EP1976961A1 - Procédé de production de combustibles à partir de déchets gras végétaux et animaux, et installation destinée à la mise en oeuvre de ce procédé - Google Patents

Procédé de production de combustibles à partir de déchets gras végétaux et animaux, et installation destinée à la mise en oeuvre de ce procédé

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Publication number
EP1976961A1
EP1976961A1 EP06805989A EP06805989A EP1976961A1 EP 1976961 A1 EP1976961 A1 EP 1976961A1 EP 06805989 A EP06805989 A EP 06805989A EP 06805989 A EP06805989 A EP 06805989A EP 1976961 A1 EP1976961 A1 EP 1976961A1
Authority
EP
European Patent Office
Prior art keywords
reaction
fatty acids
fat
free fatty
fats
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Withdrawn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
EP06805989A
Other languages
German (de)
English (en)
Inventor
Stefan Farwick
Ludger Overmann
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.)
Wulfenia Beteiligungs GmbH
Original Assignee
Wulfenia Beteiligungs GmbH
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 Wulfenia Beteiligungs GmbH filed Critical Wulfenia Beteiligungs GmbH
Publication of EP1976961A1 publication Critical patent/EP1976961A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Definitions

  • the present invention relates to a process for the recovery of fuels from fat waste based on vegetable and animal fats and the fuels produced therefrom and their use.
  • the present invention equally relates to a system for carrying out the method according to the invention.
  • Fats and oils is the collective name for solid, semi-solid or liquid, more or less viscous products of the plant or animal body, which consist chemically essentially of glycerol esters of higher fatty acids. Fats and oils are therefore triglycerides, d. H. Ester compounds of glycerol with various fatty acids, in particular higher fatty acids. In general, such fatty acids are referred to as higher fatty acids containing more than twelve carbon atoms in the molecule. In the usual triglycerides, one molecule of glycerol binds three molecules of fatty acid. The fatty acids contained in the respective triglyceride vary widely and are species-dependent.
  • oils and fats outweighs the proportion of unsaturated and polyunsaturated fatty acids, which in this case z.
  • it can be oleic acid or linoleic acid
  • saturated fatty acids mainly palmic acid
  • the proportion of monounsaturated fatty acids, mainly oleic acid, and the saturated fatty acids, mainly palmitic and stearic outweighs the high melting point of animal fats compared to vegetable fats and oils.
  • fats and oils can be referenced, for example, Römpp Lexikon Chemie, 10th edition, Volume 2, 1997, Georg Thieme Verlag Stuttgart / New York, pages 1320 to 1322, keyword: "fats and oils”.
  • fats and oils are regenerative biogenic energy stores and thus suitable as fuels.
  • fuels is understood to mean, in particular, a summary designation for solid, liquid or gaseous substances, which can be utilized either in natural form or derived therefrom by refinement with atmospheric oxygen. Heat can be burned economically (see Rompp Lexikon Chemie, loc. cit., Volume 1, 1996, pages 513/514, keyword: "fuels").
  • fats and oils can be used as fuels, for example for the operation of internal combustion engines.
  • many accompanying substances of fats and oils are not desirable for technical use: pure fats and oils are odorless and tasteless; however, upon prolonged storage, they become rancid under the influence of light and / or air due to autoxidation and desmolysis, enzymatic or oxidative degradation to malodorous, short-chain ketones and aldehydes.
  • decomposition processes occur with elimination of glycerol, which gives rise to mono- and diglycerides and, above all, free fatty acids.
  • the abovementioned decomposition or decomposition products can be co-incinerated, but have a disadvantageous effect on the exhaust gas compositions and have a particularly corrosive effect with respect to internal combustion engines.
  • a high fatty acid content leads to a strong corrosive wear of internal combustion engines.
  • DE 199 56 599 A1 describes a process for the preparation of deacidified fats and oils, wherein technical triglycerides having acid numbers of up to 60 in the presence of lipases are treated with lower aliphatic alcohols so that a precesterification product having an acid number in the range of 0 , 5 to 10 results, and the reaction product after removing water and unreacted alcohol and subsequent drying with re-addition of lower aliphatic alcohols is subjected to a post-esterification, in the course of which the acid number of the starting materials to values in the range of 0.1 is lowered to 0.5.
