WO2010068139A1 - Procédé de traitement de produits contenant du carbone et/ou des hydrocarbures et réacteur pour sa mise en œuvre - Google Patents

Procédé de traitement de produits contenant du carbone et/ou des hydrocarbures et réacteur pour sa mise en œuvre Download PDF

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Publication number
WO2010068139A1
WO2010068139A1 PCT/RU2009/000675 RU2009000675W WO2010068139A1 WO 2010068139 A1 WO2010068139 A1 WO 2010068139A1 RU 2009000675 W RU2009000675 W RU 2009000675W WO 2010068139 A1 WO2010068139 A1 WO 2010068139A1
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zone
reactor
synthesis
hydrogenation
temperature
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PCT/RU2009/000675
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English (en)
Russian (ru)
Inventor
Максим Викторович АНИГУРКИН
Асланбек Хажмурадович АРСАМАКОВ
Грачья Пайлакович БАДАЛЯН
Денис Игоревич ДОЛМАТОВ
Алексей Васильевич ЕРУСЛAHOB
Вячеслав Александрович ПАНФИЛОВ
Павел Вениаминович ПОЛЯКОВ
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Закрытое Акционерное Общество Научно-Производственная Компания "Интергаз"
Общество С Ограниченной Ответственностью "Мировые Экологические Стандарты"
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Publication of WO2010068139A1 publication Critical patent/WO2010068139A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/06—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated according to the moving bed type
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the invention relates to the field of industrial processing of carbon- and hydrocarbon-containing products and can be used, in particular, for processing a variety of industrial and household waste, for processing low-quality combustible minerals, such as, for example, brown coal, oil shale, and the like.
  • a known method of processing solid domestic waste by gasification implemented in a reactor with refractory lining with a length of 1600 mm and an inner diameter of 250 mm, for which a gasifying agent containing oxygen is fed countercurrently into a vertical shaft furnace, the wastes (usually mixed with lumpy fuel) are sequentially stay in the heating and drying zone, the pyrolysis zone, the combustion (oxidation) zone and the cooling zone, while the maximum temperature in the reactor is maintained within 700-1400 0 C by adjusting at least m
  • the mass fraction of oxygen in the gasifying agent and / or the mass fraction of non-combustible material in the waste and / or the mass fraction of combustible material in the waste the process being carried out periodically, for which the waste is loaded and the solid products are unloaded after shutting down the reactor [Description of the invention to the patent RF N ° 2079051 dated 1994.06.23, IPC F23G5 / 027, publ. 1997.05.10].
  • the disadvantage of this method is the high specific consumption of the oxidizing gas, which leads to the formation of an excessive amount of oxides and acid components in the product gas and the need to load additional solid lump fuel in the case of a low calorific value of the processed product, as well as its low productivity.
  • a known method of processing combustible solid household waste which is a modification of the method according to the patent of the Russian Federation N ° 2079051, the difference of which is that the temperature in the reactor is maintained in the range from 800 to 1300 0 C, is used as a gasifying agent, mainly in a mixture with air, and the steam released during drying is included in the composition of the gasification agent [Description of the invention to RF patent N ° 2150045 from 1998.01.22, IPC 7 F23G5 / 027, publ. 2000.05.27].
  • the method provides the processing of solid waste without supplying heat from the outside with high energy efficiency, high yield of valuable products, including pyrolysis resins and combustible gas, and high overall energy efficiency of the process.
  • a known method of processing condensed fuels which is a modification of the method according to RF patent N ° 2079051, for which a charge consisting of combustible components and a lump of solid non-combustible material is loaded into the reactor, a gas flow is established through the charge with the supply of a gasifying agent with oxygen, steam and carbon dioxide, the products of processing are removed from the reactor, where successive sections of the aforementioned charge are sequentially located in the zones of heating, pyrolysis, coking, gasification and cooling Regulate the temperature in the combustion zone ranges from 800 to 1300 0 C, was discharged from the reactor solid products, burn at least part of the gaseous, while as a gasifying agent used in the flue gas is mixed with air and steam, wherein the process control is carried out a change in the fraction of flue gas in the gasification agent [Description of the invention to the patent of the Russian Federation ⁇ Ns 2152561 from 1998.01.22, IPC 7 F23G5 / 027, publ.
