EP1027406A1 - Procede et dispositif d'evaluation de matieres premieres energetiques et chimiques par reaction de matieres premieres a cout reduit - Google Patents

Procede et dispositif d'evaluation de matieres premieres energetiques et chimiques par reaction de matieres premieres a cout reduit

Info

Publication number
EP1027406A1
EP1027406A1 EP98955409A EP98955409A EP1027406A1 EP 1027406 A1 EP1027406 A1 EP 1027406A1 EP 98955409 A EP98955409 A EP 98955409A EP 98955409 A EP98955409 A EP 98955409A EP 1027406 A1 EP1027406 A1 EP 1027406A1
Authority
EP
European Patent Office
Prior art keywords
substances
water
phase
upgrading
hydrogen
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP98955409A
Other languages
German (de)
English (en)
Inventor
Ludger Steinmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP1027406A1 publication Critical patent/EP1027406A1/fr
Withdrawn legal-status Critical Current

Links

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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/004—Sludge detoxification
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning

Definitions

  • the invention relates firstly to an environmentally friendly process suitable for the use and upgrading of low-value carbon-containing raw materials, residues and waste materials at high temperature and high pressure in the presence of a proton- or electron-conducting substance, and secondly to a device for carrying them out.
  • the environmental friendliness of the process for the production of energy and chemical raw materials is achieved by reducing the increase in CO 2 emissions by using up to 100% regenerative feedstocks.
  • the process is made appropriate to the substance in that the diverse special properties of the substances which have been used and which have been obtained in the meantime are recognized and as much as possible is used to advantage.
  • the input materials are used both as an energy source and as an energy source, as well as a reagent, as well as a precipitant, and also as a separation aid (flocculant, detergent, demulsifier, coalescence promoter, fixator, demister in a liquid / liquid system ) as a catalyst, as well as a reaction medium, as well as a desiccant, and also as a conveying medium, as well as an entrainer, and also as a heat transfer medium, and also as a heat buffer, and also as a reducing agent.
  • the process is particularly appropriate to the substance that it is based on the usual procedure, the substances first to separate thermally and then to upgrade by first upgrading the materials and then separating them.
  • the usual process first separates crude petroleum and its natural and synthetic precursors by distillation and then evaluates them.
  • hydrogen-rich heteroatom-containing components are first broken down into problematic substances such as PAH, thiophenes, pyrroles, pyridines and dienes which are low in hydrogen.
  • the initially non-existent problem substances are created by a lack of hydrogen and then with expensive hydrogen with the help of expensive catalysts under expensive energetic conditions in expensive large-volume plants under expensive safety measures with the help of an expensive large number of aftercare procedures with high energy consumption removed.
  • the new process is particularly material-friendly, because it does not allow the problem of hydrogen deficiency to arise in the first place, by first upgrading the substances with water without additional hydrogen gas and then separating them, by multiplying and versatile the diverse macroscopic properties of the input materials and the intermediate products uses and thus improves the properties of product and wastewater and by separating the substances only when, after the processing steps, the substances differ in their properties to such an extent that they can also be separated with such separation processes that can be separated by a small amount Mark up energy requirements.
  • a variant of the method according to the invention is also suitable for the substance in that it only cleans the substances of bound oxygen and / or only removes the water until the substances meet the requirements of an application, for example that of a fuel.
  • the oxygen content improves, for example, the ignitability, the lubricity, the octane number and the emission values, such as NOx, CO and soot from heating and fuels, and water, for example, also improves the exhaust gas emission values.
  • the low value of the starting materials is due to one or more of the following properties which are perceived as disadvantageous: water-containing, emulsion-like, colloidal, hydrophilic, amphiphilic, high-molecular, polar, rich in heteroatoms, in particular sulfur, nitrogen and metals, tending to form coke, Contains asphaltene, low calorific value, solid state of aggregation, low purity, difficult to dose, difficult to handle, toxic, contaminated by viruses and other microbiologically active substances, harmful from an epidemic point of view, contaminated with highly active substances such as
  • Hormones, antibiotics, etc. explosive, unstable, less prone to sedimentation, expensive to dispose of, color-unstable, staining, air-sensitive, temperature-sensitive, light-sensitive, expensive to dispose of, emitting unwanted volatile substances during combustion, radioactive, bulky, difficult to transport , unpleasant smell, little accepted by neighbors, self-igniting, corrosive.
  • the upgrading according to the invention takes place firstly through chemical conversions and secondly through simultaneous and / or upstream and / or downstream separation processes.
  • the special feature of the chemical transformations according to the invention is that, firstly, they produce the higher quality products and / or that, secondly, they facilitate the separation of the substances or even make them possible in the first place.
  • the special feature of the separation processes according to the invention is that, in conjunction with the chemical conversions, they are arranged in such an order that they simplify, shorten, and therefore make the whole of the refining steps more economical.
  • the number of hydrotreating processes is reduced by four process steps.
  • the gasification of the feedstock, the purification of the synthesis gas, the complex heat removal of the heat of reaction of the FT reaction, the compression of gases and the heat recovery from the No reaction mixture there is a simplification in that the gasification of the feedstock, the purification of the synthesis gas, the complex heat removal of the heat of reaction of the FT reaction, the compression of gases and the heat recovery from the No reaction mixture.
  • the separation processes also have the following special feature: They use the feed material several times as a separation aid. For example, one part of the feed stream is used as an adsorbent for the enrichment of oil from oil-contaminated water, another part as a basic adsorbent for cleaning the product from acidic components, another part as an adsorbent for cleaning the waste water and also the exhaust gases. It is common to all applications that the adsorbents are available at low cost because they are already present anyway and, moreover, as waste or residual material.