  • DE 101 55 241 Cl describes a process for the production of fuels from acidic vegetable or animal fats containing free fatty acids by catalytic esterification reaction in a tower apparatus, wherein the free fatty acids contained in the acidic fats at elevated temperature and under vacuum with polyvalent Alcohols in the presence of solid neutral metal catalysts, which are present in a fixed bed within the reaction system, are esterified, wherein the acidic fats in the reaction system from top to bottom and this countercurrently passed the alcohol and under the influence of the vacuum, a mixture containing alcohol and water in the Upper part of the reaction system is withdrawn.
  • the method described there is associated with a number of disadvantages: First, the method described there is mandatory the use of a metal catalyst ahead; Although this metal catalyst is present in a fixed bed, certain amounts of the metal catalyst are always introduced into the processed fats, which must necessarily be removed by incineration of the processed fats by acidic scrubbing. In addition, the catalytic activity is quickly exhausted by the formation of gums as reaction by-products which deposit on the catalyst surface, so that they must be frequently regenerated or replaced. In addition, the process described in DE 101 55 241 Cl requires a complex tower apparatus and a complex process, since the acidic fat on the one hand and the esterification alcohol on the other hand must be conducted in countercurrent.
  • the present invention is therefore an object of the invention to provide a method and a corresponding system, can be obtained with or from the fuel substances starting from vegetable and / or animal fat waste, which in addition to fats and / or oils free fatty acids, and / or can be removed or reacted with or with the free fatty acids from vegetable and / or animal fats or oils, in particular fat waste.
  • the Applicant has now surprisingly found that in the case of acid fats and oils, especially in the case of free fatty acids containing vegetable and / or animal fat wastes, the free fatty acids in the absence of enzymatic and solid neutral catalysts, especially in the absence of metallic catalysts, in an esterification reaction with polyhydric alcohols to the corresponding esters, provided that reaction temperatures above 220 ° C are selected.
  • the present invention therefore proposes a method according to claim 1 or a system according to claim 24. Further, advantageous embodiments of the method and the inventive system are the subject of the respective subclaims.
  • the subject matter of the present invention is thus a process for the recovery of fuels from vegetable and / or animal fat waste, which ben fats and oils containing free fatty acids, wherein the fatty acids contained in the fat waste at reaction temperatures T reaction above 220 0 C (T reaction > 220 0 C) with at least one polyhydric alcohol in the absence of enzymatic and solid neutral catalysts are reacted such that an esterification of the free fatty acids takes place.
  • reaction or reaction temperature above 220 0 C (T reaction > 220 0 C, wherein the lower limit of 220 0 C is not included) is chosen because under these conditions a at least substantially complete reaction of the free fatty acids or an at least substantially complete esterification of the free fatty acids to the corresponding esters, and this without the relevant catalysts and without significant decomposition or denaturation of the fats and oils treated in this way.
  • any fat waste of plant and / or animal origin can be used by the process according to the invention.
  • the term fat waste is used in simplified form as a collective term for wastes based on fats and / or oils. These include, for example, wastes based on animal fats, waste fats, covering fats, industrial residual fats, fats from oil separators, fats from sewage treatment plants, fats from tanneries and acidic vegetable fats or oils.
  • waste based on land animal fats in particular pork fat, beef tallow, mutton tallow, horse fat or goose fat and chicken fat, but also on the basis of acidic fish oils can be used.
  • the acidic fats and oils used according to the invention may be, for example, non-particularly in need of monitoring fat waste for utilization of food processing companies, which are required by the Water Resources Act (WHG), upstream of discharging the wastewater before a light material shutdown, or other animal and vegetable fats and oils with a high content of so-called free fatty acids.
  • WG Water Resources Act
  • fat waste with a content of free fatty acids of 25 wt .-%, based on the fat waste used preferably fat waste with a content of free fatty acids of 25 wt .-%, based on the fat waste used.
  • fat waste with a lower content of free fatty acids can be used; however, in the event that the free fatty acid content is below 25% by weight, based on the fat wastes, it may be advisable to add a base starting catalyst, especially in the form of an inorganic hydroxide, but this measure may be optional less preferred according to the invention.
  • the process according to the invention leads to an at least substantially complete conversion of the free fatty acids contained in the fatty wastes to the corresponding fatty acid esters.
  • the polyhydric alcohol used can be an at least dihydric alcohol, in particular an at least trihydric alcohol, preferably a dihydric to tetrahydric alcohol.