  • the disadvantage of this method is the excess amount of chemically unbound carbon in the solid residue at the outlet of the reactor, the high content of water, oxides and acid components in the product gas, which reduces the efficiency of its further use, as well as its low productivity.
  • a known method of disposal and destruction of solid waste, mainly hospital, containing combustible materials including loading the waste into the gasification chamber, their initial ignition with the formation of a gasification zone, supplying a gasifying agent to it, moving the waste through the chamber, carrying out pyrolysis with a relative lack of air and subsequent afterburning pyrolysis products in the afterburning chamber with excess air, regulating the air supply depending on the temperatures in the gasification and afterburning chambers, at the withdrawal of gaseous gasification products is carried out directly from the gasification zone at a temperature not lower than 800 0 C and provide heat to the gasification zone by heating the walls of the gasification chamber with exhaust gases at a temperature in the range 800-1200 0 C [Description of the invention to RF patent JNo 2089786 from 1994.06.06 .23, IPC 6 F23G5 / 00, publ. 1997.09.10].
  • the disadvantage of this method is the high specific consumption of the oxidizing gas, the high temperature of the product gas at the outlet of the gasification chamber, the formation of an excessive amount of oxides and acid components in the gas at the outlet of the afterburner, the need for an additional heating source in the case of low calorific value and high humidity of the charge product to initiate and maintain the gasification process, as well as its low productivity.
  • the method is characterized by low productivity and the impossibility of implementation in industrial volumes.
  • a known method of processing worn tires including thermal decomposition at 400-600 0 C with the formation of gas and vapor products and a solid carbon residue, their separation into liquid and vapor phases and a solid carbon residue, separation of the liquid phase into light and heavy fractions, grinding of the carbon residue, granulation of the carbon residue using a wetting liquid, carbonization of the carbon residue, and the gases and light resins formed in the proposed process are fed to the combustion furnaces of the reactor, carbonizer and activator [Description of the invention to the patent of the Russian Federation Jvfe 2142357 from 1998.07.03, IPC 6 . B29B17 / 00, CÜGl / 10, C08J11 / 02, publ. 1999.12.10].
  • the method reduces the volume and spectrum of emissions from the process of processing used tires.
  • the disadvantage of this method is its lack of performance and the need to burn its own pyrolysis gases and light resins to maintain the thermal regime of the reactor, which leads to a high consumption of oxidizing gas and the formation of an excessive amount of oxides and acid components.
  • the disadvantage of this method is the need to use water or carbon dioxide in the composition of the gasification agent, as well as the need to introduce water into the combustion and / or cooling zone to control the thermal regime, which leads to additional heat costs and a decrease in the calorific value of the product gas at the outlet of the reactor, and also the formation of an excessive amount of oxides and acid components in the product gas due to the excessively high temperature in the combustion zone.
  • the method includes a high-temperature layer-by-layer treatment of waste in the reactor, when an oxygen-containing agent and water vapor are supplied, burning part of the waste, pyrolysis of combustible waste constituents with the formation of gas-vapor products with a predominant content of hydrocarbons and solid residues, their cooling, removal and removal from the reactor working zone.
  • the disadvantages of the method is the necessity of using water as a part of the gasification agent, which leads to additional costs heat and reduce the calorific value of the product gas at the outlet of the reactor, the need to load additional solid lump fuel in the case of a low calorific value of the processed product, as well as increased oxygen consumption in the gasification agent and the formation of excessive oxides and acid components during product gas combustion.
  • the method is implemented at the level of a laboratory experiment, which makes it impossible to evaluate its potential and technological features.
