacketed evaporator/water-cooled flaker 10 polisher caustic scrubber
  • shift reactor section 14 comprising shift reactor gas-to-gas heat exchanger
  • Gasifier 2 may be a metallic vertical cylinder constructed to withstand the temperatures, pressures, and corrosive conditions of the process. Refractory materials are used for the gasifier lining (as opposed to the use of other materials such as a cold wall) since incandescent refractory materials help catalyze and promote the oxidation reactions occurring in the gasifier.
  • the gasifier may have a carbon steel jacket which is also insulated. Heat transfer fluid may flow through this jacket.
  • a third shell is preferably provided on gasifier 2, outside the jacket's insulation, which serves as a containment shell.
  • the outer shell is preferably made of stainless steel.
  • gasifier residue rake sweeps any gasifier residue that collects in the gasifier into a jacketed screw, which cools and transfers the gasifier residue into a collection hopper.
  • Low pressure steam is injected into the hopper to further cool the gasifier residue and to remove any remaining volatile materials from the gasifier residue.
  • the steam may be provided by a conventional steam plant 34.
  • the steam (and any volatile materials) pass up through the jacketed screw into the gasifier.
  • An injection nozzle is used to introduce the carbonaceous feedstock (such as hazardous waste-derived feedstock) , oxygen and steam into gasifier 2.
  • the purpose of the gasifier is to mix the reactants - carbonaceous feedstock, oxygen, and steam - at high temperature and gasify them.
  • the feedstock a mixture of organic compounds wxth some inorganic constituents, is pyrolyzed into molecular form. Carbon, hydrogen, oxygen, and various inorganic molecules such as metals and chlorine are produced.
  • the steam that is added to the gasifier is reformed into oxygen and hydrogen.
  • incandescent carbon from the pyrolized feedstock contacts oxygen pyrolized from the feedstock, reformed from the steam, and present from the oxygen feed stream, competing reactions produce carbon dioxide and carbon monoxide.
  • the thermodynamic properties of the reactants and products are such that the carbon monoxide content of the gases produced is maximized and the carbon dioxide content is minimized.
  • most of the hydrogen from the pyrolized feedstock and the reformed steam leaves the gasifier as hydrogen and does not react. Some hydrogen is consumed by any chlorine present and leaves the reactor as hydrogen chloride.
  • Normal operating temperature inside the gasifier is about 1650°F-1900°F, preferably about 1800°F, while normal operating pressure is slightly below atmospheric pressure. A gasifier pressure of about minus five inches water column pressure is preferred.
  • the gasifier temperature is maintained by heat addition from the exothermic reactions of oxygen with the carbonaceous feedstock and incandescent carbon balanced by heat removal through the endothermic reformer reaction of the steam with the incandescent carbon. The presence of the incandescent carbon is required to maintain this balance.
  • Gasifier residue is preferably removed through the bottom of gasifier 2 and collected in a gasifier residue holding vessel (not shown) where it is thereafter transferred to a gasifier residue transfer container (not shown) for appropriate disposal.
  • the carbon monoxide/hydrogen stream that leaves the gasifier is first cooled to an intermediate temperature in quencher 4 to quickly stop all gasification reactions.
  • the quencher is preferably attached to the gasifier via a duct.
  • Quencher 4 is a cylindrical duct that may be constructed of one or more metallic and polymeric material(s) that withstand(s) the temperatures, pressures, and corrosive conditions of the process gas stream.
  • the quencher may or may not have a cooling jacket. Thermal fluid may flow through the jacket to remove heat from the quencher.
  • the outside of the jacket may be insulated.
  • the carbon monoxide/hydrogen stream is cooled from about 1800°F to below 250°F in the quencher. From the quencher, the cooled gas stream is transferred to venturi scrubber 6. Venturi Scrubber
  • the venturi scrubber 6 is used to remove contaminants from the carbon monoxide/hydrogen stream exiting the quencher. These contaminants consist of particulates of gasifier residue and carbon char.
  • a liquid is used in the venturi scrubber which may be either an aqueous solution or a hydrocarbon oil solution. As contaminants trapped in the venturi scrubber build up in the solution, part of the solution is removed, or blown down, from the venturi scrubber and injected into the gasifier. New solution is added to the venturi scrubber to replace the removed solution.