  • the loading and disposal of the separation aids can take place in the same company. This means no additional administrative work due to special waste accompanying documents and no significant effort for transport to disposal.
  • the grain size for use as a filter is designed so that the substances can be used in the further process according to the invention without any further change in shape. The disposal of these separation aids is particularly cheap because the loaded auxiliary materials can be disposed of at the point of origin.
  • This advantage which corresponds to the logistical advantage of cleaning in place, is particularly great because bulky goods are incurred on site, disposed of, and recycled, thereby reducing the main costs of transport.
  • the auxiliary is selected so that it has a calorific value. This has the advantage that the auxiliary can be burned after loading.
  • the particular advantage here is that the loaded auxiliary material can be utilized even more economically by being processed into a liquid heating or fuel. This is all the easier if the filter materials can be selected so that they are highly reactive and require little energy for a chemical conversion.
  • the waste water purification method according to the invention selects the adsorbents from different points of view than the waste water technology. While adsorbents are used in wastewater technology that have a high procurement price and are therefore regenerated with considerable material, investment and operating costs, the adsorbates are not only disposed of inexpensively, but also at a low cost to a product in demand processed. While the adsorbents of wastewater technology have to be brought to abrasion resistance, heat resistance, solvent resistance and thus inertness due to their regenerability, the separation aids of the invention do not need to be brought to a greater durability in the first place. They are intentionally kept as reactive as possible so that they can be disposed of and upgraded more cheaply in one go.
  • the device according to the invention is a reactor which gently heats the starting materials as a slurry, allothermally and autothermally in countercurrent. At the same time, it separates the product stream.
  • the reactor impresses with the low outlay in terms of pressure, since the temperature gradients are low and since, in a particular embodiment, the temperature falls from the inside out, and in the low outlay for fittings, since the working temperatures for them are low.
  • the device according to the invention impresses with optimum heat management. It generates heat only where and when and how much is needed for the process.
  • processes for upgrading heteroatom-containing and / or polymeric and / or solid and / or liquid and / or liquefied substances by compression using thermal and / or catalytic processes which include terms such as pyrolysis, hydrolysis, hydrocracking, hydrofinishing, electrolysis liquefaction , Fischer-Tropsch synthesis (FTS), FTS with (CO + H20), methanol-to-olefin process, methanol-to-gasoline process, Guerbet alcohol synthesis, Varga process, depolymerization, liquefaction, dewaxing, wet carbonizing, hot water drying, autohydrogenation, ferrofining, and others can be summarized and which consist of the following sub-operations.
  • thermal and / or catalytic processes which include terms such as pyrolysis, hydrolysis, hydrocracking, hydrofinishing, electrolysis liquefaction , Fischer-Tropsch synthesis (FTS), FTS with (CO + H20), methanol-to-olefin process,
  • the upgrading of the feedstocks ultimately consists in a reduction or elimination of one or more of the properties which are perceived as disadvantageous and which, as described above, cause or contribute to the low value of the feedstocks.
  • the operating conditions are designed in such a way that the valuable substances are generally separated first and then the rest is treated until only salable and disposable substances remain.
  • the operating conditions are designed so that an undesirably high proportion of gases, coke and coke precursors is formed.
  • Most problems are caused by the coke precursors that occur in the liquid product. They largely reduce the value of the liquid phase. They include the oligo- and polycondensed aromatics, the dienes and the derivatives of pyrrole, thiophene and pyridine. On average, these substances have a density close to 1 g / cm3. The consequence of this is that separation from an aqueous phase is made more difficult.
  • the nitrogen derivatives increase the NOx content of the exhaust gases during combustion.
  • the sulfur derivatives can be found in the exhaust gas as S02. In general, these problematic substances have a low hydrogen content and contribute to the formation of gum during storage, heating for coking, catalytic cleavage to inactivate the catalyst, thermal cleavage to reduce the product yield and combustion to soot formation.
  • the reactivity of the low-hydrogen problem substances is so low that they require a highly active catalyst which loses its activity due to the addition of hydrogen and therefore requires high-purity hydrogen.
  • Aerobic decomposition does not convert everything to gas and ash. About half of the heavy metals are found in the liquid and one in the solid phase.
  • the reactor in the deep shaft process burns all organic matter and generates thermal energy at a low level that is difficult to market outside the heating season.
  • the reactor of the deep-shaft process has places in the hot zone that are susceptible to deposits when mud flows through it.
  • the procedural conditions should be designed in such a way that the stalemate of environmental policy objectives can be lifted using non-fossil substances. (The current standstill is that environmentally friendly fuels are being promoted, which can only be produced with the conventional processes of petroleum processing with an additional CO 2 emission.) It is therefore intended to produce such fuels and fuels that are both combustible lower emissions of undesirable substances, such as S02, soot or condensed aromatics, as well as no higher CO2 emissions during production. 4th 00. 04
  • the fabrics should be processed so that they do not over-ripen. 4.00.05
  • the substances should be treated in such a way that the products can be processed into salable components with little effort.
  • the efficiency of the processes is to be increased by coordinating the processes with the upstream and downstream processes. 4.00.08
  • a process is sought that has a high degree of self-sufficiency and is suitable for technical islands. 4.00.09.01
  • the ash-containing components should have matured to such an extent that they can be deposited without intermediate storage.
  • the ash-containing components should be washed to such an extent that they can be deposited without the risk of elution.
  • the system of procedural steps can be simplified. Several process steps can also be combined into a one-pot process or included in another process step.
  • the reactions can at a lower temperature.
