EP3098291B1 - Verfahren zur aufbereitung von altöl - Google Patents

Verfahren zur aufbereitung von altöl Download PDF

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Publication number
EP3098291B1
EP3098291B1 EP16164521.3A EP16164521A EP3098291B1 EP 3098291 B1 EP3098291 B1 EP 3098291B1 EP 16164521 A EP16164521 A EP 16164521A EP 3098291 B1 EP3098291 B1 EP 3098291B1
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EP
European Patent Office
Prior art keywords
fraction
oil
pipeline
bitumen
column
Prior art date
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Application number
EP16164521.3A
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English (en)
French (fr)
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EP3098291A1 (de
Inventor
Francesco Gallo
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.)
Itelyum Regeneration SpA
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Viscolube Srl
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0016—Working-up used lubricants to recover useful products ; Cleaning with the use of chemical agents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C10M175/0033—Working-up used lubricants to recover useful products ; Cleaning by thermal processes using distillation processes; devices therefor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C10M175/0041—Working-up used lubricants to recover useful products ; Cleaning by thermal processes by hydrogenation processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0058—Working-up used lubricants to recover useful products ; Cleaning by filtration and centrifugation processes; apparatus therefor

Definitions

  • the present invention relates to a regeneration process for waste oils, in particular mineral oils, aimed at obtaining a particularly clean product, suitable to be used as a lubricant base, increasing the enhancement of waste oil compared to the prior art processes.
  • Lubricating oils are used in almost all the fields of mechanics to allow engine parts or the like to slide on each other.
  • a classic example is that of oil used in internal combustion engines to help the sliding of the pistons in the cylinders, without the parts getting stuck into one another.
  • Lubricating oils are often used in machinery involving relative, very fast sliding movements of their parts. Because of this, in addition to other aspects, lubricating oils frequently undergo temperature changes, which are in some cases very remarkable. For this reason, oils undergo chemical reactions of various kinds and their nature is altered. So reactions such as cleavage, dehydration, dehydrogenation, condensation, etc. take place. An example of such a reaction is the dehydrogenation-dehydration of oils, which leads to the formation of carbon in the form of carbon black. In some cases, the formation of asphaltenes and bitumens also occurs. Furthermore, the oils can contact with other substances, such as, for example, metallic and/or ceramic particles, thus remaining inside the oil itself.
  • Waste oil contains a number of toxic substances, for which reason it cannot be simply discharged into the environment, but must be treated to reduce its environmental impact.
  • the regeneration of waste oils has thus emerged as a solution allowing to reduce waste and the resulting environmental impact.
  • the typical yield of a regeneration process starting from 100 kg of waste oil to be sent to the process, is now around 60 kg of regenerated oil (base for lubricants), 20-25 kg of fuel and 20-25 kg of bitumen.
  • the step of acid treatment is completely replaced by clarification with liquid propane.
  • the chosen hydrocarbon is propane for being easily liquefiable and having a low density once liquefied. It therefore acts as fluidifying agent on oils to which it is added, so as to allow the separation of a high-density phase - containing high molecular weight polymers and heavy metals - from a second fraction, constituted by clarified and dehydrated oils.
  • the propane is then removed and recycled by mixing with the in-fed oils.
  • a hot filtration is then performed, allowing the recovery of a gaseous fraction. Discolouration and deodorisation of the content are the final steps.
  • EP 0 618 959 discloses a process for re-refining waste oils, in which said oils are contacted with a basic reagent and heated to remove contained water, polymers and heavy metals are separated and fractioned distillation is performed in a packed column in order to obtain one or more base fractions for lubricants, followed by discolouration.
  • the basic reagent is a strong base, water is removed together with a more volatile fraction in a preliminary step of flash distillation, while polymers and heavy metals are removed mostly by decanting.
  • the packed distillation column tends to become clogged by solid residues, still contained in the oil to be fed inside the same.
  • WO2004/033 608 discloses a process and a device for the treatment of waste oils, which includes a preliminary separation by decanting of at least one fraction of the water and one fraction of solid particles (sediments), a preliminary heating of the oily phase from the decanting step and centrifugal separation of the oil, preheated to a temperature below the boiling point of water, followed by the separation of water and other pollutants.
  • the product obtained is not reused to produce new lubricant bases, but is fed to a combustion step, along with other hydrocarbons, therefore with no enhancement of the same.
  • WO96/00 273 discloses a process of reclamation of waste oils, with a view to their reuse. According to this document, waste oil undergoes a centrifugation as it is to remove solids; the output oil is then contacted with diammonium phosphate and/or oxalic acid at a temperature between 60 and 85-90°C and is then subjected to a new centrifugation to separate oil and water. There are no distillation steps.