  • the polyhydric alcohol is particularly preferably selected from the group of diols, such as ethylene glycol, triols, such as glycerol, pentaerythritol and pentitols, in particular from the group of ethylene glycol and / or glycerol. Mixtures of different polyhydric alcohols are also suitable according to the invention.
  • glycerol is used as the polyhydric alcohol.
  • the glycerol as a trivalent alcohol can bind a larger amount of fatty acids and thus provides a favorable mass balance.
  • glycerol has the particular advantage that the fatty acids are predominantly converted into triglycerides, which chemically equate to the main mass of fat waste to be processed.
  • mono- and di-glycerides are also formed, so that in general a mixture of various glyceryl esters, in particular mono-, di- and triglycerides, is formed, the triglycerides generally forming the main constituent.
  • Glycerol also has the advantage that it is available relatively inexpensively in technical form. Although technical glycerol has a relatively high water content, but before the reaction readily, for example, by evaporation or removal of the water from the mixture to be reacted before reaction, can be removed. However, care should be taken that, in the case of the use of technical grade glycerol, this is substantially free of methanol and / or ethanol to prevent competing esterification reactions of the reacted free fatty acids with methanol and / or ethanol.
  • the reaction of the free fatty acids is carried out with an excess of polyhydric alcohol, based on the free fatty acids contained in the fatty wastes.
  • an excess of from 5 to 40% by weight, preferably from 10 to 30% by weight, more preferably from 15 to 20% by weight, of the polyhydric alcohol is carried out with respect to the free fatty acids contained in the fatty wastes.
  • the excess of polyhydric alcohol refers to the mass of the total put polyhydric alcohol.
  • excess unreacted polyhydric alcohol can be separated or recovered again after conversion and subsequently recycled.
  • the separation of the excess polyhydric alcohol, especially glycerol, after the reaction is relatively unproblematic, since after cooling the reaction mixture results in a two-phase mixture - the polyhydric alcohol, especially the glycerol, is immiscible with the fats and oils -, so that the unreacted easily disassociate polyhydric alcohol.
  • the thus separated excess unreacted polyhydric alcohol can then be recycled to the next reaction batch.
  • reaction or esterification reaction is carried out as previously described in general at reaction temperatures T reaction in the range of above 220 0 C (lower limit not included) to 270 0 C, in particular 225 0 C to 265 0 C, preferably 225 ° C to 250 0 C, Particular preference is given to 230 ° C. to 240 ° C. Care should be taken that the reaction is carried out at temperatures which are below the boiling point of the polyhydric alcohol used.
  • the reaction or reaction is carried out in a stirred reactor which is equipped with the appropriate stirring devices for mixing the reaction mixture. It has proven to be particularly advantageous if, in addition to the stirring devices, the stirred reactor has at least one nozzle for atomizing, ie atomizing or finely distributing the reaction mixture, the reaction mixture being continuously atomised, in particular atomized, by the nozzle during the reaction and / or or finely distributed. This can speed up the implementation. Without wishing to be bound by any particular theory, the reaction thus accelerated can be explained by an enlargement of the reaction surface.
  • the nozzle may be arranged so that it dips into the reaction mixture, wherein withdrawn via a line located at the bottom of the stirred reactor, a portion of the reaction mixture continuously and dipping into the reaction mixture Nozzle head is supplied for the purpose of atomization.
  • the reaction mixture is mixed in the reaction by stirring with the corresponding stirring devices or stirrers and preferably also atomized by an additionally existing nozzle ("esterification nozzle"), ie atomized or finely distributed.
  • reaction will be discontinuous, i. H. batchwise or batchwise.
  • the water of reaction formed in the reaction is continuously withdrawn. This is done by means of continuous evaporation or removal of the resulting water of reaction, since working at temperatures above the boiling point of water.
  • a slight negative pressure is applied for this purpose, in particular in the range of 100 to 300 mbar, in particular 150 to 250 mbar.
  • reaction or reaction is carried out at atmospheric pressure or at reduced pressure, in particular at reduced pressure in the range of 100 to 300 mbar, in particular 150 to 250 mbar.
  • the reaction takes place in such a way, in particular over such a period of time, that the conversion of the fatty acids to the corresponding esters takes place to at least 95%, in particular at least 97%, preferably at least 98%, very particularly preferably at least 99% ( Degree of conversion).
