WO2002102930A2 - Processus economes en energie pour la conversion de dechets de raffinerie et de dechets a base de petrole en carburants standards - Google Patents

Processus economes en energie pour la conversion de dechets de raffinerie et de dechets a base de petrole en carburants standards Download PDF

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Publication number
WO2002102930A2
WO2002102930A2 PCT/US2002/014089 US0214089W WO02102930A2 WO 2002102930 A2 WO2002102930 A2 WO 2002102930A2 US 0214089 W US0214089 W US 0214089W WO 02102930 A2 WO02102930 A2 WO 02102930A2
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Prior art keywords
ash
hot
petroleum
dewatering
water
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PCT/US2002/014089
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English (en)
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WO2002102930A3 (fr
Inventor
Alexander P. Brohnshtein
Moshe Gewertz
Vladimir M. Rozhansky
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Ipson Ltd.
Karmali, Rashida, A.
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Application filed by Ipson Ltd., Karmali, Rashida, A. filed Critical Ipson Ltd.
Priority to AU2002332393A priority Critical patent/AU2002332393A1/en
Publication of WO2002102930A2 publication Critical patent/WO2002102930A2/fr
Publication of WO2002102930A3 publication Critical patent/WO2002102930A3/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09C—RECLAMATION OF CONTAMINATED SOIL
    • B09C1/00—Reclamation of contaminated soil
    • B09C1/06—Reclamation of contaminated soil thermally
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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
    • C10G33/00—Dewatering or demulsification of hydrocarbon oils
    • C10G33/04—Dewatering or demulsification of hydrocarbon oils with chemical means
    • 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
    • C10G33/00—Dewatering or demulsification of hydrocarbon oils
    • C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration

Definitions

  • the present invention relates to the process of making a useable product out of refinery and other petroleum based sludge, bottoms, among others, and to the waste heat energy utilization with minimum environmental impact.
  • the invention is particularly suited to process waste of the type, but not limited to, slow moving emulsions and suspensions, containing organic matter and water with dissolved substances, and containing suspended particles and waste of heat energy.
  • the present invention also provides an apparatus for producing useful and standard fuels from refining and petroleum-based waste.
  • U.S. Patent 4,750,274 of Erdman, et al. discloses a method for improving the sludge drying by addition of large scouring particles.
  • the scouring particles remove the particulate residue from the surfaces of the heat exchanger, where the sludge is heated.
  • the heat transfer is also intensified.
  • U.S. Patent 4,786,401 of Jacob, et al. discloses a process for liquid sludge disposal by blending with the feedstock being passed to a fluid catalyst cracking.
  • the sludge is premixed with hydrocarbons, such as light oil, prior to mixing with the feed.
  • U.S. Patent 4,897,205 of Landry is directed to petroleum sludge treatment by the use of steam and a re-circulating solvent with the purpose to decrease their viscosity and as a next step to separate the solid and the liquid components by settlement.
  • U.S. Patent 4,927,530 of Ueda, et al. is directed to sludge treatment in the special tank by the use of anaerobic bacteria.
  • GB Patent 2218256 and U.S. Patent 4,906,409 of Leister discloses a method in which sludge is dried in a fluid bed of preheated glass frit suspensed in nitrogen. The dried sludge and glass is conveyed pneumatically (by nitrogen) to the verification device.
  • U.S. Patent 4,990,237 of Heuer, et al. discloses a method for oil recovery from waste oil sludge (pump-able, low viscosity, high oil and/or water-content sludge) by centrifugation of this type sludge. After that the centrifuge solids with low oil and water content are heated to volatize the contained water and oil. The oil and water are condensed and separated by settling. The separated oil is centrifuged again and refined; the solids can be disposed.
  • U.S. Patent 5,022,992 of Looker discloses an apparatus for sludge separating by flotation for the floatable sludge.
  • U.S. Patent 5,246,599 of Aicher discloses a method and arrangement for sewage sludge treatment in closed system, where the treatment steps are connected by continuous passages in a closed system.