  • the overall thermal efficiency of raw material refinement is greater and processing costs are lower. Devices in which this can be simulated, measured, optimized and carried out are presented.
  • the flexibility of the plant is great, so that the input materials can be varied.
  • the system does not necessarily need to be close to a hydrogen generator.
  • the wastewater is contacted with a separating agent, and the previous pollutants are converted into more harmless ones and, in the case of the highly effective special substances, burned as fuel.
  • the waste water is heated and / or cleaned to such an extent that the highly effective substances are decomposed to such an extent that their functional groups and / or their
  • Suitable derivatization agents are, for example, dimethyl ether or dimethyl carbonate or alkanes or isoalkanes or alcohols or isobutane, ie also those substances which are already used or potentially used as main fuel components.
  • This independence of the plant from a hydrogen supplier creates a high degree of self-sufficiency and makes it suitable for technical islands. These include, for example, the pioneering plants in new industrial settlements in Yünnan, the supply and disposal centers in tourist conurbations, in oases or in remote research stations. 6.00.07
  • the reactor has the flow profile of a plug. It is therefore easy to control and easy to simulate and easy to change in scale. 6.00.10
  • the reactions are combined in such a way that the sum of the reactions instead of endothermic exothermic reactions takes place, that the sum of the reactions develops so much heat that the usual heat losses are approximately just compensated for.
  • the process develops so much heat that it is only slightly heated allothermally or has to be cooled slightly. (cf. 6.00.21) 6.00.11 This results in low temperature gradients that protect the material, reduce safety problems and therefore require less safety margins. 6.00.12
  • the process has the safety advantage that there is no H2 or CO. 6.00.13
  • Low density lipophilic substances are also added.
  • the reaction conditions are such that the formation of aliphates is promoted less than that of aromatics.
  • the presence of low-density lipophilic substances is thus ensured, and thus ultimately the presence of a class of substances which enables easy separation of lipophilic substances from water and water-like, water-containing and water-absorbing substances.
  • the substances are only separated if they can be separated due to their different strengths. 6.00.14
  • the used aids are used in the further process steps.
  • the auxiliaries are energetically enriched by the adsorbate; those substances are also adsorbed which have a high reactivity and are therefore processed for disposal faster than the actual adsorbents.
  • the bulky loaded aids are disposed of in the vicinity of the place of occurrence without much transport effort and above all without the great administrative effort of transport via public transport routes (accompanying documents for substances that require special monitoring). 6.00.17 With a simple arrangement, the reaction behavior of the feed under hydrothermal conditions can be estimated. The measured value corresponds to the available (carbon + hydrogen) and shows what valuable materials can be obtained.
  • the carbon measurement according to Conradson, Ramsbotton or Fischer is a measure of the behavior of the substance; if treated improperly, it measures the length of a subject on the procrust bed.
  • the measured value for the available (carbon + hydrogen) measures the ability with the right medium, it measures the ability of the long jumper in the sand pit. 6.00.18
  • the ash accumulates in a washed and in a thermally matured state, so that it is suitable for landfilling. 6.00.20
  • the heat requirement is at such a low temperature level that the heat energy requirement can be met with the exhaust gases of a power generator.
  • the convective heat supply means that the temperatures in the reactor are more uniform than in the radiation zone of a Visbreaker furnace. By adding secondary air, the system can be controlled with simple means even at low temperatures. This makes it easier to change the temperature gently and evenly when starting up and shutting down the system. This reduces the thermal stress and reduces stress corrosion cracking in the high pressure / high temperature part of the system. 6.00.22
  • the reactor is designed so that the heating, the reaction and the cooling can take place in one and the same reactor.
  • the hydrolysis can take place during heating, in which the heteroatoms are split off as hydrides and other groups of substances polymerize.
  • CC bonds can be split and react to paraffins and olefins.
  • C02 groups are split off.
  • Figure 1 is a schematic representation of an embodiment of the method according to the invention or the device according to the invention
  • Figure 2 is a schematic diagram of a reactor in
  • FIG. 1 shown embodiment of the device according to the invention
  • FIG. 3 shows a basic illustration of a method step of the method according to the invention
  • FIG. 4 shows a basic illustration of an application example of the method according to the invention in an oil refinery
  • FIG. 5 shows a basic illustration of a test apparatus according to example 5. This includes the entire list of reference symbols.
  • Cooling result The fresh note of the wine has been converted into a heavy one, very similar to kerosene was.
  • Magnetic stirrer with heating from Heidolph Probe 25 ml Thomy oil from Thomy 20 ml water 2 g paper from an office punch 1 spatula tip MgO 1 spatula tip
  • CaO Reaction conditions The sample was heated in the glass to 100 degrees C and deaerated. The reaction mixture was further heated in the aluminum block. The heating of the magnetic stirrer was set to 280 degrees Celsius.
  • Sample 300 ml untreated pyrolysis gasoline from a steam cracker 20 g waste paper from an office punch 10 g MgO 10 g CaO made up to 1.5 l with water. Reaction conditions: The sample was removed by the
  • the product was 1/3 distilled with steam.
  • the distillation temperature rose from 65 degrees C to 100 degrees C.
  • the composition of the starting material has changed according to the numerical values on the following page: Teaching: With carbohydrates from starch, the gum formers can be removed from the pyrolysis gasoline by selective hydrogenation under the reaction conditions according to the invention remove.
  • a tube reactor such as that found in a tube heater or visbreaker, is sufficient as a system for continuous upgrading.
  • Aromatics C7 14.20 21.10 * Detection limit 0.05% by weight
  • volume of the test loop 1.9 1 length of preheater, reactor and soaker and
  • reaction conditions according to the invention are simulated so that natural and synthetic raw materials can be converted into a crude oil and separated from inorganic substances.
  • a tubular reactor like the one in the tube heater or
  • Visbreaker occurs, is sufficient as a system for continuous upgrading.
  • Vessel 4 A preheat
