WO2002072731A1 - Appareil et procede de recuperation d'huile a partir de pneus usages ou de dechets de produits elastomeres - Google Patents

Appareil et procede de recuperation d'huile a partir de pneus usages ou de dechets de produits elastomeres Download PDF

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WO2002072731A1
WO2002072731A1 PCT/GE2001/000001 GE0100001W WO02072731A1 WO 2002072731 A1 WO2002072731 A1 WO 2002072731A1 GE 0100001 W GE0100001 W GE 0100001W WO 02072731 A1 WO02072731 A1 WO 02072731A1
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Prior art keywords
gas generator
partition
heat
heating
starting material
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English (en)
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Gurami Piranishvili
Levani Sharikadze
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DANGADZE JUMBER
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DANGADZE JUMBER
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    • 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
    • C10B51/00—Destructive distillation of solid carbonaceous materials by combined direct and indirect heating
    • 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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics

Definitions

  • the present invention refers to the field of organic chemistry, and, more particularly, to the method and device for obtaining hydrocarbons and other products by pyrolysis of the organic raw materials, in particular, used tyres and elastomeric products.
  • a method for reclaiming carbon black from scrap rubber material is known, which is disclosed in the United States patent specification US 5037628, including the following steps.
  • the scrap rubber material is first pyrolyzed to produce a char material that contains a mixture of agglomerated or cluster particles which consist of agglomerations of finer carbon black particles and unitary grit like particles.
  • the agglomerated particles are then selectively de-agglomerated by agitation of the char material into the finite component particles of carbon black. These finite component particles are then separated from the unitary particles to obtain a final carbon black which is comparable to commercial grade carbon blacks.
  • FIG. 1 Another patent specification US4074979 discloses a thermal decomposition apparatus according which waste material heated in the bottom of a thermal decomposition furnace is vaporized to create gas flow upwardly within the furnace.
  • Cooling means located to have the upwardly flowing gas pass thereacross operates to control the temperature of the gas leaving the furnace through the upper end thereof so that gaseous product having a boiling point above the boiling point induced by the cooling means will condense and fall within the furnace onto tray means located below the cooling means and adapted to receive therein condensed liquid from the cooling means.
  • the tray means include orifice means for enabling upwardly flowing gas to come into contact with the liquid received in the tray means, and downflow tubes for causing liquid within the tray means to flow downwardly to the bottom of the furnace into contact with heating means.
  • Gas flowing upwardly from the heating means passes through the orifice means and into contact with the liquid in the tray means.
  • exit gas flow is controlled to prevent clogging of the exhaust portions of the apparatus by solidification of the decomposition product.
  • the vapors and gases which are produced and/or liberated within the tube are quickly removed therefrom by means of a vacuum of from about four inches to about six inches of mercury, with the vapors being condensed and the gases separated therefrom.
  • the char or residue which is a black, powdery, carbon-type material is also recovered.
  • a process for economically recovering carbon black, oil and fuel gas from vehicle tyres is disclosed in the patent US467443, for either whole tyres or physically fragmented tyres.
  • the tyres are washed to remove dirt and road film.
  • the clean tyres are dried and preheated with super-heat steam.
  • the hot tyres are pyrolyzed to partially devolatize a major portion of the hydrocarbons and produce a char that can be separated from the steel and fiber glass.
  • the char is subsequently pyrolyzed with microwaves that elevate the tyre temperature and devolatize the remaining hydrocarbons from the char as gas.
  • the hot gases are cooled and partially condensed.
  • the uncondensed gas is used as fuel.
  • the condensed oil is sent to storage.
  • the solid residue from the tyre pyrolysis is char, fiberglass and steel.
  • the char is mechanically separated from the glass and steel.
  • the char is milled to break down agglomerates and subsequently pelletized and bagged. The steel and glass are discarded as trash.
  • a Process for recovering carbon black and hydrocarbons from used tyres is described in the patent US4250158.
  • the invention is a process for economically recovering carbon black, tar, oil and fuel gas from used tyres.