  • the reaction is generally carried out in such a way, in particular over such a period of time, that the content of free fatty acids after the reaction at most 2 wt .-%, in particular at most 1 wt .-%, preferably at most 0.5 wt .-%, particularly preferably at most 0, 1 wt .-%, most preferably at most 0.05 wt .-%, based on the product mixture obtained after the reaction (ie, the neutralized fats and / or oils), is.
  • the reaction mixture obtained after the reaction generally has an acid number of at most 4, in particular at most 2, preferably at most 1, more preferably at most 0.2, most preferably at most 0, 1, on.
  • the reaction as such is generally carried out for a period of 0.1 to 5 hours, more preferably 0.5 to 4 hours, preferably 0.75 to 1.5 hours.
  • the fatty wastes to be neutralized or transesterified are generally subjected to physical treatment before the actual reaction or reaction with the polyhydric alcohol.
  • the physical treatment comprises in particular a (physical) separation of water contained in the fat waste, for example by decantation, in particular a residual water content ⁇ 0.5 wt .-%, based on the fat waste, is set.
  • the physical treatment comprises a mechanical separation of solids, preferably by sieving and / or filtration, the fat waste being adjusted to residual solids contents ⁇ 0.1% by weight, based on the fat wastes.
  • the fat waste is thus freed of excess water on the one hand and solids or sediments on the other hand.
  • the fatty wastes processed in this way can then be stored, if appropriate, before their subsequent reaction with the polyhydric alcohol, in a buffer tank until a sufficient amount has been accumulated in the buffer tank for the subsequent reaction or reaction.
  • the post-processing generally comprises a physical separation of solids formed in the reaction products in the reaction, in particular mucilages, such as may arise in particular by denaturing the fats and oils;
  • the separation of the solids, in particular gums is preferably carried out by means of filtration ("polishing filtration"), in particular using filter aids (for example cellulose, silica gel, kieselguhr, perlites, charcoal or wood flour).
  • the post-processing comprises a separation of the excess unreacted polyhydric alcohols contained in the reaction products, in particular by means of phase separation (The polyhydric alcohols are generally combined with the product mixture of fats and / or oils immiscible.); As described above, excess unreacted polyhydric alcohol is then advantageously recycled.
  • reaction products obtained by the process according to the invention may, if appropriate after intermediate storage in a buffer tank, subsequently be used as the fuels of a heat engine, in particular
  • Vehicles of any kind such as ships, or serve in power plants for power generation.
  • the inventive method thus enables efficient recovery of neutralized fat and / or oil mixtures starting from acid, fatty acid-containing Trustfett- and / or -ölgemischen, especially Fettabpart- len, and thus of biogenic fuels.
  • the process according to the invention surprisingly comes without catalysts, so that it works on the one hand cost and less complex in the Anlagensbowung than processes that work with catalysts, and on the other hand the risk of the introduction of catalysts is excluded in the final products.
  • the starting raw materials are acid fat and / or oil mixtures or fat waste with a content of free fatty acids of at least 25% by weight or with acid numbers of at least 50 and / or if with an excess of the polyhydric Alcohol will proceed in terms of the free fatty acids, since in this case the reaction proceeds in a very short time and at particularly good conversion rates.
  • Another object of the present invention are - according to a second aspect of the present invention - the neutralized fats and / or oils obtainable by the method according to the invention starting from acidic (ie containing starting from free fatty acids) vegetable and / or animal fat wastes as such Fuels based on vegetable and / or animal fats.
  • the neutralized fats and / or oils or fuels obtainable by the process according to the invention are characterized by a low content of free fatty acids of at most 2% by weight, in particular at most 1% by weight, preferably at most 0.5% by weight, special ders preferably at most 0, 1 wt .-%, most preferably at most 0.05 wt .-%, based on the neutralized fats and / or oils or fuels, from, which in about acid numbers of at most 4, in particular at most 2, preferably at most 1, particularly preferably at most 0.2, very particularly preferably at most 0.1.
  • the products obtainable by the process according to the invention generally comprise a mixture of mono-, di- and triglyceridic fats and / or oils (ie a mixture of different glycerol esters) when using polyhydric alcohol as glycerol, the triglycerides generally being the major fraction form.
  • Another object of the present invention - according to a third aspect of the present invention - is the use of the neutralized fats and / or oils or (biogenic) fuels obtainable by the process of the invention for operating a heat engine, in particular an internal combustion engine, or for operating a power plant or for power and / or heat generation.