  • Methyl cellulose, starch, cellulose, clay slurry Methyl cellulose, starch, cellulose, clay slurry
  • Sample loop flows;, rinse with water so much that 7b contains 50 ml more water in the vessel than corresponds to the sample;
  • Vredestein (the rubber was cut into flour in a kitchen machine from Moulines, type 643-763-899)
  • the sample was pumped through the reactor within 1 hour.
  • the sample can be pumped through the apparatus.
  • a water-clear, colorless product was obtained. This came about 400 ml earlier than the clayey fraction.
  • the first fraction was milky.
  • the second was less cloudy.
  • the cloudiness of the third was even less, but still clearly visible. Over time, the samples darkened.
  • the organic phase of the second fraction was examined for aniline by GC-MS. About 1% by weight of aniline was detected.
  • a tube reactor such as that found in a tube heater or visbreaker, is sufficient as a system for continuous upgrading.
  • nitrobenzene can react in various ways in a reducing environment to nitrosobenzene, hydroxyaniline, diazobenzene and dihydrazobenzene and also to other substances, it can be seen from the presence of aniline that the reduction potential is considerable under the conditions according to the invention is. Because at room temperature, the hydrogenation of nitrobenzene with hydrogen over platinum in the presence of an base, such as pyridine, remains at the reduction stage of the dihydrazobenzene (see dissertation Steinmann, 1975, pages 72 to 77).
  • H2S The presence of H2S in amounts which indicate that the sulfur of the product is predominantly in the form of H2S is understood as a measure of the reduction-oxidation potential of the reaction mixture.
  • the minus sign missing in the publication on the lower half of the abscissa is a typographical error.
  • Apparatus apparatus from example 5
  • Example 1 Apparatus from Example 1 with the following changes: In addition to the sample, the bomb tube was also additionally loaded with a nail and mounted in an open steel tube. The steel tube, which was encased and thermostatted by a heating jacket from Heräeus, was made to tumble during the experiment. The mixing was caused by the sound of the moving Nagels controls. Sample: Polyethylene in powder form from Vestolen GmbH, Gelsenmün,
  • Polyvinyl chloride stabilized with organic Sn compounds, powder, Vestolen GmbH, Gelsenmün oatmeal, type Kernige, from Kölln, Elmshorn,
  • the product was a blue-gray, matt pasty mass. When the reaction mixture cooled, the noise of the nail was no longer heard below 80 degrees C.
  • the product has a melting point nearby of 80 degrees C.
  • plastics from the yellow bin are hand-picked and cleaned so that they can be used for a more noble material as a waste incineration plant and that the calorific value of the waste is burned with high and non-boiling by-products of petroleum refining.
  • Waste oils are usually roughly cleaned and then used as a fuel, such as heavy fuel oil.
  • the price for cleaned waste oil is -DM 10, - / t to + DM 10, - / t and is then even lower than that for petroleum coke or heavy fuel oil.
  • An upgrade according to the invention consists in contacting the waste oil with one (adsorption and / or separation aid and / or extraction agent) which, if possible, has a calorific value which contains carbon and which is degradable by hydrolysis. Since the degree of soiling fluctuates from delivery to delivery, the need for cleaning agents is determined in small-scale tests. For the time being it is assumed that about 2% sawdust and about 0.5% CaO are added. Before, at the same time and / or afterwards, it will be seen with water, which can be contaminated with organic substances like the mother liquor (here, for example, distilled water + methanol). The by-products (salt + emulsion + water + detergent + oil) are processed like an emulsion and like loaded oil binder.
  • the cleaned oil is suitable for olefin production by means of thermal allothermic steam splitting, for the manufacture of petrol components in a catalytic cracker and for use as a fuel component in a combined heat and power plant.
  • Brake fluids occur in a motor vehicle mechanic operation. Because of the prohibition of mixing hazardous waste, the effort involved in collecting, storing and transporting it is considerable. They have a heating value that is only half as high as used oil. The costs for disposal are about DM 1000, - / t.
  • An upgrade according to the invention consists in contacting the used brake fluid with one (adsorption and / or separation aid and / or extraction agent) which, if possible, has a calorific value which contains carbon and which is degradable by hydrolysis. Since the degree of soiling fluctuates from delivery to delivery, the need for cleaning agents is determined in small-scale tests. For the time being it is assumed that approx. 2% sawdust and approx. 0.5% CaO are added. Before, at the same time and / or afterwards, it is mixed with water containing organic substances of the type of mother water (here for example distilled water + methanol) can be washed. The by-products (salt + emulsion -fr- water + detergent + oil) are processed like an emulsion and like loaded oil binder.
  • water containing organic substances of the type of mother water here for example distilled water + methanol
  • the cleaned brake fluid is suitable as a cetane number improver in diesel fuels (see Pecci at the alcohol symposium)
  • Cooling fluids are generated in a motor vehicle mechanic operation. Because of the prohibition of mixing hazardous waste, the effort involved in collecting, storing and transporting it is considerable. They have a heating value that is only half as high as used oil. The costs for disposal are about DM 1000, - / t.
  • An upgrade according to the invention consists in contacting the used coolant with one (adsorption and / or separation aid and / or extraction agent) which, if possible, has a calorific value which contains carbon and which is degradable by hydrolysis. Since the degree of soiling fluctuates from delivery to delivery, the need for cleaning agents is determined in small-scale tests.
  • the cleaned coolant is suitable as a cetance number improver in diesel fuels or as an octane number improver in gasoline fuels, as a cooling starting aid for jet engines or in other gas turbines.
  • the chlorine-free solvents are hydrothermally treated with CaO milk and water at elevated to near-stoichiometric pressure.
  • Chlorinated substances are hydrothermally treated with CaO milk and water at high to near-stoichiometric pressure.
  • Chlorine is split off at lower temperatures. Then the other
  • Example 9 Upgrading water hyacinths to diesel fuel
  • the solution is to convert the collected water hyacinths into liquid energy materials, in particular diesel fuel, using the biomass present there according to the inventive method.
  • the invention also makes it possible to extract these substances by contacting the waste water with uncontaminated substances. Straw, steamed biomass and plastics or materials that are processed into a fuel in the method according to the invention. Pump Check Valve Closing Valve Sample Reservoir Check Valve