  • Wet Scrubber The wet scrubber 8 is used to remove hydrogen chloride and other acid gas contaminants from the carbon monoxide/hydrogen stream exiting the venturi scrubber.
  • a basic solution preferably magnesium hydroxide, is used to turn the hydrogen chloride and other acid gases into solid salts such as magnesium chloride. These salts are trapped in the wet scrubber's basic solution. As the basic solution becomes saturated with salts, part of the solution is removed, or blown down, from the wet scrubber and treated in an off-line evaporator/flaker. As the hydroxide portion of the basic solution is exhausted (through reaction with hydrogen chloride and other acid gases) new hydroxide is added to the basic solution. Due to the cooling action of the wet scrubber, water is vaporized from the wet scrubber basic solution into the gas stream. As a result, additional water is added to the basic solution as needed. This water originates in the steam plant 34. Steam-Jacketed Evaporator/Water-Cooled Flaker
  • a steam-jacketed evaporator with water-cooled flaker 10 is used to treat the blown down salt solution from the wet scrubber.
  • the salt solution is heated in the evaporator to drive off (as steam) excess water from the salt solution.
  • the steam is either injected into the gasifier or condensed and added to the quencher. After the excess water is removed from the salt solution, the salt is cooled and solidified in the flaker.
  • Polisher - Caustic for Amine) Scrubber A polisher 12 is used as a final cleaning device to treat the carbon monoxide/hydrogen stream from the wet scrubber.
  • Either an aqueous sodium hydroxide solution (caustic) or a liquid a ine solution is used in the polisher to remove any traces of contaminants such as hydrogen chloride.
  • a packed column or a tray tower is used to provide optimum mixing between the gas stream and the liquid solution.
  • the shift reactor section 14 consists of a shift reactor gas-to-gas heat exchanger 16, a steam jet ejector (vacuum pump) 22, a shift reactor catalyst first bed 18, and a shift reactor catalyst second bed 20.
  • the shift reactor section is one option for converting the cleaned carbon monoxide/hydrogen gas stream into commercial products.
  • the gas stream is converted into a carbon dioxide/hydrogen stream using steam as a co-reactant with the carbon monoxide/hydrogen stream from the polisher.
  • Shift reactions promoted by a shift reactor catalyst operate at elevated temperatures.
  • the shift reactor gas-to-gas heat exchanger 16 heats the cold gas stream from the polisher prior to entering the first shift reactor catalyst bed.
  • the steam jet ejector (vacuum pump) 22 is used downstream of the shift reactor heat exchanger for two reasons: (1) to provide the pumping action needed to propel the carbon monoxide/hydrogen gas stream from the gasifier downstream through the quencher, the gas cleaning operations, and through the shift reactor heat exchanger; and (2) to add the appropriate amount of the co-reactant steam needed in the shift reactor catalyst beds.
  • the steam jet ejector raises the pressure of the gas stream from well below atmospheric pressure at its inlet to just below atmospheric pressure at its outlet.
  • the shift reactor catalyst first bed 18 consists of an enclosed vessel containing a fixed bed of solid shift reactor catalyst beads. In the bed, a portion of the carbon monoxide from the carbon monoxide/hydrogen gas stream reacts with water vapor present in that stream as well as with the steam added in the steam jet ejector. The products of this reaction are carbon dioxide and hydrogen. Since the reaction is exothermic, the gas stream leaving the first bed must be cooled before entering a second bed. This cooling is done using the shift reactor gas-to-gas heat exchanger 16.
  • the shift reactor catalyst second bed 20 is similar to the first bed and is used to convert additional carbon monoxide and water into carbon dioxide and hydrogen. Compression Section
  • the compression section 24 consists of multistage blower (vacuum pump) 26 with precondenser and postcondenser, a turboblower compressor 28 with postcondenser, and a reciprocating compressor 30 with intercoolers and aftercooler.
  • This section serves two functions: (l) to raise the pressure of the carbon dioxide/hydrogen gas stream leaving the shift reactor section; and (2) to cool and _emove condensed water vapor from this compressed carbon dioxide/hydrogen gas stream.
  • the multistage blower provides the pumping action needed to propel the gas stream from steam jet ejector outlet downstream through the shift reactor first bed, the shift reactor gas-to-gas heat exchanger, the shift reactor second bed, and the multistage blower (vacuum pump) precondenser.