  • a further subject matter of the present invention is a plant for carrying out the process according to the invention described above, the plant comprising, in the order of the process steps to be carried out and in each case one after the other, the following units: a treatment unit i for the physical treatment of vegetable and / or animal fat waste, which in addition to fats and / or oils free fatty acids and a certain proportion of water and solids (The treatment unit i can in particular a device for the physical separation of water, in particular a decanter, and / or a device for separating solids, in particular a screening and / or filtering device.); b) in the production line downstream of the treatment unit I optionally a buffer tank 2 for receiving and / or intermediate storage of the physically treated fat waste originating from the treatment unit i; c) in the production line downstream of the treatment unit I and / or the optional buffer tank 2, a reactor unit 3. to
  • the reaction unit 3 is formed heatable via a heating medium £, and the reactor unit 3_ can from a storage tank 4 esterification alcohol and from the processing unit i and / or the possibly existing buffer tank 2, the physically treated fat waste, preferably as separate educt streams, are supplied.); d) in the production line downstream of the reactor unit 3 optionally an intermediate tank 7 for receiving and / or intermediate storage, in particular for purposes of cooling, originating from the reactor unit Commanderrohgemisches (The intermediate tank 7 can with a heating medium 8, in particular a heat exchanger, for the removal of heat and their return be coupled into the reactor unit 3_.).
  • the system according to the invention e) in the production line downstream of the reactor unit 3 and / or the intermediate tank 7 may include a post-processing unit 9 for the physical post-processing of the product mixture originating from the reactor unit 3_ and / or the optionally existing intermediate tank 7
  • the post-processing unit 9 can in particular Device for the physical separation of solids, in particular of mucins formed in the reaction, preferably a filtration device, and / or a device for the physical separation of water, in particular a decanter and / or centrifuging comprise.).
  • the plant f) downstream of the post-processing unit 9 can comprise a tank K) for receiving and / or intermediate storage of the post-unit 9 post-processed, in particular, polished product mixture (the tank JjO can in particular at its lower part, in particular at the foot of the Tanks K), a pipe for extracting unreacted, settling at the foot of the tank JJO Esterification alcohol and for its return to the storage tank 4 include).
  • the various, series-connected in production line units, tanks, containers and the like i, 2, 3, 4, 7, 9 are advantageously connected to each other via lines.
  • the individual lines are preferably able to be shut off and / or formed separately from one another in a controllable manner.
  • the reactor unit 3. of the system according to the invention can, in a particularly advantageous embodiment, additionally have a nozzle 6 for atomising and / or finely distributing the reaction mixture.
  • the nozzle 6 can be arranged such that it dips into the reaction mixture in the operating state of the reactor unit 3, wherein a via at the bottom of the Reaktorein- unit 3_, in particular at the foot of the reactor unit 3, located line (“loop") removable reaction mixture and can be fed into the nozzle 6.
  • the plant according to the invention is integrated in a power plant, in particular in a combined heat and power plant (CHP) or its component.
  • at least one heat engine in particular at least one internal combustion engine, can be connected downstream of the system according to the invention for generating electricity and / or for heat generation by burning the fat waste processed in the system according to the invention.
  • the single FIGURE shows a schematic, simplified sequence of the method according to the invention or a schematic, simplified structure of a system according to the invention:
  • the waste fat to be processed may be, for example, waste not requiring special monitoring for use in food-processing establishments which are required by the Water Resources Act (WHG) to precede the discharge of water with a light-weight separator, or waste based on animal and vegetable fats with a high Content of so-called free fatty acids as described above.
  • WSG Water Resources Act
  • the residual water content is here advantageously to values below 0.5 wt .-%, based on the raw materials, and the residual solids or residual sediment content to values ⁇ 0, 1 wt .-% at a grain size of 50 microns, each based on the Raw materials, discontinued. These are optional entry requirements for the downstream chemical treatment or conversion.
  • the liberated in the physical preparation J, of water and solids or sediments waste fats may optionally be temporarily stored in a buffer tank 2, from where they then the chemical treatment system and the reactor 3_, derived together with from the supply tank 4 polyhydric alcohol, preferably glycerol , can be supplied to the esterification of the free fatty acids.
  • polyhydric alcohol preferably glycerol
  • the free fatty acids contained in the crude fats and oils generally with fatty acid contents above 25 wt .-%, based on the fat waste, in the absence of enzymatic and solid neutral catalysts with the alcohol or Glycerol reacted in stoichiometric excess in the manner according to the invention at temperatures above 220 0 C, especially in the corresponding glycerol esters, mainly triglycerides, converted, wherein mono- and diglycerides are formed as by-products.