  • the sludge is dried, converted by 250-350 C and finally sintered at least by 1250°C.
  • the vapors removed in the drying stage and in conversion stage are condensed.
  • U.S. Patent 5,259,945 of Johnson, et al. is directed to the bottom waste processing by means of the vapor rapid stripping and by treatment of the heavy part of waste in a pyrolytic reactor for producing vapors, gases and solid residue, which may be used as fuels.
  • U.S. Patent 5,271,851 of Nelson, et al. discloses a treatment system for refining oily sludge.
  • the sludge is mixed with a particulate filter aid and with solvent selected from refinery products.
  • the mixture contacts with a plate filter.
  • a mixture of oil, water and solvent is produced as a filtrate.
  • the filtrate is separated into an oil and water fraction.
  • the oil fraction is directed to refinery.
  • the produced water is routed to a refinery water treatment system.
  • the filter coke residue is washed with a solvent, stripped to remove hydrocarbons and is removed for disposal.
  • U.S. Patent 5,324,417 of Harandi discloses a method for refinery sludge and slop oils upgrading over hot equilibrium catalyst removed from FCC regenerator. The hot catalyst demetallized and/or demulsifies sludge and slop streams in an auxiliary reactor and converts the sludge and slop oil hydrocarbons to more light products.
  • U.S. Patent 5,389,234 of Bhargava, et al. discloses a method for waste sludge disposal in a delayed coking process.
  • the waste at first is diluted with light hydrocarbons produced by delayed coking (naphtha or gas oil) to minimize fouling and foaming.
  • the mixture stream is heated; the water and the light hydrocarbons are evaporated.
  • the more heavy residue stream is heated to a coking temperature and is introduced into a coking drum.
  • U.S. Patent 5,428,904 of Rutz discloses a method for drying sewage by a gas with temperature up to 50°C.
  • the drying gas itself is reconditioned by reducing its moisture in a separate circuit and is returned to the start of the process.
  • the gas-drying agent (a hygroscopic material) is regenerated by withdrawing moisture there from.
  • U.S. Patent 5,466,383 of Lee is disclosed to treating dried sludge, also containing heavy metals.
  • This process comprises indirectly heating the sludge in the absence of oxygen, up to temperature 300-550°C for organic material volatilization and heating the residue up to 750-1000°C together with steam for the non- volatile organic material gasification.
  • the heavy metals remain in the ash as metal-sulfide complexes, which aren't soluble in acidic water.
  • U.S. Patent 5,573,672 of Rappas, et al. discloses a process for separating extractable organic material intermixed with solids and water by dewatering the mixture with dehydration additives in common with organic solvent and following separation the organic solvent containing extractable organic material from the solids and hydrated additive.
  • U.S. Patent 5,580,391 of Franco discloses a process for the thermo-chemical cleaning of storage tanks by combined action of an organic solvent and the generation of nitrogen gas and heat, whereby produced heating in city, agitation and flotation of the fluidized sludge and its transfer to tanks or desalting units. It is assumed the matter can be reintroduced after that in the usual refining flow.
  • U.S. Patent 5,670,024 of Baltzer, et al. discloses a method for thermal treating of waste and residual material having coats of organic material by employing a drum-reactor developed for this process, heating the waste by a hot gas steam up to 850°C, evaporating and carbonizing the organic material and completely combustion the material.
  • U.S. Patent 5,681,449 and Japan Patent of Yokoyama, et al. discloses a method for treating an organic material containing solid sludge with water by means of heating the material up to 150-240°C by pressure to obtain a fluidized sludge and processing the fluidized sludge up to 350°C by 30-200 arm to convert the organic material to oil and after discharging separating oil from rest.
  • U.S. Patent 5,827,432 of Huhta aki et al. is directed to sludge dewatering by electrically ionizing or by ultrasound treating and adding coagulant to the sludge to effect coagulation.