  • the problem to be solved by the first invention of the group and the technical result achieved is to create another environmentally friendly high-performance method for high-temperature processing of combustible carbon and / or hydrocarbon-containing products, reduce its energy capacity, expand technological capabilities in terms of controlling the chemical composition and increasing the yield of products ready for further use as well as improving their quality.
  • the nozzle further comprises chemically unbound carbon
  • the nozzle is made of fly ash containing chemically unbound carbon.
  • a reactor for processing combustible carbon and hydrocarbon-containing wastes is a batch or continuous-cycle device for the environmentally friendly disposal of oil waste or sludge and other wastes
  • a sealed working chamber equipped with appropriate instrumentation with located p working areas: unloading solid processing residues with an unloading window, supplying air and water vapor, heating air and water vapor, burning, coking, pyrolysis, heating waste, selection of combined-cycle products with at least one waste collection and loading channel with a gateway, moreover, each zone is equipped with temperature sensors, and the air supply and selection of combined-cycle products are equipped with pressure sensors.
  • This device has the same disadvantages as the method implemented on it.
  • the problem solved by the second invention of the group and the technical result achieved are to create an economical reactor that implements an environmentally friendly high-performance method of processing ki of combustible carbon and / or hydrocarbon-containing products according to the first invention, which provides a reduction in the energy capacity of the process, expansion of technological capabilities in the process of high-temperature waste treatment, increase the yield of products ready for further use and improve their quality.
  • the reactor for processing combustible carbon and / or hydrocarbon-containing products includes a sealed working chamber with working zones located in the technological sequence: unloading solid processing residues with an unloading window, air and water vapor through the corresponding channels, heating of air and water vapor, combustion, coking and pyrolysis, heating of processed products, selection of a gas-vapor mixture with at least one channel ohm of selection, and a loading zone of processed products with a gateway, with each zone equipped with at least one temperature sensor, and the heating zones of air and water vapor, and selection of the gas-vapor mixture are equipped with pressure sensors, while the working chamber contains a zone equipped with additional temperature sensors synthesis and hydrogenation of hydrocarbons located directly behind the coking and pyrolysis zone.
  • the zone of synthesis and hydrogenation of hydrocarbons is configured to maintain a working temperature of 250-400 0 C;
  • the zone of synthesis and hydrogenation of hydrocarbons is equipped with at least two channels of additional hydrogen supply located at different levels.
  • FIG. 1 shows the design of a reactor for the processing of combustible carbon and / or hydrocarbon-containing waste - a general view
  • FIG. 2 shows a distribution diagram of characteristic work areas in the reactor.
  • a method of processing combustible carbon and / or hydrocarbon-containing products is implemented on the appropriate equipment — in a reactor, which includes a sealed heat-insulated working chamber 1 with working zones located in the technological sequence: unloading solid processing residues — 2 with a discharge window 3; air supply and water vapor - 4 through channels 5; heating air and water vapor - 6; burning - 7; coking and pyrolysis - 8; heating of processed products - 9; selection of the gas-vapor mixture - 10 s, at least one channel 11 of its selection; and a zone 12 for loading processed products with a gateway (not shown conventionally), each zone being equipped with at least one temperature sensor 13 of a corresponding design, and a zone for heating air and water vapor — 6, and a selection of gas-vapor mixture — 10 (intersects with the zone 12 download processing products) - equipped with pressure sensors 14, while the working chamber 1 contains equipped with temperature sensors 15 zone 16 synthesis and hydrogenation of hydrocarbons located directly behind zone 8 of coking and pyr
  • the described reactor implements a method for the high-temperature processing of carbon and / or hydrocarbon-containing products in the presence of a nozzle with the supply of oxygen-containing a burning agent and water vapor, burning, coking and pyrolysis of their combustible components, the formation of a gas-vapor mixture and solid residues, their cooling, removal and removal from the working space of the reactor through channels 11, while synthesis zone 16 is formed directly behind coking and pyrolysis zone 8 and hydrogenation of hydrocarbons with a temperature of 250-400 0 C, a temperature of 900-1300 0 C is maintained in the combustion zone 7, chemically unbound carbon is emitted in the coking and pyrolysis zone 8, which is treated with steam in the combustion zone 7 with the formation of free hydrogen supplied to the zone of synthesis and hydrogenation of hydrocarbons - 16, sequentially carrying out their synthesis (conditional element 19 of zone 16) and hydrogenation (conditional element 20 of zone 16), while in the working space of the reactor form a vacuum and the process is carried out in
  • combustion zone 7 eliminates the formation of nitrogen oxides, while the lower temperature limit of 85O 0 C ensures guaranteed combustion of the processed products.