  • the advantage of the reduction or dismantling that takes place in this way The content of free fatty acids is such that even raw materials containing large amounts of free fatty acids can be processed without loss of mass - in contrast to prior art processes which remove the free fatty acids by alkaline scrubbing.
  • the reactor 3 is brought to the appropriate reaction temperature via a corresponding heating medium 5.
  • at least one nozzle (“esterification nozzle") 6 for atomizing, in particular atomizing or finely distributing, the reaction mixture is present in the reactor 3.
  • the reaction mixture to be atomized fed to the nozzle 6 via a line or Conduction loop ("loop") in the lower part of the reactor 3_, in particular at the bottom of the reactor 3, is withdrawn.
  • the product After completion of the esterification reaction, the product is fed to a tank 7 for the purpose of cooling, wherein the heat released during the cooling can be returned to the esterification via a heating medium or a heat exchanger%.
  • the cooled product is freed from gums by polishing filtration in 9, generally using filter aids (eg, perlites), and the resulting cake can be stored, for example, in a watertight container until disposed of properly.
  • the plant according to the invention described below is a combined heat and power plant with a rated thermal input below 20 MW, in the biogenic fuels based on processed animal and / or vegetable fats for electricity and heat generation according to the law for the promotion of renewable energies (EEG) or biomass regulation (BiomasseV).
  • EEG renewable energies
  • BiomasseV biomass regulation
  • the grease separator contents are directed to a leveling or vacuum vessel, which is level monitored.
  • the raw material is homogenized by means of a screw pump and fed into a tank garden, where the delivered grease separator contents are stored until processing.
  • the tank garden consists of two standing tanks with a useful volume of 400 m each, with both tanks being heated to a temperature of 35 ° C. by means of a heat cycle from the power plant. The tanks are filled alternately over the acceptance area. The heating and a continuous mixing of the tank contents takes place with the help of a heat exchanger.
  • the raw The material is drained from the tank at the bottom, passed through a heat exchanger and returned to the tank from above.
  • the heated fat / water mixture is then pumped out of the tank via a heated piping system into the physical treatment.
  • the physical treatment consists of a three-phase decanter and a separator.
  • the fats are pumped from the tank garden via the heated pipe system directly into the decanter.
  • the fat / water mixture is heated via the heat cycle of the CHP to a temperature of 80 0 C.
  • the water which has been cut off in the decanter is sent to wastewater treatment, separated sediments are discharged with a compression screw and stored in a watertight container until they are disposed of properly.
  • the resulting grease is further heated to a temperature of 95 0 C over the heat cycle of the power plant and cleaned in the separator.
  • the water phase which has been cut off here is in turn fed to wastewater treatment, sediments are stored in a watertight container until they are disposed of properly.
  • the containers for storing the sediments are provided with an active ventilation system, whereby the exhaust air is cleaned by a corresponding biofilter in order to avoid possible odor emissions.
  • the fat obtained in the physical treatment is stored in a buffer tank with a volume of 50 m until further treatment in the chemical treatment.
  • the chemical treatment of the fats takes place in batch mode. This gives 60 t of fuel (mixture of mono-, di- and triglycerides or glycerol ester mixture) in 4 batches (batches) per 24 hours.
  • the fats are conveyed from the buffer tank of the physical treatment via a piping system in the reactor and heated by the high-temperature circuit of the power plant to a temperature above 220 0 C, in particular to about 230 0 C to about 245 0 C.
  • the free fatty acids contained in the fat waste are reesterified in the absence of catalysts. Reesterification takes place without pressure over a period of about one and a half hours.
  • the reactor is a stirred reactor with stirring tools for mixing the reaction mixture and one or more additional, immersed in the reaction mixture esterification for atomizing the reaction mixture
  • the product is freed of mucilage in the course of a polishing filtration using filter aids by means of a chamber filter press.
  • the presscake is stored in a watertight container until properly disposed of.
  • the cleaned product is pumped into the fuel tanks via a double-walled, heated pipe system.
  • the fuel storage facility consists - as does the tank garden - of two tanks with a volume of 400 m each.
  • the tanks are single-walled and equipped with a vacuum floor, a level control and a leak detector. Furthermore, they are secured by an upstand as collision protection.
  • the combustion engines of the CHP are operated exclusively with the fuel obtained as described above.