  • RU Patent 2106313 of Fokin, et al. discloses a method of drying petroleum sludge under vacuum at heat carrier temperature 120-140 C. Drying is performed in three steps: stripping water and part of sludge hydrocarbons, continuously feeding organic solvent (toluene, gasoline fraction etc.) and stripping excess solvent.
  • U.S. Patent 5,882,506 of Ohsol, et al. discloses a process for recovering oil from refinery waste emulsion by adding a sufficient amount of a light hydrocarbon diluent to the emulsion to lower its viscosity and specific gravity. The diluted emulsions are subjected to flashing at emulsion-breaking conditions after the oil is recovered.
  • U.S. Patent 5,922,189 of Santos discloses a process to refine petroleum residues and sludges generated by the oil producers, refineries and re-refineries comprising heating the mixture at this temperature for a time 1-6 hours for asphalt generating.
  • the volatile products after condensation are directed to produce fuel, waxy oil and can be further processed.
  • U.S. Patent 5,961,786 of Freel, et al. discloses an apparatus for a fast pyrolytic system.
  • the feedstock, non-oxidative transport gas and inorganic particulate heated material are rapidly mixed, than transported upward through an entrained-bed tubular reactor.
  • the system includes a cyclonic hot solids re-circulation system and the vapor quenching system.
  • U.S. Patent 6,153,017 of Ward, et al discloses a method for treatment of soil contaminated with oil residues by means of forming aqueous slurry with hydrophobic foamed adsorbent (polymer or copolymer of styrene or other foamed materials having a density less than water). After mixing the adsorbent with sorbed oil is separated by gravity separation from the aqueous admixture.
  • hydrophobic foamed adsorbent polymer or copolymer of styrene or other foamed materials having a density less than water.
  • DE Patent 19716436 of Matschiner is directed for used cooling lubricants reprocessing comprising: treating the lubricants with peroxo-di-sulphuric acid or their salts at 50-90°C, concentrating the sulphate-containing aqueous phase liberated from organics. The concentrate is used for electrochemical production of peroxo-di-sulphate and the water is recycled back to the process.
  • U.S. Patent 5,672,277 of Parker, et al. discloses a method extraction of water by means of water-sorbing material that covers an inner surface of bag and presents in the bag as filaments.
  • U.S. Patent 5,676,711 of Kuzara discloses a process of conversion used oil to a low-sulfur diesel fuel processing the used oil with coal as an oil-coal slurry by 850°F and - 100 atm in a time more than 1 hour.
  • U.S. Patent 5,755,955 of Benham, et al. uses a hydro-cracking process with preliminary addition to the feed coke as an inhibitor and iron compound.
  • U.S. Patent 5,938,935 of Shimion discloses method and apparatus for purifying and treating cooling agents and/or lubricants used in the metallurgical industry.
  • the solid particles are removed from the liquid by sedimentation on the plates, which are placed in specific manner, and additionally by magnetic force.
  • the waste heat (of the hot ashes) from boiler's assemblies is used as a heat source for driving the process.
  • the primary object of this invention is to provide a process and apparatus able to handle variable waste loads in an economically viable manner.
  • figure 1 is a flow diagram detailing option of the process and figure 2 details the inner workings of the reactor for petroleum based waste processing.
  • Fig. 1 comprises of a dewatering mixer unit (1), a reactor (2), a sieve (3), a bunker-portioner (4), and a fractional column (5).
  • Fig 2. represents a diagram detailing the inner workings of the reactor for the petroleum-based waste, the reactor (21), comprising a petroleum-based waste charge pipe (22), set of hoppers for the hot ash (23), a plurality of mixing elements (24), a pipe for cracking gases and vapors evacuation (25), a filtering system for gas-vapor and solid particles separation (26),
  • the invention provides the process of making a useable product out of refinery and other petroleum-based sludge, bottoms among others and at the same time utilize the heat energy present in the waste, so that there is minimum environmental impact.