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Materials Engineering (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

Jusqu'à maintenant, les pétroles bruts, qu'ils soient naturels ou synthétiques, étaient d'abord séparés par distillation, puis enrichis. Dans un premier temps, les constituants contenant des hétéroatomes sont décomposés par distillation pour donner lieu à des matières dangereuses indésirables à faible teneur en hydrogène, telles que des hydrocarbures aromatiques polycycliques (HAP), des thiophènes, des pyrrolènes, des pyridines et des diènes, avant d'être éliminées à l'aide d'hydrogène à action enrichissante, qui est onéreux. Les matières sont d'abord enrichies avec de l'eau sans hydrogène, puis sont séparées. Comme la thermolyse sous eau pressurisée utilise de manière multiple et variée les propriétés des matières chargées, les matières dangereuses indésirables ne peuvent en aucun cas se développer. Par ailleurs, ce procédé permet d'améliorer les propriétés du produit et des eaux résiduaires et permet en outre de mettre en oeuvre des procédés de séparation à faible consommation d'énergie. Le réacteur permet de procéder simultanément à l'enrichissement autothermique/allothermique, ainsi qu'à la séparation du produit.
EP98955409A 1997-09-25 1998-09-24 Procede et dispositif d'evaluation de matieres premieres energetiques et chimiques par reaction de matieres premieres a cout reduit Withdrawn EP1027406A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19742266 1997-09-25
DE19742266A DE19742266A1 (de) 1997-09-25 1997-09-25 Aufwertung von Chemie- und Energierohstoffen durch Reaktion mit geringwertigen Rohstoffen
PCT/EP1998/006101 WO1999015605A1 (fr) 1997-09-25 1998-09-24 Procede et dispositif d'evaluation de matieres premieres energetiques et chimiques par reaction de matieres premieres a cout reduit