  • Used tyres are physically sliced and fragmented. The fragments are pyrolized in an oxygen-limited, hydrocarbon vapor at subatmospheric pressure while being refluxed with process tar condensate.
  • Vapor phase products of the pyrolysis are fractionated into tar, oil and fuel gas.
  • the fuel gas can be compressed and burnt to provide process heat.
  • Solid phase pyrolysis products are stripped of trash and milled to carbon black in an air swept roller mill. Carbon black is mechanically separated from the effluent air stream of the roller mill and formed into pellets that are dried in a series multi-stage fluid bed dryer.
  • the united states patent US4983278 discloses a two step retorting process for pyrolyzing a solid feed selected from the group consisting of oil shale, tar sand, waste motor oil, and scrap tyres to recover valuable products therefrom comprising retorting a mixture of the solid feed in heavy oil at a relatively low temperature, recycling the oil formed back to the first step, and completing the pyrolysis of the residue formed at a higher temperature in the absence of product oil recycling.
  • Apparatus is provided including a means for feeding and soaking the solid feed, a HSPR, an IFBC, and means for handling product liquid and gas.
  • Still another US patent US4284616 discloses a process for economically recovering carbon black, oil and fuel gas from used tyres. Used tyres are physically fragmented. The fragments are pyrolized at slightly subatmospheric pressure in a reactor while process char is being recycled to increase heat transfer and avoid coke on heat transfer surfaces. Entrained char is separated from the vapor phase products of the pyrolysis, and the vapor phase products of the pyrolysis are then fractionated into oil and fuel gas.
  • a preferred embodiment condenses reactor vapors in two stages at two temperature levels to separate dust from an oil-dust mixture, without water in the first stage and light oil in the second stage. The fuel gas can be compressed and burnt to provide process heat.
  • the entrained char dust and some heavy oil is returned to the reactor.
  • Solid phase pyrolysis products are stripped of trash and milled to carbon black.
  • Carbon black is mechanically separated from the effluent air stream of the mill and formed into pellets with added water and dried.
  • the reactor is equipped with the first inlet means for receiving shredded tyres; second inlet means for receiving petroleum products; and heating means for heating the inside of the reactor to a temperature sufficient to cause a reaction between the shredded tyres and the petroleum product to produce tyre oil; a separating means for separating unreacted components of the shredded tyress from the petroleum product; discharge means for discharging the petroleum product from the reactor; removal means for removing the unreacted components from the reactor, which compreses a substantially horizontal first conduit means affixed to the reactor; a substantially vertical second conduit means connected to the first conduit means; a first screw auger means, having a portion located within the reactor and the remaning portion within the first conduit means, for moving the unreacted components from the reactor through the first conduit to the second conduit, a first motor means being connected to the first screw auger means for driving the first screw auger means, and a second screw auger means being located within the second conduit means for preventing binding of the unreacted components in the reactor
  • the reactor cemprises also a pair of screens located within the chamber means at a predetermined angle with the vertical, and bottom element connecting to said screens to facilitate the movement of the unreacted components down the screens while the petroleum products pass through the screens.
  • a method for obtaining oil by reacting tyres with petroleum products which is described in the partenent specification US 5423950 comprises the steps of introducing shredded tyres and oil into the reactor; heating the inside of the reactor to a temperature sufficient to cause a reaction between the shredded tyres and the oil to produce oil, separating unreacted components of the shredded tyres from the reactor and discharging the tyre oil from the reactor, removing the unreacted components from the reactor by using a first screw auger means in a substantially horizontal first conduit means to move the unreacted components from the reactor through the first conduit means and through a substantially vertical second conduit means connected to the first conduit means and containing a second screw auger means.
  • the heat exchange is performed by means of the reactor wall, which substantially decreases the intensity of the process. Separation of the reaction volume from the atmosphere by means of valves at an elevated temperature is not reliable, the post-pyrolysis remaining products of the starting material come into the direct contact with combusted gases thereby preventing the capability of producing the pure synthesis gas that could be utilized in wide range of industry areas. In addition, along with the combusted gases and reduction gases existing in the atmosphere, impurities obtained from the gas are exhausted into the atmosphere, poluting thereby the environment, and the big quantity of sulphur is remained in coke, being also undesirable in the view of environment protection.