  • the treatment relates to the processing of slow moving emulsions and suspensions, containing organic matter and water with dissolved substances and suspended particles.
  • the overall process for treating the petroleum-based wastes comprises of the following steps: a. removing the water by the use of solid grain dewatering materials derived from hot industrial waste (hot oil shale ash or other suitable solid fuel ash, coal ash etc.) in the dewatering mixer (1); b. removing the water from the petroleum-based waste by water selective adsorption into the dewatering additives.
  • dewatering additives are protected from contamination by oils by controlling the introduction of the additives in accordance with the moisture of the raw material and in accordance with the kinetics of the water adsorption by the used additives; c. evaporating the adsorbed water without needing water expulsion, thereby avoiding the use of complicated and expensive equipment for the operation; d.
  • the petroleum-based sludges generally contain, up to 70% water.
  • the water content ranged within 57-68%.
  • the sludge also contained 15-25% oil and 15-20% mineral particles.
  • the sludge is a stable oil-water emulsion and the mineral particles are suspended in the emulsion.
  • the components of the sludge exhibit insignificant levels of settling, and therefore pose problems, for the dewatering step.
  • the water evaporation method of the present invention is preferable, because it generates only pure steam, and not sewage, to be discarded into the environment.
  • dewatering materials An additional problem regarding the use of dewatering materials is that once the dewatering materials and petroleum-based waste are mixed, both the water and oils are adsorbed. As a result the water adsorption capacity of the dewatering additives is decreased and after several cycles becomes negligible. To regain the adsorption capacity, dehydrating materials (CaO, CaCl 2 , Al 2 O 3 , silica gel, etc.) are added to watered material and mixed. However, these dehydrating materials rapidly lose the ability to adsorb, and at the same time, cannot be recycled. Hence, the overall energy consumption requirement for dehydrating materials is increased.
  • dehydrating materials CaO, CaCl 2 , Al 2 O 3 , silica gel, etc.
  • the present invention bypasses these problems by creating a situation of selective adsorption of the water from the oil emulsion, while simultaneously utilizing inexpensive dewatering agents, by using such solid dewatering grain materials as oil shale ash or other suitable ashes.
  • the present invention is able to achieve selective adsorption due to the adsorption kinetics of the water and oil components.
  • the adsorption capacity and rate is higher for the water component than for the oil component. So if the dewatering additive is linked to a variable feed mechanism then the optimal rate of application can be calculated.
  • the advantage of this is that all of the additives are not applied at once and the water is completely adsorbed while the oil layer persists untouched.
  • the dewatering material is then introduced depending on the program developed and is changed by varying the screw-feeder rotation speed.
  • the present invention also provides the procedure to determine the adequacy of a given material as a dewatering additive by the petroleum-based waste processing.
  • a suitable additive the materials must be shown to have been created as a by-product of another process.
  • These by-products include: ⁇ D oil shale ash; oil shale coke-ash residue after the oil shale thermal processing - half- coking or retorting, gasification, etc.; (3D suitable ashes from other solid fuels.
  • These and other like materials adsorb not only water selectively, but also oils. However the selective adsorption of water can be achieved by the procedure of the present invention.
  • the adsorption capacity of the oil shale ash of water is 65-70% by weight.
  • the dewatering grain material granularity ranges within 1.0-6.0 mm that allows for separation of the material from the dewatered raw matter, and its mineral particles.
  • the size of the mineral particles in processed petroleum-based waste is generally smaller than 100 ⁇ m. Therefore, variants of the conditions of the dewatering stage can be used depending on the dewatering material granularity.
  • the dewatering material is introduced into the sludge in a controlled manner, and the water is adsorbed under suitable conditions.
  • the mixture then consists of coarse dewatering particles impregnated by water, and the dewatered raw material.
  • the mixture formed is heated by adding the needed amount of the hot ash, and is dried.