Publications (1)

Publication Number Publication Date
EP1027406A1 true EP1027406A1 (fr) 2000-08-16

Family

ID=7843551

Family Applications (1)

Application Number Title Priority Date Filing Date
EP98955409A Withdrawn EP1027406A1 (fr) 1997-09-25 1998-09-24 Procede et dispositif d'evaluation de matieres premieres energetiques et chimiques par reaction de matieres premieres a cout reduit

Country Status (4)

Country Link
EP (1) EP1027406A1 (fr)
AU (1) AU1226299A (fr)
DE (1) DE19742266A1 (fr)
WO (1) WO1999015605A1 (fr)

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102006020843B4 (de) * 2006-05-04 2008-03-06 Krause-Röhm-Systeme Ag Verwendung von Rotschlamm
DE102007056170A1 (de) * 2006-12-28 2008-11-06 Dominik Peus Semikontinuierliches Verfahren zur Herstellung von Brennstoff aus Biomasse
US7862708B2 (en) 2007-12-13 2011-01-04 Exxonmobil Research And Engineering Company Process for the desulfurization of heavy oils and bitumens
CN102213439B (zh) * 2010-04-01 2012-10-10 上海亚安电站辅机设备制造有限公司 一种无回油重油热喷燃烧系统
DE102010014768B4 (de) 2010-04-13 2021-10-28 Nexxoil Gmbh Verfahren zur thermischen Spaltung hochmolekularer organischer Abfälle
CN102252326B (zh) * 2010-05-19 2013-05-29 上海安大机械制造有限公司 一种环保型重油热喷燃烧系统
US8704019B2 (en) 2010-12-13 2014-04-22 Exxonmobil Research And Engineering Company Catalyst recovery in hydrothermal treatment of biomass
US8487148B2 (en) 2010-12-13 2013-07-16 Exxonmobil Research And Engineering Company Hydrothermal treatment of biomass with heterogeneous catalyst
US8704020B2 (en) 2010-12-13 2014-04-22 Exxonmobil Research And Engineering Company Catalytic hydrothermal treatment of biomass
US8624070B2 (en) 2010-12-13 2014-01-07 Exxonmobil Research And Engineering Company Phosphorus recovery from hydrothermal treatment of biomass
CN102491566B (zh) * 2011-12-30 2013-07-17 济南大学 一种多相催化氧化污水处理方法
CN106186628B (zh) * 2016-09-27 2019-08-23 华中科技大学 污泥水热处理及其废液催化气化同步反应装置
CN106810030B (zh) * 2017-01-04 2020-06-09 克拉玛依金鑫油田环保工程有限公司 油泥的安全处理方法
DE102018110296A1 (de) * 2018-04-27 2019-10-31 Linde Aktiengesellschaft Verfahren zur Behandlung einer sulfidhaltigen Ablauge
CN110950513B (zh) * 2019-11-26 2021-07-13 西安交通大学 一种利用表面活性剂预处理-水热氧化-热裂解耦合法处理罐底泥的方法
CN111450576B (zh) * 2020-04-15 2022-02-01 中国石油化工股份有限公司 一种油水分离装置及油水分离方法
CN112718806A (zh) * 2020-12-31 2021-04-30 福建省固体废物处置有限公司 填埋类物料有机质降解的处置装置及其方法
CN114380393B (zh) * 2022-01-25 2022-12-09 南京大学 一种负载二茂铁的耦合反硝化脱氮生物填料及其制备方法和应用
CN117965198B (zh) * 2022-10-24 2025-09-19 中国石油化工股份有限公司 用于原油裂解工艺的不饱和烃加氢方法
CN116573830B (zh) * 2023-04-20 2026-01-02 中交（天津）生态环保设计研究院有限公司 生态疏浚底泥温压耦合热相变式脱水干化系统及方法
CN116768689A (zh) * 2023-07-03 2023-09-19 国家能源集团宁夏煤业有限责任公司 用于乳化炸药的复合蜡