  • a lower combustion temperature makes the process of hydrogen formation in the combustion zone 7 unstable or even impossible as a result of the reaction of the interaction of carbon with water.
  • Such active nozzles may include waste from the concentration of iron ore deposits, solid waste from thermal stations operating on solid fuel, and other similar products containing metallic inclusions that can act as catalysts.
  • Zone 8 of coking and pyrolysis is certainly not divided into conditional zones — the coking zone and the pyrolysis zone — for the reason that, depending on the processed raw materials, their size and, accordingly, the ratio can vary within very wide limits, for example, for the case of processing solid household the waste pyrolysis zone will dominate the coking zone, and in the case of the processing of automobile tires - vice versa.
  • the decarburized residue of the processed products and the decarburized nozzle are removed from the reactor and can be used for a special purpose, for example, for the manufacture of building mixtures, etc.
  • An industrial reactor designed for the continuous processing of a variety of combustible carbon and hydrocarbon-containing products has a significant advantage over its conventionally called “laboratory” samples of small sizes - in it, due to the large surface area of the zones, it becomes impossible to clog the reactor’s internal section with various plastic ones ( resinous) substances of pyrolysis products - they simply do not have time to merge into a single volume. In this way, a situation of unhindered passage of reactor gases over the entire height of the reactor becomes possible.
  • the organized process of processing raw materials allowed the formation of a pressure of the order of 500-5000 Pa (50-500 mm water column) inside the reactor, which eliminates the ingress of decomposition and synthesis products into the environment.
  • the claimed process can be considered environmentally friendly.
  • a method for processing combustible carbon and hydrocarbon-containing products can be implemented in a reactor, the working chamber of which, unlike typical reactors (see the prior art), contains a zone 16 for the synthesis and hydrogenation of hydrocarbons located directly behind zone 8 of pyrolysis and coking.
  • the location of the indicated zone 16 is marked on the reactor with the corresponding conclusions of the temperature sensors 15. In zone 8, complete or partial coking of the processed products
  • a situation is possible where, to obtain additional hydrogen, it is possible to use a nozzle containing chemically unbound carbon (and metals - catalysts) in advance, which can be used in the combustion zone 7 for the reaction of interaction with water to occur. It is possible to make such a nozzle from fly ash, for example, TPP, by decarburizing it in the reactor for the purpose of further independent processing.
  • the gas-vapor mixture contains pyrolysis and synthesis products such as isoprene, dipentene, C 4 -C 8 hydrocarbons that make up the gasoline fraction, C 9 -Ci 2 hydrocarbons that make up the kerosene fraction and light gas oil fraction, as well as entrained gas in the form of drops, high-boiling compounds and other substances, the composition of which depends on the feedstock and the catalysts used.
  • pyrolysis and synthesis products such as isoprene, dipentene, C 4 -C 8 hydrocarbons that make up the gasoline fraction, C 9 -Ci 2 hydrocarbons that make up the kerosene fraction and light gas oil fraction, as well as entrained gas in the form of drops, high-boiling compounds and other substances, the composition of which depends on the feedstock and the catalysts used.