  • the multistage blower raises the pressure of the carbon dioxide/hydrogen gas stream from well below atmospheric pressure to just below atmospheric pressure.
  • the precondenser and postcondenser for the multistage blower (vacuum pump) remove water from the gas stream by cooling the gas stream using noncontact heat exchangers cooled with cooling water.
  • the condensate from these condensers is supplied to the steam plant 34 where it is used to either (1) generate steam needed for addition to the gasifier or the steam jet ejector, or (2) make up part of the water needed for addition to the quencher or wet scrubber.
  • the turboblower compressor 28 with postcondenser is used to raise the pressure of the carbon dioxide/hydrogen gas stream from the multistage blower (vacuum pump) postcondenser from just below atmospheric pressure to a positive pressure of between 15 and 60 psig.
  • the turboblower postcondenser removes water from the gas stream by cooling the gas stream using a noncontact heat exchanger cooled with cooling water.
  • the condensate from this condenser is supplied to the steam plant 34 where it is used to either (1) generate steam needed for addition to the gasifier or the steam jet ejector, or (2) make up part of the water needed for addition to the quencher or wet scrubber.
  • a reciprocating compressor 30 with intercoolers and aftercooler is used to raise the pressure of the carbon dioxide/hydrogen gas stream from the turboblower compressor postcondenser from the postcondenser's outlet pressure of 15 to 60 psig to approximately 450 psig.
  • the reciprocating compressor's intercoolers and aftercooler remove water from the gas stream by cooling the gas stream using noncontact heat exchangers cooled with cooling water.
  • the condensate from these coolers is supplied to the steam plant where it is used to either (1) generate steam needed for addition to the gasifier or the steam jet ejector, or (2) make up part of the water needed for addition to the quencher or wet scrubber.
  • the gas separation unit 32 separates the carbon dioxide/hydrogen gas stream into two streams: (1) pure hydrogen, and (2) carbon dioxide.
  • a pressure swing adsorption (PSA) gas separation unit is used to accomplish this separation.
  • the pure hydrogen stream is liquified in a hydrogen liquefaction unit, while the carbon dioxide stream, which exits the PSA unit at low pressure, is compressed in a reciprocating compressor equipped with intercoolers and an aftercooler.
  • the reciprocating compressor's intercoolers and aftercooler remove water from the gas stream by cooling the gas stream using noncontact heat exchangers cooled with cooling water.
  • the condensate from these coolers is supplied to the steam plant where it is used to either (1) generate steam needed for addition to the gasifier or the steam jet ejector, or (2) make up part of the water needed for addition to the quencher or wet scrubber.
  • the liquid hydrogen and compressed carbon dioxide from the gas separation unit may be stored and shipped for commercial use in any convenient manner (e.g., tank trucks, pipelines, etc.).
  • a typical carbonaceous feedstock (such as one which could be derived from hazardous waste, for example) is prepared by blending materials to produce a feedstock having the following approximate composition:
  • Component Amount (mass fraction percent)
  • the feedstock is sprayed into gasifier 2, which is maintained at a temperature of about 1800°F and pressure of about -5 inches water column pressure.
  • the gas stream produced in the gasifier is then passed through the remaining apparatus shown in FIG. 1 as described above.
  • the solid/liquid/vapor state, mass flowrate, temperature, pressure, vapor flowrate and composition of the gas stream at the various flow number positions are described in the Tables 1-6 below.
  • MASS FLOWRATE (LB./M1N.) 185 - 23 134 5 337 199 536
  • VAPOR FLOWRATE (ACFM) 32,800 16,400
  • MASS FLOWRATE (LB./MIN.) 0.01 543 543 592 1135 1135 1135 1135 1135 1135
  • VAPOR FLOWRATE (ACFM) 21,800 43,100 55,000 84,800 71,400 101,700 f-
  • MASS FLOWRATE (LB./MIN.) 335 800 800 253 548 548 21 527
  • VAPOR FLOWRATE (ACFM) 37,000 23,100 13,400 8,290 5,840
  • MASS FLOWRATE (LB./MIN.) 15 512 30 482 30 1 482 7
  • VAPOR FLOWRATE (ACFM) 388 201 2,500 156
  • the process produces liquid hydrogen and compressed carbon dioxide in commercially useful amounts. These useful products have purities that are acceptable for immediate commercial sale. The products are produced at a cost that makes sale of the C0 2 and hydrogen economically viable. All gaseous products produced by the process are either converted into carbon dioxide and hydrogen for commercial sale or are recycled back into the gasification process. No gases are released into the environment.