  • the method of carbonaceous pyrolysis which comprises the steps of: forming a mixture of the solid feed with heavy product oil; heating the mixture, in a first retorting step, to a first temperature at substantially atmospheric pressure to form light oil, heavy oil, and solid residue; recovering the heavy oil from the residue and recycling the heavy oil to the first retorting step; treating the residue, in a second retorting step in a horizontal screw pyrolysis reactor, at a second temperature at substantially atmospheric pressure, the second temperature being higher than the first temperature, the second retorting step completing pyrolysis of the residue and forming solid residue, product liquid and product gas; and separating the solid residue from the product liquid and product gas and combusting the solid residue in a fluidized bed to form combusted solid residue and flue gas; weherein the hot flue gas downstream of the heavy oil heating step is used to heat air for the combustion step, and the pyrolisis is conducted at the first temperature range of about 400-500° F
  • the above described invention does not provide for the pyrolysis of any product other than the raw material, which, naturally, causes production of carbon as product requiring specific treatment in addition.
  • the process is carried out at a low temperature allowing for fractioning of heavy hydrocarbons alone and not allowing the process of "deep cracking" to be performed. Removal of the result solid products after the pyrolysis from the reaction zone is conducted by means of screws without performing any cooling step (at the reaction temperature) which causes significant losses of liquid.
  • Use of such reactors is limited in such a technological process where there is need of synthesis of other hudrocarbons apart from the primary products of pyrolysis.
  • Known also is a method and apparatus for recovering energy of waste classification incineration which is disclised in the international application published under the document number WO 9853251.
  • the method and apparatus allows to effectively recovery oil, gas and remainders to use again by a series of processing, such as classify, incineration and recovery.
  • the method and apparatus can self-sufficiently feedback electric power and heating power needed by the apparatus and successfully reduce the opportunity of seconded pollution taken by the waste processing.
  • Another international application WO 068338 describes condensation and recovery process of oil from pyrolysis of material containing hydrocarbons such as shredded vehicle tyres.
  • a pair of sequentially positional packed towers to recover at least 95% of the oil contained in the pyrolysis gases is utilized.
  • the first packed tower operates above the dew point of the water vapor in the pyrolysis gases to ensure that no water is condensed and obtain a primary oil fraction having oil with a high flash point of about 60° C or greater and a primary vapor fraction containing additional oils, fuel gases and water vapor.
  • the primary vapor fraction is fed to the second packed tower which operates below the dew point of the water vapor to condense the water and oil having a low flash point of 34° C or below, and provide a secondary vapor fraction containing valuable fuel gases.
  • a method for the pyrolysis of waste products which can be carried out by means of the above described apparatus comprises the steps of: disintegrating the waste products into cuttings; drying the cuttings and driving the dried cuttings subsequently through the reactor vessel; heating the cutting as they are being driven from the entrance end to the delivery end of the reactor vessel up to the temperature sufficient for the decomposition of the cuttings, reactor vessel being maintained at a subatmospheric pressure and, further, airtight and substantially free of oxigen; damming the cutting at the delivery end such that the entyre reactor becames filled with the cuttings being kept compressed at a predetermined dynamic prossure; and passing the decomposition gases and residue of undecomposed cuttings into the delivery chamber where the gases and residue are seperately removed, while the delivery chamber is maintained at subatmospheric pressure and substantially oxygen free by the exclusion of air.
  • the present invention has for its objective to simplify the egineering process and decrease the amount of the heat-transfer medium.