  • the listed products are removed from the reactor through the appropriate selection channels 11 for direct use or subsequent processing.
  • a method for processing combustible carbon- and hydrocarbon-containing products will first be considered for the case of their loading into a continuous reactor and their further movement from top to bottom with the complete decomposition of high molecular weight organic compounds and the conversion of carbon-containing inorganic to carbon monoxide and hydrogen with the inert components unchanged and further sequential synthesis of hydrocarbons from the obtained carbon monoxide and hydrogen and their further hydrogenation with the acquisition of specified chemical voystv.
  • Such a presentation of information on inventions will most fully illustrate the operation of the reactor.
  • Processing products with a nozzle containing a catalyst (iron, iron oxides, etc.) through the gateway enter the zone 12 of the reactor load with temperature of 20-50 ° C and sequentially pass zone 9 of the heating of the processed products (which includes the zone 10 of the selection of the gas mixture) with a temperature of 150-250 0 C, zone 16 of the synthesis and hydrogenation of hydrocarbons with a temperature of 250-400 0 C, zone 8 of pyrolysis coking with a temperature of 350-850 0 C, combustion zone 7 with a temperature of 850 -1300 0 C, heating zone 6 involved in the process of processing air and steam to a temperature of 800-1000 0 C 5 zone 4 of air and steam with a temperature of 20-140 0 C, and zone 2 of the discharge of solid processing residues with a temperature of 20-60 0 C.
  • zone 9 of the heating of the processed products (which includes the zone 10 of the selection of the gas mixture) with a temperature of 150-250 0 C, zone 16 of the synthesis and hydrogenation of hydro
  • zone 8 of pyrolysis and coking the processed products are decomposed into constituent unstructured hydrocarbon fragments, which rise up and give up heat to the newly incoming processed products and fall into zone 16 of the synthesis and hydrogenation of hydrocarbons, forming mainly saturated (saturated hydrocarbons). If necessary, additional hydrogen is supplied to the synthesis and hydrogenation zone 16 from the outside. After all the planned processes have passed, the resulting vapor-gas mixture containing droplets of high-boiling liquid is cooled, giving heat to the loaded solid waste and, with a temperature of 190-240 0 C, is removed outside the reactor for further processing.
  • a mixture consisting of 1600 kg / h of cut pieces of tires made of isoprene rubber with linear dimensions of 20-100 mm and 1600 kg / h of nozzles with linear dimensions of 25-100 mm containing a catalyst in the form of iron and iron oxides is fed into a continuous reactor.
  • the quantitative composition of the components included in tires made of isoprene rubber the following, kg / h: isoprene rubber - 776; metal cord - (stainless steel type Xl 8Hl OT) - 310; chemically unbound carbon - 310; oxygen adsorbed - 30; hydrogen adsorbed - 10; softeners (vegetable oils, wax, higher acids) - 128; sulfur - 30; metal oxides - 6.
  • the quantitative composition of the components included in the nozzle is as follows, kg / h: chamotte -1550; catalyst (iron, magnetite, hematite) - 50.
  • air is supplied to the corresponding zone of the reactor in an amount of 2300 nm / h or 2967 kg / h, including nitrogen - 2255 kg / h and oxygen - 712 kg / h.
  • the temperature in the combustion zone does not exceed 1100 0 C.
  • zone 16 of the synthesis and hydrogenation of hydrocarbons serves hydrogen in an amount of about 60 kg / h.
  • the gas-vapor products leaving the reactor with a temperature of 24O 0 C and the hydrocarbons contained in them are separated into liquid and gas components, which is carried out sequentially in a cyclone and condensers cooled by water with an initial temperature of about 18 0 C.
  • the gas component the amount of which will be 3598 kg / h, will have the following composition,% of the mass:
  • the liquid component the amount of which was 870 kg / h, has the following composition,% of the mass:
  • the output stream of solid residues from the discharge zone of the reactor amounted to 1936 kg / h in quantity and its structure includes: nozzle - 1600; metal cord - 320; carbon-containing (soot) - 10; metal oxides - 6.