  • the procedure of drying runs without the expulsion of matter by heating. This is because the adsorbed water evaporates in (1) from solid particles. In this case the water- oil phase is destroyed by adsorbing the water to the dewatering material prior to evaporation. This type of separation of the emulsion is the key to successful evaporation.
  • the steam formed during drying is directed into the boiler (6), where the oil shale or other solid fuel is burned and is treated there at a temperature of ⁇ 750°C.
  • the organic substances, which can be captured by steam are decomposed and burned at this temperature.
  • the amount of captured organic substance by this operation does not equal more than 0.5-1% of the total.
  • This mechanism may be used to successfully remove the organic based wastewater in form of pure and disinfected steam. This therefore avoids the expulsion of the watered matter during the heating process.
  • the mixture After the dewatering stage the mixture is directed into the reactor for carrying out several operations as enumerated below.
  • the raw material is skimmed up to the cut-off point of 350°C.
  • the heat for the skimming is provided by the addition of the required amount of the hot ash, which serves as a direct heat carrier. Therefore, no additional energy is required and the process of the invention becomes economical.
  • the treated matter is transferred into its activation zone (25).
  • the hot ash is added into the activation zone for mixing, at temperatures of 350-380°C. At this stage the acidic sulfur and oxygen compounds of the sludge become decomposed.
  • the activated matter is then transported into the cracking zone where it is treated by the ash as a catalytic active material at a temperature appropriate for catalytic cracking.
  • the composition of oil shale ash (the silica-alumina up to 30% and calcium oxide) makes it possible to carry out the thermo-catalytic cracking.
  • the preliminary adsorbing of the organic matter into the catalyst (ash) grains, and the subsequent activation of matter, increases the intensity of the temperature, thereby reducing the heat consumption of the process. The net result is energy conservation.
  • the vapors and gases formed move out from the reactor and enter into the vortex chamber where they are cleaned to remove the captured ash dust.
  • the cleaned vapors and gases are separated by means of the fractional column (5), the gases are cooled, and the vapors condensed and cooled.
  • the ash and the coke formed are removed from the reactor (2) by means of the same mixer elements performing the task of both mixing and discharging.
  • the residual ash contains no more 1-1.5% of coke and is directed into the main hot ash flow from the furnace.
  • the dust mineral component of a refinery sludge coated with coke (after the reactor) has been found to be useful in the cement industry. Its coke gives an added heat in the cement kiln, and its particles size and composition (SiO 2 , Al 2 O 3 , CaO, Fe O 3 , etc.) are acceptable for cement production. It is clear that the dust and coarse catalyst separation after cracking process are suitable for this alternative application, when the dust particles are coated with the coke. In other cases it is reasonable to bum out the coke in the dust to use the dusty minerals depending on their composition and properties as filling or covering materials, etc.
  • the gases formed during sludge processing basically contain hydrogen, hydrocarbons, hydrosulfide and a very small amount of carbon monoxide and dioxides. All of the gases are burned in the boiler furnace (6) in common with oil shale.
  • the sulfur oxide formed by the burning of H 2 S is caught by the calcium oxide and calcium carbonate contained within in the formed oil shale ash and the sulfur oxide emission is prevented.
  • the materials containing calcium carbonate are added to aid in the trapping of the SO 2 . Their presence, positively affects the cracking process and the desulfurization of the formed fuels.
  • FIG. 1 shows the flow diagram of the process referring to Fig.l, the watery petroleum-based waste (sludge, etc.) is mixed with the hot ash, which is introduced by the controlled regime into horizontal mixer-dryer 1 with paddle mixing elements.
  • the mixture temperature doesn't rise more then 70°C.
  • the matter is heated up to 150-160°C by the hot ash which is added into the mixer-dryer through the other appropriate feeding system.
  • the mixture is dried and the formed vapors are directed into the boiler furnace. Here they are heated and burned. The same procedure can be carried out in the boiler furnace (6). Often, the furnaces are fluidized bed burners .