Family Cites Families (39)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB584671A (en) * 1942-11-13 1947-01-21 Baltzar Carl Von Platen Improvements relating to the removal of dissolved salts and other non-volatile substances from liquids
FR2079506A5 (fr) * 1970-02-03 1971-11-12 Salomone Georges
US3652405A (en) * 1970-06-15 1972-03-28 Texaco Inc Sewage and municipal refuse liquid phase coking process
FR2125770A5 (fr) * 1971-02-19 1972-09-29 Fusey Pierre
US4005005A (en) * 1974-05-31 1977-01-25 Standard Oil Company (Indiana) Process for recovering and upgrading hydrocarbons from tar sands
DE2440379A1 (de) * 1974-08-23 1976-03-04 Bayer Ag Verfahren zum entfaerben von gefaerbten abwaessern
DE2903056A1 (de) * 1978-01-26 1979-08-09 Budny Lucina Bindemittel mit absorptionseigenschaften und verfahren zur entfernung von substanzen aus gasen, pasten und pumpfaehigen medien mit dem bindemittel und rueckgewinnung der substanzen und des bindemittels
DE2850624A1 (de) * 1978-11-22 1980-06-04 Kneer Franz X Verfahren zur herstellung eines aufsaugenden oelbindemittels
US4450066A (en) * 1980-09-02 1984-05-22 Exxon Research And Engineering Co. Hydrothermal pretreatment to prevent scale during liquefaction of certain solid carbonaceous materials
GB2089831B (en) * 1980-12-18 1984-10-31 Univ Salford Ind Centre Conversion of municipal waste to fuel
DD214749A3 (de) * 1982-03-09 1984-10-17 Schwarze Pumpe Gas Veb Verfahren zur hydrierenden spaltung von altgummi und gummiabfaellen
FI840787A7 (fi) * 1983-03-03 1984-09-04 Rollan Swanson Raskasjuoksuisten raakaöljyn tislausjätteiden, kuten asfalteenien, hartsien tms. pilkkominen ja hydraus.
US4579562A (en) * 1984-05-16 1986-04-01 Institute Of Gas Technology Thermochemical beneficiation of low rank coals
DE3433088A1 (de) * 1984-09-08 1985-10-03 Wilhelm 7464 Schömberg Wissing Verfahren zur selektiven energiegewinnung aus festen brennstoffen, unter abtrennung von fluechtigen bestandteilen, schwefel und aschen und verwertung der anfallenden anorgan. bestandteile etc.
JPS61115994A (ja) * 1984-11-09 1986-06-03 Agency Of Ind Science & Technol セルロ−ス系バイオマスの液化方法
DE3442506C2 (de) * 1984-11-22 1987-04-16 Union Rheinische Braunkohlen Kraftstoff AG, 5000 Köln Verfahren zur Aufarbeitung von Kohlenstoff enthaltenden Abfällen
JPS61200928A (ja) * 1985-03-04 1986-09-05 Agency Of Ind Science & Technol 低級オレフインの製造方法
GB8511587D0 (en) * 1985-05-08 1985-06-12 Shell Int Research Producing hydrocarbon-containing liquids
DE3640573A1 (de) * 1985-11-28 1987-06-04 Suppan Friedrich Verfahren und anlage zur energiegewinnung aus giftigen abfallstoffen bei deren gleichzeitiger entsorgung
DE3602041C2 (de) * 1986-01-24 1996-02-29 Rwe Entsorgung Ag Verbessertes Verfahren zur Aufarbeitung von Kohlenstoff enthaltenden Abfällen
DE3623430A1 (de) * 1986-07-11 1988-01-28 Veba Oel Entwicklungs Gmbh Verfahren zur hydrierenden behandlung von mit chlorbiphenylen u. dgl. kontaminierten mineraloelen
DE3634275A1 (de) * 1986-10-08 1988-04-28 Veba Oel Entwicklungs Gmbh Verfahren zur hydrierenden konversion von schwer- und rueckstandsoelen
DE3642362A1 (de) * 1986-12-11 1988-06-16 Schill & Seilacher Mittel zur abtrennung dispergierter teilchen aus dispersionen
DE3713730A1 (de) * 1987-04-24 1988-11-10 Union Rheinische Braunkohlen Verbessertes verfahren zur aufarbeitung von kohlenstoff enthaltenden abfaellen und biomasse
US4775460A (en) * 1987-12-24 1988-10-04 Uop, Inc. Hydrocracking process with feed pretreatment
DE3917129A1 (de) * 1989-05-26 1990-11-29 Rheinische Braunkohlenw Ag Verfahren zur umweltfreundlichen abfallverwertung
US5151173A (en) * 1989-12-21 1992-09-29 Exxon Research And Engineering Company Conversion of coal with promoted carbon monoxide pretreatment
CA2042630A1 (fr) * 1990-09-27 1992-03-28 Louis O. Torregrossa Procede et appareil pour la valorisation des eaux usees
DE4104898A1 (de) * 1991-02-18 1992-08-20 Edama Gmbh Verfahren und bindemittel zum entfernen einer auf wasser schwimmenden fluessigkeitsschicht
DE4114526A1 (de) * 1991-05-03 1992-11-05 Envi Lab Electronics Gmbh Verfahren zum aufsammeln von oeligen substanzen, aerosolen, emulsionen etc. aus wasser
DE4203928A1 (de) * 1992-02-11 1993-08-12 Juergen Buil Bindemittel, insbesondere fuer mineraloelprodukte
US5248413A (en) * 1992-02-28 1993-09-28 University Of Kentucky Research Foundation Process for removing sulfur and producing enhanced quality and environmentally acceptable products for energy production from coal
DE4207233A1 (de) * 1992-03-07 1993-11-18 Geier Henninger Kurt Verfahren zur Herstellung von porösen Filterkörpern
DE4308959C2 (de) * 1992-07-09 1996-05-02 Dierig Holding Ag Verwendung eines Vliesstoffes aus natürlichen Materialien
DE9213809U1 (de) * 1992-10-15 1994-02-17 Deutsche Torfgesellschaft mbH, 26683 Saterland Ölaufsaugelement und Verpackung hierfür
DE4423089C2 (de) * 1994-07-01 1997-02-20 Wilhelm Schilling Verfahren zur Aufarbeitung von gebrauchten, mit Fremdstoffen verunreinigten Schmierölen
DE19530096C2 (de) * 1995-08-16 1998-04-09 Oeko Finanz Holding Luxembourg Verfahren zur Herstellung eines Aufnahmesubstrates
GB2311789B (en) * 1996-04-01 1998-11-04 Fina Research Process for converting wax-containing hydrocarbon feedstocks into high-grade middle distillate products
DE29705010U1 (de) * 1997-03-19 1997-07-10 FARU Forschungsstelle Dr. Kubsch Laboratorium für Analytik, Radiometrie und Umwelttechnologie GmbH, 01187 Dresden Bindemittel für Öle und flüssige Chemikalien