  • a mixture consisting of 1,600 kg / h of cut pieces of tires made of isoprene rubber with linear dimensions of 20-100 mm and 1,600 kg / h of nozzle is fed into a continuous reactor.
  • the difference 19 is in the qualitative composition of the nozzle - its only component is chamotte, which has linear dimensions of 25-100 mm, while no catalyst in the packing.
  • air is also fed into the reactor in an amount of 2300 nmVh.
  • the temperature in the combustion zone is not higher than 1100 0 C.
  • the gas-vapor products leaving the reactor with a temperature of 200 ° C and the hydrocarbons contained in it are separated into liquid and gas components.
  • the gas component the amount of which is 3889 kg / h, has the following composition,% of the mass:
  • the liquid component After the condensation system, the liquid component, the amount of which is 320 kg / h, has the following composition by chromatographic analysis,% of the mass:
  • the output stream of solid residues from the discharge zone of the reactor is similar in quantity to Example 1.
  • the feedstock for processing in the reactor is household waste with a density of 200-300 kg / m 3 , including the following components,% of the mass: paper - 47.0; food waste - 29.0; textile - 5.0; glass and stones - 4.9; metal - 4.5; plastic - 2.0; leather and rubber - 1.8; wood - 1.0; bones - 0.5; screening less than 15 mm - 4.5; other - 0.4.
  • composition of the working mass,% of the mass water - 39.65; ash content - 18.43; carbon 21.36; oxygen - 17.52; sulfur - 0.13; hydrogen 2.80; nitrogen - 0.13
  • briquettes with dimensions of 150x150x150 mm were obtained, of the following composition,% of the mass: water - 20.00; ash content - 24.40; carbon 28.32; oxygen 23.23; sulfur - 0.17; hydrogen - 3.71; nitrogen - 0.17
  • a gasifying agent is supplied to the air supply zone, in which air is used in an amount of 2064 kg / h (1600 nm 3 / h) and water vapor in an amount of 200 kg / h, and 30 kg of hydrogen in the synthesis and hydrogenation of hydrocarbons /hour.
  • the combustion process is carried out at a temperature of about 1000 0 C.
  • the gas-vapor products leaving the reactor with a temperature of 190 ° C and the hydrocarbons contained in them are separated into liquid and gas components, which is carried out sequentially in a cyclone and condensers cooled by water with an initial temperature of about 18 ° C.
  • the gas component the amount of which is 2694.5 kg / h, has the following composition,% of the mass:
  • an organic liquid component in the amount of 320 kg / h was obtained, containing a mixture of hydrocarbons C 6 - Syu (including octane, benzene, xylene isomers).
  • the output stream of solid residues from the discharge zone of the reactor amounted to 2020 kg / h in quantity and its structure includes, kg / h: nozzle - 1600; mineral raw materials - 320; metal - 90; sulfur-containing compounds - 10.
  • Brown coal of the Moscow Region basin of the following composition is used as the initial raw material,% of the mass: water - 32.00; ash content - 21.00; carbon 28.70; oxygen - 9.00; total sulfur - 2.70; hydrogen - 2.20; nitrogen - 0.60
  • Gasification agent (air) is supplied to the reactor’s air supply zone in the amount of 3870 kg / h or 3000 nmVh and water vapor in the amount of 300 kg / h, and hydrogen in the amount of 30 kg / h to the zone of hydrocarbon synthesis and hydrogenation.
  • the combustion process is carried out at a temperature not exceeding 1100 0 C.
  • the gas-vapor products leaving the reactor with a temperature of 190 ° C and the hydrocarbons contained in them are separated into liquid and gas components, which is carried out sequentially in a cyclone and condensers cooled by water with an initial temperature of about 18 ° C.