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Abstract

L'invention se rapporte à un procédé de gazéification autonome conçu pour produire un gaz pur à partir d'une charge carbonée, telle qu'une charge dérivée de déchets dangereux. Le procédé consiste à gazéifier une charge carbonée dans un gazéificateur (2) maintenue à une température d'environ 1 650 °F et à une pression inférieure à la pression atmosphérique, tout en conservant un excédent de carbone dans le gazéificateur, afin de produire un courant gazeux, puis à refroidir et à épurer le courant gazeux (4, 6, 8) afin d'obtenir un gaz pur. Aucun gaz d'effluent n'est libéré dans l'environnement. L'invention se rapporte également à un procédé (32) économique et sans danger pour l'environnement qui permet d'obtenir à partir d'un gaz pur des produits à usage commercial.
PCT/US1995/000105 1994-01-14 1995-01-05 Procede de gazeification autonome Ceased WO1995019407A1 (fr)

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AU15586/95A AU1558695A (en) 1994-01-14 1995-01-05 Self-contained gasification process

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US08/181,030 1994-01-14

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006109294A1 (fr) * 2005-04-12 2006-10-19 C. En. Limited Systemes et procedes pour la production d’hydrogene

Citations (7)

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Publication number Priority date Publication date Assignee Title
US1799885A (en) * 1924-02-13 1931-04-07 Chavanne Louis Process of generating producer gas
US3671209A (en) * 1970-12-21 1972-06-20 Texaco Development Corp Garbage disposal process
US3687646A (en) * 1970-12-21 1972-08-29 Texaco Development Corp Sewage disposal process
US4530702A (en) * 1980-08-14 1985-07-23 Pyrenco, Inc. Method for producing fuel gas from organic material, capable of self-sustaining operation
US4728341A (en) * 1981-10-26 1988-03-01 Nielsen Jay P Method for treating, in transit, hydrocarbon gases containing carbon dioxide and potential atmospheric pollutants
US4950309A (en) * 1987-10-07 1990-08-21 Dynecology Incorporated Process for the conversion of toxic organic substances to useful products
US5104419A (en) * 1990-02-28 1992-04-14 Funk Harald F Solid waste refining and conversion to methanol

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1799885A (en) * 1924-02-13 1931-04-07 Chavanne Louis Process of generating producer gas
US3671209A (en) * 1970-12-21 1972-06-20 Texaco Development Corp Garbage disposal process
US3687646A (en) * 1970-12-21 1972-08-29 Texaco Development Corp Sewage disposal process
US4530702A (en) * 1980-08-14 1985-07-23 Pyrenco, Inc. Method for producing fuel gas from organic material, capable of self-sustaining operation
US4728341A (en) * 1981-10-26 1988-03-01 Nielsen Jay P Method for treating, in transit, hydrocarbon gases containing carbon dioxide and potential atmospheric pollutants
US4950309A (en) * 1987-10-07 1990-08-21 Dynecology Incorporated Process for the conversion of toxic organic substances to useful products
US5104419A (en) * 1990-02-28 1992-04-14 Funk Harald F Solid waste refining and conversion to methanol

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006109294A1 (fr) * 2005-04-12 2006-10-19 C. En. Limited Systemes et procedes pour la production d’hydrogene

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