  • the present invention provides an apparates for recovery of oil (hydrocarbons) from used tyres and wastes of elastomeric products, which comprises: a cylindrical housing; means for feeding the cut starting material to a gas generator; heating means for heating the gas generator with the starting material contained therein; a feed hopper airtightly connected to the gas generator entrance end; a partition separating the inside portions of the reactor, wherein the internal surface of the gas generator cylindrical housing is covered with the flame-resistant material, and the outer surface of the housing is enclosed by a steam jacket, the cylindrical bottom thereof being separated by a partition formed by the paralel members arranged in a plane perpendicular to the axis of the gas generator, which is oscillable vertically with respect to the axis of the gas generator; and being connected via a vibroseparator to an intermediate hopper connected via a camshaft with a motor having a reduction gear, the internal space of the gas generator being divided by a fixed conical partition into two portions, another fixed partition being disposed over the conical
  • an outlet for combusted gases is provided in the conical cover thereof.
  • the lower portion of the furnace is a combustion chamber provided with a flame tube and an atomizer and the heating furnace is connected by means of an inclined tube with the gas generator the top of which is provided with an outlet for process gases.
  • the present invention provides also a method for recovery of oil (hydrocarbons) from used tyres and wastes of elastomeric products, which comprises the steps of disintegrating the waste products into cuttings; heating the cuttings up to the temperature sufficient for the decomposition thereof, wherein the heating step of the cuttings is performed by feeding the heat released by the heat-transfer medium in the heaating furnace to the lower portion of the gas generator; and the step of pyrolusis of the starting material located above the partition separating the gas generator starts with production of hydrocarbon vapor and coke, releasing of process gases from the outlet for the hydrocarbon vapors and transfering of the coke to the space under the partition, the starting material is then subject to the gasification and further mixing with the coke heat-transfer medium to improve the heat contact between them, the inorganic components contained in the starting material being separated by means of the screw feeder into the hopper, and the heat-transfer medium accumulated in the intermediate hopper being fed to the upper space of the heating furnace.
  • hydrocarbons hydrocarbons
  • Fig. 1 shows diagram of the gas generator according to the present invention
  • Fig. 2 shows flow diagram of the enginering process.
  • the gas generator 1 is a cylindrical housing the internal surface of which is covered by a flame-resistant layer (brick) 2, the outer surface of which is enclosed by a vapor jacket 3, the bottom of which has the shape of the cone and is separated from the internal space of the generator by means of a partition 5 consisting of several members parallel to one another and arranged in the plane which is perpendicular to the axis of the gas generator, and oscillable vertically along the axis, and heaving a contact with a reduction gear motor 5' by means of a camshaft.
  • a partition 5 consisting of several members parallel to one another and arranged in the plane which is perpendicular to the axis of the gas generator, and oscillable vertically along the axis, and heaving a contact with a reduction gear motor 5' by means of a camshaft.
  • the internal space of the gas generator is divided into two portions by means of a fixed conical partition 6 above which another fixed partition 7 is disposed.
  • the partitions 6 and 7 are provided with cuts parallel to the generator line. The cuts have walls raised by about 3-5 mm.
  • a tubular (hollow) mixer 8 is mounted which is connected with a reduction gear motor 9' by means of a gearing 9.
  • a screw feeder 10 For feeding the starting material to the gas generator, a screw feeder 10 connected with a reduction gear motor 10' is provided.
  • the conical bottom 4 of the gas generator is connected to a vibrosepartor 11 being with its one end connected to intermediate hoppers 12, 13.
  • the intermediate hopper 12 is connected to a waste separiating feeder 14, and the intermediate hopper 13 is connected to a screw feeder 15 for feeding the heat-transfer medium.
  • the screw feeder 15 is connected with a tubular furnace 17 for heating the heat- transfer medium by means of a pepeline 16.
  • the internal surface of the heating furnace upper portion is covered with a flame- resistant layer 18, and the outer surface thereof is provided with an air jacket 19.
  • the conical roof of the heating furnace 17 is provided with an outlet for combusted gases.
  • the lower portion of the heating furnace 17 is a combustion chamber 20 with a flame tube 2 land an atomizer 22.
  • the heating furnace 17 is connected with the gas generator having an outlet tube 24 for process gases by means of an inclined tube 23.
  • the under-partition 6 space of the gas generator 1 and heating furnace 17 is filled with the heat-transfer medium, e.g. Al 2 O 3 , by means of the intermediate hopper 13, and the heat-transfer medium starts to circulate.