  • the gas component After the condensation system, the gas component, the amount of which is 4602 kg / h, has the following composition,% of the mass:
  • the organic liquid component was obtained in an amount of 293 kg / h, containing a mixture of C 6 -Ci S hydrocarbons ( ⁇ including octane, benzene, xylene isomers, decane, n-hexadecane).
  • the output stream of solid residues from the discharge zone of the reactor amounted to 2665 kg / h in quantity and its structure includes, kg / h:
  • the nozzle mentioned in Examples 1, 3 and 4 can be made of fly ash, for example, the Cherepetskaya state district power station of the Tula region or other power plants.
  • fly ash contains a sufficient amount of iron oxides. It also contains alumina (Al 2 O 3 ), which is a promoter of catalysts based on iron oxides.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Wood Science & Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention se rapporte au domaine du traitement industriel des produits contenant du carbone et/ou des hydrocarbures, et peut être utilisée notamment dans le traitement de déchets industriels et domestiques de divers types, afin de traiter des produits minéraux combustibles de basse qualité. Le procédé de traitement est caractérisé en ce qu'immédiatement derrière la zone de cokéfaction et de pyrolyse se trouve une zone de synthèse et d'hydrogénation des hydrocarbures à une température de 250 à 400°C, tandis qu'on maintient une température de 850 à 1300°C dans la zone de combustion. Dans la zone de cokéfaction et de pyrolyse, on sépare le carbone non lié chimiquement, tandis que dans la zone de combustion, on le traite à la vapeur d'eau de manière à former de l'hydrogène libre qui est envoyé vers la zone de synthèse et d'hydrogénation, après quoi on effectue la synthèse et l'hydrogénation des hydrocarbures. On procède à une raréfaction à l'intérieur de l'espace de travail du réacteur et le processus est réalisé en présence d'un catalyseur qui est introduit dans la composition du jet. L’invention permet de réduire la capacité thermique du processus, d'élargir les possibilités industrielles en ce qui concerne la gestion de la composition chimique et l'accroissement du rendement de produits prêts pour une utilisation ultérieure, ainsi que d'en améliorer la qualité.
PCT/RU2009/000675 2008-12-10 2009-12-08 Procédé de traitement de produits contenant du carbone et/ou des hydrocarbures et réacteur pour sa mise en œuvre WO2010068139A1 (fr)

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RU2544669C1 (ru) * 2014-02-03 2015-03-20 Закрытое Акционерное Общество Научно-Производственная Компания "Интергаз" Способ переработки горючих углерод- и/или углеводородсодержащих продуктов и реактор для его осуществления
RU2591075C1 (ru) * 2015-05-12 2016-07-10 федеральное государственное бюджетное образовательное учреждение высшего образования "Кузбасский государственный технический университет имени Т.Ф. Горбачева" (КузГТУ) Полигенерирующий энерготехнологический комплекс
RU2668447C1 (ru) * 2017-09-25 2018-10-01 Федеральное государственное унитарное предприятие "Центр эксплуатации объектов наземной космической инфраструктуры" (ФГУП "ЦЭНКИ") Способ газификации твердого топлива и устройство для его осуществления
RU2762192C1 (ru) * 2018-08-31 2021-12-16 Макс Айхер Гмбх Унд Ко. Кг Способ изготовления продукта коксования

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150144476A1 (en) * 2012-07-25 2015-05-28 ZAKRYTOE AKTSIONERNOE OBSHCHESTVO NAUCHNO- PROIZVODSTVENNAYA KOMPANIYA «INTERGAZ» Method for processing combustible products, reactor for implementing same (variants) and apparatus comprising said reactor
EP2889360A4 (fr) * 2012-07-25 2016-04-06 N Proizv Kompaniya Intergaz Aozt Procédé de transformation de produits combustibles à base de carbone et/ou d' hydrocarbures, réacteur pour sa mise en oeuvre (et variantes) et installation destinée à la transformation de produits combustibles à base de carbone et/ou d' hydrocarbures

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