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9915605A1 *

Also Published As

Publication number Publication date
AU1226299A (en) 1999-04-12
WO1999015605A1 (fr) 1999-04-01
DE19742266A1 (de) 1999-05-06

Similar Documents

Publication Publication Date Title
EP1027406A1 (fr) Procede et dispositif d'evaluation de matieres premieres energetiques et chimiques par reaction de matieres premieres a cout reduit
Bolognesi et al. Biochar production from sewage sludge and microalgae mixtures: properties, sustainability and possible role in circular economy
US7507869B2 (en) Method for extracting oil from plant material
JP5036303B2 (ja) 有機材料、廃棄物材料または低価値材料を有用な生成物へと転換するための方法および装置
EP0073355B1 (fr) Procédé de fabrication d'hydrocarbures liquides
KR20070058673A (ko) 유기물, 폐기물 또는 저가치의 물질을 유용한 생성물로전환시키는 방법
Siagian et al. Circular economy approaches in the palm oil industry: Enhancing profitability through waste reduction and product diversification
Elliott et al. Conversion of a wet waste feedstock to biocrude by hydrothermal processing in a continuous-flow reactor: grape pomace
JP2008514422A (ja) 有機物質を付着不溶性固体から分離し、有用な製品へ転化するための装置および方法
CN103911171A (zh) 由城市固体垃圾制备生物燃料的综合方法
DE3412536A1 (de) Verfahren zur herstellung von kohlenwasserstoffen aus klaerschlamm
JP2009511734A (ja) 有機廃棄物質および非有機廃棄物質の有用生成物への転換方法
Abonyi et al. Kinetic modeling and half-life study on bioremediation of crude oil dispersed by palm bunch enhanced stimulant
DE10215679B4 (de) Direkte thermochemische Umwandlung von hochmolekularen organischen Substanzen in niedrigviskose flüssige Brennstoffe
DE19532802C1 (de) Verfahren und Vorrichtung zur Verwertung von Schleifschlämmen
DE102006061217B3 (de) Verfahren zur thermischen Aufbereitung von Klärschlamm und Einrichtung zur Durchführung des Verfahrens
CN103402930B (zh) 由来自废水净化设备的污泥制备生物油的集成方法
EP1910499A2 (fr) Procede et dispositif de transformation thermochimique de substances organiques en produits organiques de grande valeur
EP3692012B1 (fr) Procédé de production de substances valorisables
DE69129588T2 (de) Bioentschwefelung von bitumen-brennstoffen
Hussain et al. Production of highly upgraded bio-oils through two-step catalytic pyrolysis of water hyacinth
DE102008047563A1 (de) Verfahren und Vorrichtung zur Aufbereitung von kunststoffhaltigen Stoffen
DE2832848A1 (de) Fluessigbrennstoff und verfahren zu dessen herstellung
Koo et al. Treatment of oily waste using activated carbon from agriculture waste
DE10232976A1 (de) Verfahren zur Konzentration von Fettabscheiderinhalten

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20000425

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

RAX Requested extension states of the european patent have changed

Free format text: LT PAYMENT 20000425;LV PAYMENT 20000425;SI PAYMENT 20000425

17Q First examination report despatched

Effective date: 20010521

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20040401