  • the combustion chamber 20 sets to operate by feeding the fuel into the atomizer 22 and the air into the jacket 19, resulting in ignition of the combustion chamber and starting the heating of the heat-transfer medium up to the temperature of 1000°C.
  • the screw feeder 10 the starting material is fed to the gas generator 1, and, simultaneously, the vapor is entered into the vapor jacket 2 in the upper portion of which, i.e. in the space above the partition 6, pyrolysis process starts resulting in production of hydrocarbons vapor and coke.
  • the production vapor of the hydrocarbons is let through the outlet tube 24 for process gases, and the coke is transported into the under-partition 6 space of the gas generator wherein the coke is subject to the gasification by the influence of water vapor and conversion thereof, accordingly, into hydrogen (H 2 ) and carbon oxid (CO).
  • the partition 5 starts 10 to oscilate by means of the reduction gear motor 5' by the frequency of about 0.1-0.3 Hz. As a result of the oscilation the heat-transfer medium and coke are remixed thereby increasing the heat exchange between them.
  • the inorganic components contained in the starting material are separated from the heat-tranfer medium by means of the vibroseparator 11 and they are accumulated in the intermediate hopper 13 and, subsequently, fed to the upper space of the heating furnace by means of the screw feeder 15.
  • the starting material - waste of the rubber of the like products, for the purposes of washing out of mechanical impurities, is subject to the washing just before the treatment process with circulating water.
  • the impurities (grime, crushed stone and the like) accumulate in the settler and are discharged from time to time.
  • the washed material is fed to the cutting tool cutting it in 30-50 mm size peaces.
  • the cutting step is performed without any preliminary drying process which prevents its overheating and releasing of the volatiles in the course of cutting.
  • the washed and cut starting material is initially subject to the chemical treatment in the gas generator where it is sequentally thermally treated in the pyrolysis and gasification zones and is entyrely converted into the process gas by acting the water vapor and carbon oxid thereon.
  • the gas generator works on the principle of so called "thermophore-process", the heat necessary for performing the chemical reactions is entered by means of the prelimirally heated heat-transfer medium.
  • the first stage of the thermal treatment by use of the gasification product gases (hydrogen, carbon oxide and little amount of other admixture gases) is the decomposition pyrolysis performed at the temperature of about 500-900°C. This time the starting material is subject to weathering and the volatile compounds are released therefrom in the form of hydrocarbon vapor.
  • the thermal cracking caused by basically hydrogen and water vapor takes also place.
  • the resulting solid residue-coke from the weathering of the starting material is subject to the gasification by acting the water vapor thereon at the second stage of the thermal treatment and so called "water-gas" substance i.e. mixture of the hydrogen and carbon oxide is produced.
  • the process gas obtained from the gas generator is the mixture of hydrogen (H 2 ), carbon oxide (CO), carbon dioxide (CO 2 ), sulfur-containing gases (H 2 S ⁇ , COS, CS 2 , etc), Sodium oxides (NxOy), methane (CH 4 ), hydrocarbon vapors and excessive (unreacted) steam, which is fed to the system for sulfur removal and processing.
  • mineral residue is also obtained from the starting material with the amount of about 2-5% by the weight of the starting material. It is a zinc oxide (ZnO), magnesia (MgO) and ferroxides (FexOy), contained in the starting material-rubber for various purposes. They are separated from the gas generator and is manufactured to obtain ready products for use as raw materials in metallurgy.
  • the part of the gas coming out of the gas generator is cooled together with the combustion products produced in the furnace for heating the heat-fransfer medium to be mixed together in a steam utilizer.
  • the cooled combustion gases comprising the products free from the sulfur ( CO , H 2 O, NxOy) are exhausted into the atmosphere, and the process gas is mixed with its basic part so as to produce a mixture having temperature of about 300°C and, subsequently, to feed the mixture to the sulfur removal system.
  • Removal of the sulfur is conducted in two stages: in the first stage, all compounds of the sulfur are subject to hydrogenation in an adiabatic manner in a special reactor to produce hydrogen sulfide, and at the second stage, the hydrogen sulfide is absorbed by means of zinc oxide and nickelic oxide also in special adiabatic reactors.
  • the process gas coming out of the absorbing reactors is substantially free from sulfur as its remaining amount does not exceed 10 "3 %.
  • Regeneration of the absorbing reactors is performed by heated air or steam (at 550°C).