  • This fuel has ren the property mecanickristallisie- at temperatures below 30 0 C. Therefore, the fuel storage and the fuel lines are heated by means of a heat cycle of the power plant during normal operation of the power plant to the optimum viscosity to obtain the fuel. If the power plant is shut down, it must be ensured that no fuel remains in the lines and machines and hardens there. For this reason, conventional diesel is used as fuel for starting and stopping the power plant.
  • the internal combustion engines of the power plant are two diesel engines each with 3.257 MW of electrical power installed.
  • the engines are 9-cylinder / 4-stroke inline engines with supercharging and intercooling. They are originally designed for ship propulsion and now converted for operation with the biofuel produced according to the invention.
  • Each motor is coupled to a three-phase synchronous generator. The electrical energy generated is fed via a 10 kV switchgear into a 10 kV power supply network.
  • Each engine-generator unit is followed by a NO x reduction system for cleaning the resulting flue gases.
  • the hot combustion gases of the diesel engines are used to heat a thermal oil for the so-called high-temperature cycle to 250 ° C.
  • the power plant is designed for the generation of electricity in continuous operation.
  • the chemical energy of the abandoned fuels is converted by combustion into heat energy.
  • the two engines deliver a thermal output of 8.6 MW.
  • the heat energy is supplied via the hot exhaust gases to the exhaust gas boiler.
  • the largest part of the heat is, as described above, absorbed by a thermal oil as a carrier medium.
  • the wastewater produced during the fuel treatment is purified in a water treatment plant which comprises a grease separator, a feed tank and a flotation plant.
  • the water treatment plant causes a residual separation of emulsified hydrocarbons and heavy metals after pretreatment by a separator. Subsequent cleaning of the waste water ensures compliance with the limit values with regard to pH, hydrocarbons, lipophilic substances and heavy metals. COD and BOD levels are greatly reduced.

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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)
  • Liquid Carbonaceous Fuels (AREA)
  • Fats And Perfumes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de production de combustibles à partir de déchets gras végétaux et/ou animaux contenant non seulement les graisses et/ou huiles mais aussi des acides gras libres. Les acides gras libres contenus dans les déchets gras peuvent réagir avec au moins un alcool polyvalent en présence de catalyseurs enzymatiques et neutres solides à des températures de réaction supérieures à 220 °C de manière à entraîner une estérification des acides gras libres.
EP06805989A 2006-01-23 2006-10-02 Procédé de production de combustibles à partir de déchets gras végétaux et animaux, et installation destinée à la mise en oeuvre de ce procédé Withdrawn EP1976961A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102006003328 2006-01-23
DE102006019763A DE102006019763B4 (de) 2006-01-23 2006-04-28 Verfahren zur Gewinnung von Brennstoffen aus pflanzlichen und tierischen Fettabfällen sowie Anlage zur Durchführung des Verfahrens
PCT/EP2006/009544 WO2007087838A1 (fr) 2006-01-23 2006-10-02 Procédé de production de combustibles à partir de déchets gras végétaux et animaux, et installation destinée à la mise en oeuvre de ce procédé

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EP (1) EP1976961A1 (fr)
JP (1) JP2009523866A (fr)
CA (1) CA2637799A1 (fr)
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WO (1) WO2007087838A1 (fr)

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FR2951194B1 (fr) * 2009-10-14 2015-05-15 Olva Technologies Dispositif de production d'un biodiesel
US8952210B2 (en) * 2010-07-13 2015-02-10 Kior, Inc. Solids removal from bio-oil using biomass filter aid
US9222044B2 (en) 2010-07-26 2015-12-29 Uop Llc Methods for producing low oxygen biomass-derived pyrolysis oils
KR101297495B1 (ko) 2010-09-27 2013-08-16 삼성석유화학(주) 지방산 알킬에스테르의 제조방법
WO2014190436A1 (fr) * 2013-05-29 2014-12-04 Polyvalor Limited Partnership Procédé et système de production d'un ester d'alkyle d'acide gras
KR20180067261A (ko) * 2016-12-12 2018-06-20 에너바이오 주식회사 바이오 중유를 제조하는 방법
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JP2009523866A (ja) 2009-06-25
DE102006019763B4 (de) 2009-04-09
DE102006019763A1 (de) 2007-08-02
CA2637799A1 (fr) 2007-08-09
US20100058652A1 (en) 2010-03-11

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