  • the dewatered sludge is directed into reactor 2 (Fig.l).
  • the reactor is a horizontal mixer with paddle mixing and discharge elements (Fig.2).
  • the reactor isn't jacket heated.
  • the reactor is provided with a system (22) that controls the introduction of hot catalyst (ash) and with a hot filtering system for the separation of the dust.
  • the processed material is therefore heated in three reactor zones by introducing hot ash into each of the zones.
  • slamming the petroleum-based material is carried out, with a cutoff point of up to 350°C. This is controlled by means of adding the appropriate amount of hot ash.
  • the vapors are evacuated through the fractional column 5 (Fig.l) that separate two fractions: (a) up to 210°C containing gasoline and (b) up to 350°C containing gas oil.
  • the second zone some non-hydrocarbon components are decomposed. This is followed by the activation of all remaining reaction matter, for example, the catalyst impregnated by remainder of the processed material. Furthermore, the hot catalyst is also added as a direct heat carrier.
  • the catalytic cracking of the remaining material is carried out and the vapors and gases formed are evacuated through the fractional column 5.
  • the coke covered ash catalyst and dusty mineral part of the processed sludge are discharged from the reactor 2 by the same mixer elements and are separated by means of sieve 3.
  • the coarser part of catalyst grains are directed to the mixer-dryer 1.
  • the overall coke content 0.6-1.3% is not reduced. Neither is its adsorption capacity to water.
  • the remaining part of the ash material is introduced into the hot ash flow, which is formed by the burning of the oil shale.
  • the petroleum-based waste processing can be organized as a batch process. Its advantage lies in the ability of the process to carry on the basic operation on the principle of "all operation in one reactor". It means that the dewatering stage can by carried out in the reactor, and after production of enough of the dewatered matter, the thermal processing (skimming, reaction matter activation, catalytic cracking) is carried out next in the same reactor. Thus this batch process is convenient for the small plants that need to process anywhere between 2-3 tons of material per hour on the basis of raw materials formed.
  • the equipment used for the process development and testing includes:
  • the oil shale ash was used as a dewatering additive and as a catalytically active material.
  • the oil shale ash composition, (mass %) is:
  • Oil shale ash from the reactor has a water adsorption capacity of about 61.3%. This oil shale ash consumption on the sludge was about 80%
  • the sludge dewatering was carried out in a batch regime feeding the sludge, which allows for reliable water selective adsorption during the controlled introduction of the dewatering grain matter as it described previously in pending U.S. Patent Application Serial No. 09/772,236, filed on January 29, 2001, which is incorporated herein in its entirety.
  • the sludge mass of 3 kg was put in the batch mixer, with operating volume of 45 liters.
  • the oil shale ash-feeding regime is estimated on the basis of the water adsorption kinetics and by investigating the mixing regularity.
  • the used oil shale ash granularity was ⁇ 2.5 mm.
  • oil-shale ash is introduced in the reactor the temperature reaches up to 350° C.
  • the water is adsorbed by the oil shale ash grains, and the temperature of the mixture reaches 75.7°C.
  • the dewatering vapors are directed into the boiler's burner.
  • An additional amount of oil shale ash at 700°C is introduced once again in the reactor containing the dewatered matter, for further processing, skimming and cracking of the oily material.
  • the average temperature of the catalytic cracking was 410°C.
  • the total amount of added hot oil shale ash in this stage was 22.7 kg.
  • the product yield was, mass %: water 48.5 oil 20.1 solid product (mineral particles coke covered including
  • the sludge mass of 0.5 kg is put in a reactor-mixer with operating volume 7.5 liters.
  • the oil shale ash-feeding regime used corresponds to the water adsorption kinetics.
  • An amount of about 0.16 kg of hot oil shale ash heated up to 400°C is introduced to initiate the water adsorption. This results in temperature of 73.4 C at the end of the process.
  • the product yield was, mass %: water 18.1 oil 19.1 gas 5.3 coke 16.3 minerals i 41.2.