  • the processing of the sulfur is carried out in a special system being operated on synthesized principle of basic plinciples used in conventional "concat” (company under the name “lurg”) and "modop” (company under the name “mobile”) processes which enable to obtain the sulfur coming into the atmosphere in an amount not exceeding 10 "4 % and to minimizo the power consumption.
  • the products being obtained are the elementary sulfur and sulfur acid, both being ready products.
  • the process gas is fed either to a conversion system or a separating column, or to both of them in parts.
  • the valuable products are isolated therefrom in the separation column, e.g.
  • the conversion system wherein the components of the process gas are converted into the synthesis gas at the temperature of about 800-900°C by means of steam onto the special catalyst.
  • the conversion step is performed in a single stage on the recirculation principle, in the course of which the liquid products isolated in the separator are returned back to the conversion reactor.
  • the later reactor like the gas generator, works by the principle of thermophore-process. The heat of the combusted gases is utilized in the utilizer.
  • the converted gases (free from the liquid produces) are compressed by means of a compressor up to the pressure of about 16-20 atmosphere after cooling in the separator and, subsequently, is cooled in a condenser wherein fraction of hydrocarbon C 3 -C (liquid gas) is separated therefrom, the fraction being either manufactured as ready product or returned back to the conversion system.
  • the synthesis gas obtained as a result of the conversion is subject to purification from carbon oxide in an absorption system for removing carbon dioxide (CO 2 ).
  • the absorption system consists of absorption and desorption columns and heat fransfer device by means of absorption using ethanol amine. The removed CO 2 at this stage of processing is fed to the processing system.
  • Purified synthesis gas is divided into two parts, the first part the amount of which dependes on the amount of hydrogen in the synthesis gas and the purpose of the synthesis gas being fed to the carbon oxide ( CO) conversion system.
  • the conversion system of CO consists of two transfer device, conversion reactor and separator.
  • the conversion reactor operates in an adiabatic manner, and the conversion process is carried out in standard conditions on "ferrum-chromium" catalyst.
  • the converted synthesis gas becomes free from carbon dioxide in a removal system of CO 2 which is similar to the above described one and is an independent system (absorption is carried out using ethanol amine).
  • the liberated CO 2 from this system is fed to the CO 2 processing system wherefrom the obtained synthesis gas is mixed with its basic portion.
  • the synthesis gas is obtained wherein the concentrations of carbon oxide (CO) and hydrogen (H 2 ) is determined by the conditions of further synthesis process.
  • the concentration of impurities therein does not exceed 1% by amount.
  • the obtained synthesis gas can be used for manufacture of methane, methol alcohol, petrol, hydrogen and other products producable by the standard engineering processes using CO 2 and H 2 .
  • preparation of the pure CO 2 by charging into cylinders) ready products or soda ash takes place.
  • preparation of the aoda ash the engineering process runs according to the "ammonia" method and necessary raw material is common, sodium salt (along with CO 2 ).
  • the described method for processing the carbon dioxide allows to utilize CO in a big amount so that there remains capability to isolate it from the combustion gases.
  • the described engineering process is an independent process in view of power consumption. Feeding of external fuel is not necessary except in starting regime after which the engineering process runs on the heat developed by its liquid or gaseous fuel. Meantime, the product used as fuel is the product obtained after passing through the sulfur removal system; therefore the combustiom products do not contain sulfur compounds and do not affect the atmosphere accordingly.
  • the total yeld of the engineering process is 70%) by weight of the organic starting material.
  • This basic indicator enables it to differ substantially from the similar processes (e.g. processes proposed by the company "Coalite”).
  • the runing principle of the engineering process allows to products any chemical product (not only fuel) produced by the synthesis performed on the basis of carbon dioxide ( CO 2 ) and hydrogen (H 2 ).
  • CO 2 carbon dioxide
  • H 2 hydrogen
  • This fact provides it with particular flexibility as it is possible to change to production of that product (by only altering the process regimes) which would have maximum demand in the market.
  • methanol CH OH methyl alcohol
  • the main purpose of the engineering process is to process used automobile tyres. This later field of applicability makes it especially promising technology as the reutilization of used tyres is one of the most important issues in view of current state of the environment.

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

Abstract

L'invention concerne un appareil et un procédé de récupération d'huile à partir de pneus usagés ou de déchets de produits élastomères. L'appareil comprend un générateur de gaz ayant une enveloppe cylindrique avec des moyens d'entrée pour le chargement de matières premières et des moyens de sortie pour les gaz du procédé ; des moyens de chauffage du générateur ; la surface intérieure du générateur de gaz étant recouverte d'un matériau résistant à la flamme, et la surface extérieure étant entourée d'une chemise d'air (3). Par sa portion inférieure conique (fond) (4), le générateur de gaz est séparé de son espace intérieur au moyen d'une cloison (5) connectée à un moteur (5') via un arbre à came. L'espace intérieur du générateur est divisé en deux parties par une cloison (6) au-dessus de laquelle est prévue une paroi fixe (7) munie de découpes. Dans la partie supérieure du générateur, il est prévu un mélangeur tubulaire (8) qui est connecté à un moteur (9') via une transmission à engrenages (9) et qui est connecté, par ailleurs, à un four de chauffage via un conduit oblique.
PCT/GE2001/000001 2001-03-12 2001-03-28 Appareil et procede de recuperation d'huile a partir de pneus usages ou de dechets de produits elastomeres Ceased WO2002072731A1 (fr)

Applications Claiming Priority (2)

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GEAP2001004233 2001-03-12
GEAP2001004233 2001-03-12

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WO2002072731A1 true WO2002072731A1 (fr) 2002-09-19

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PCT/GE2001/000001 Ceased WO2002072731A1 (fr) 2001-03-12 2001-03-28 Appareil et procede de recuperation d'huile a partir de pneus usages ou de dechets de produits elastomeres

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015089556A1 (fr) 2013-12-16 2015-06-25 Renergi Pty Ltd Appareillage pour pyrolyser un matériau charbonneux
US11999920B2 (en) 2020-09-14 2024-06-04 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock
US12031097B2 (en) 2021-10-14 2024-07-09 Ecolab Usa Inc. Antifouling agents for plastic-derived synthetic feedstocks
US12304888B2 (en) 2021-03-10 2025-05-20 Ecolab Usa Inc. Stabilizer additives for plastic-derived synthetic feedstock

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US4225392A (en) * 1978-09-05 1980-09-30 Taylor Leland T Pyrolysis apparatus
US4588477A (en) * 1984-05-11 1986-05-13 Habib Ikram W Traveling fluidized bed distillation of scrap tires and rubber vulcanizate
US5423950A (en) * 1993-10-28 1995-06-13 Texaco Inc. Method and reactor for producing tire oil

Patent Citations (3)

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US4225392A (en) * 1978-09-05 1980-09-30 Taylor Leland T Pyrolysis apparatus
US4588477A (en) * 1984-05-11 1986-05-13 Habib Ikram W Traveling fluidized bed distillation of scrap tires and rubber vulcanizate
US5423950A (en) * 1993-10-28 1995-06-13 Texaco Inc. Method and reactor for producing tire oil

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015089556A1 (fr) 2013-12-16 2015-06-25 Renergi Pty Ltd Appareillage pour pyrolyser un matériau charbonneux
EP3083886A4 (fr) * 2013-12-16 2017-07-05 Renergi Pty Ltd. Appareillage pour pyrolyser un matériau charbonneux
US9957444B2 (en) 2013-12-16 2018-05-01 Renergi Pty Ltd Apparatus for pyrolysing carbonaceous material
US11999920B2 (en) 2020-09-14 2024-06-04 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock
US12503663B2 (en) 2020-09-14 2025-12-23 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock
US12304888B2 (en) 2021-03-10 2025-05-20 Ecolab Usa Inc. Stabilizer additives for plastic-derived synthetic feedstock
US12031097B2 (en) 2021-10-14 2024-07-09 Ecolab Usa Inc. Antifouling agents for plastic-derived synthetic feedstocks

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