  • the produced oil properties are: density (15.56°C) 0.8445 metals, ppm: viscosity(40°C),cSt 2.1296 phosphorus 0.00 sulfur 0.35 calcium 0.00

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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)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Soil Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Treatment Of Sludge (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention se rapporte à un procédé économe en énergie permettant de traiter des déchets à base de pétrole et d'autres déchets organiques, notamment des bouses ou des dépôts de fond, au moyen de l'énergie thermique de cendres de piroschiste ou d'autres cendres appropriées, obtenues par brûlage du carburant solide. Le processus de conversion ne produit pas de sous-produits contenant des déchets comme les eaux usées polluées, les asphalténiques lourds et les sous-produits du goudron. Par contre, ce processus élimine l'eau par adsorption sélective au moyen de cendres utilisées en tant qu'additifs de déshydratation et il est suivi d'un séchage à hautes températures. Après écrémage de la matière déshydratée, le produit restant est traité par craquage thermo-catalytique au moyen de cendre de piroschiste chaude ou d'autres cendres utilisées en tant que matière catalytique active et en tant qu'élément caloporteur. Ce processus est mis en oeuvre au moyen d'un équipement économique qui est produit de manière usuelle. Le processus et l'appareil de la présente invention permettent l'obtention d'une solution pour le traitement de déchets de raffinerie et de déchets à base de pétrole, ainsi que la production de carburants liquides standards et utilisables.
PCT/US2002/014089 2001-05-02 2002-05-02 Processus economes en energie pour la conversion de dechets de raffinerie et de dechets a base de petrole en carburants standards WO2002102930A2 (fr)

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US09/847,688 US20020144928A1 (en) 2001-01-29 2001-05-02 Energy efficient process for converting refinery and petroleum-based waste to standard fuels
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CN100368053C (zh) * 2006-01-20 2008-02-13 中国矿业大学 疏水团聚造粒助滤的低灰煤脱水方法
CN102633491A (zh) * 2012-05-17 2012-08-15 浙江方远建材科技有限公司 一种高效吸声陶粒
CN103820148A (zh) * 2014-01-23 2014-05-28 周文彬 废矿物油全自动控制催化裂化环保一体化炼油装置及工艺
CN104926051A (zh) * 2015-05-11 2015-09-23 四川捷贝通能源科技有限公司 一种含油污泥热处理方法
IT202000001357A1 (it) * 2020-01-24 2021-07-24 Itelyum Regeneration S P A Valorizzazione dei sottoprodotti di un processo di rigenerazione di olii usati

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US20080182213A1 (en) * 2007-01-31 2008-07-31 Radek Masin Waste oil burning system
CN104388115B (zh) * 2014-07-23 2016-05-18 山东恒导石油化工股份有限公司 有机热载体资源化利用精细分馏的工艺方法
CN111268884B (zh) * 2020-03-31 2024-04-09 浙江科茂环境科技有限公司 一种油泥处理系统及方法
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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100368053C (zh) * 2006-01-20 2008-02-13 中国矿业大学 疏水团聚造粒助滤的低灰煤脱水方法
CN102633491A (zh) * 2012-05-17 2012-08-15 浙江方远建材科技有限公司 一种高效吸声陶粒
CN103820148A (zh) * 2014-01-23 2014-05-28 周文彬 废矿物油全自动控制催化裂化环保一体化炼油装置及工艺
CN104926051A (zh) * 2015-05-11 2015-09-23 四川捷贝通能源科技有限公司 一种含油污泥热处理方法
IT202000001357A1 (it) * 2020-01-24 2021-07-24 Itelyum Regeneration S P A Valorizzazione dei sottoprodotti di un processo di rigenerazione di olii usati
WO2021148913A1 (fr) 2020-01-24 2021-07-29 Itelyum Regeneration S.R.L. Amélioration des sous-produits d'un procédé de régéneration d'huiles d'échappement

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