  • CA 2 396 206 discloses a process for treating waste oils, comprising a dehydration step of waste oil, a subsequent fractioned distillation, managing the lowest plate of the column to a temperature between 370 and 390°C at a pressure comprised between 67 and 133 mbar, the intermediate plate at a temperature between 265 and 280°C at a pressure between 47 and 60 mbar and the top plate at a temperature between 100 and 110°C at a pressure between 40 and 53 mbar, recovering bitumen from the bottom of the column and extracting oil fractions of different density at the highest levels.
  • US2001/0 001 198 discloses a procedure for removing acidic compounds, colour, and polynuclear aromatic hydrocarbons from petroleum distillates using phase transfer catalysts, by adding suitable solvents and then removing them by distillation together with the contaminants.
  • the object underlying the invention is to propose a regeneration process of waste oils, overcoming the mentioned disadvantages and allowing for further enhancement of process effluents.
  • This object is achieved through a process for the regeneration of waste oils, comprising a step of flash distillation of the oil to be regenerated, a step of decanting of the heavy fraction, a step of distillation in a packed distillation column, allowing to produce an oil fraction suitable for being sent to hydrorefining and a bitumen fraction, characterised in that the bitumen fraction is ground, the liquid fraction obtained after grinding being separated and collected as bitumen and the remaining solid fraction being separated and recycled to said step of decanting of the heavy fraction.
  • a first embodiment of the process according to the present invention is represented as a block diagram in fig. 1 .
  • the oil to be regenerated arrives from the pipeline 1.
  • oil can be mixed with an alkaline substance.
  • a strong base is generally used, preferably KOH, which gave the best results.
  • the pipeline 1 feeds the oil to be regenerated to a flash distillation column 2.
  • the pressure inside the column 2 is maintained at about 330 mbar and the temperature is slightly higher than the boiling temperature of water, preferably about 130-140°C.
  • a substantial part of water contained in the oil, partly directly from waste oil, partly fed in 1 as the solvent of the basic substance is vaporised.
  • the vaporised water exits from a drain 3.
  • Only one decanter 5 is represented in fig. 1 , but the person skilled in the art can find practical reasons for providing two or more, without thereby departing from the scope of the present invention.
  • the further separation of oil from water and from a part of the solid particles contained in it occurs in the decanter.
  • the fraction to be subjected to the subsequent steps exits the decanter 5 through the pipeline 6.
  • the latter feeds the oil to be treated in a heat exchanger 7, preferably an oven, which brings the oil temperature to values above 300°C, preferably to values between 350° and 400°C, subsequently feeding it in a packed distillation column 8.
  • a heat exchanger 7 preferably an oven, which brings the oil temperature to values above 300°C, preferably to values between 350° and 400°C, subsequently feeding it in a packed distillation column 8.
  • some useful fractions are separated
  • the column 8 also outputs a bituminous tail fraction which, in the processes according to the prior art, is usually sold directly as bitumen.
  • the bituminous fraction exits the bottom of column 8 and is fed to a mixer 16 through a pipeline 15 in order to be homogenised.
  • a mixer 16 From the mixer 16, an outlet 17 feeds the mixed fraction to the grinding unit 18.
  • the unit 18 can be any type of grinding device. A ball mill is particularly preferred, but wedge mills, disc grinders and others can be used as well.
  • the unit 18 chops the solid particles contained in the bitumen, opening them and thus making available more oil to be regenerated. A more liquid part and a part that remains more solid are obtained.
  • Unit 18 has two outlets: an outlet 19, from which the liquid part of the product comes out, substantially a more liquid bitumen, containing less solid impurities than the one in the pipeline 15, thus having a higher value; and an outlet 20, from which the solid fraction comes out, containing, inter alia, the particles opened in the grinding step with the oil to be regenerated.
  • the outlet 20 feeds the solid fraction back to the decanter 5, where it mixes with the oil flow from the column 2 and the process begins again, releasing more oil for regeneration. In this way, process yield increases, allowing to obtain a higher amount of lubricant base (fine fraction), up to 67-70% by weight, and lower amounts of fuel and bitumen (poorer fractions).
  • Fig. 2 represents a block diagram of an alternative embodiment of the present invention. Elements identical to those of Fig. 1 are indicated with the same reference numbers.
  • Flows 9, 10, 11 and 12, output from the packed distillation column 8, are fed to a tank 21 which acts as a buffer, to allow the subsequent operations to be carried out discontinuously, load-wise or batch-wise.
  • a pipeline 22 leads to microfiltration unit 23, of a type known per se.
  • a flow 24 brings the liquid fraction to the reactor 13 to perform the hydrorefining and collect the produced lubricant base from the outlet 14.
  • a pipeline 15 carries the bitumen fraction from the packed distillation column 8.
  • the pipeline 15, joined by the pipeline 25, carry the bitumen fraction, containing solid particles, to the mixer 16 and from there, through the pipeline 17, to the grinding unit 18.
  • the pipeline 19 transports and discharges bitumen, more valuable than that obtainable according to the prior art, while the pipeline 20 recycles the solid part ground during the first process steps according to the present invention, bringing the lubricant base yield to higher levels.
  • the fraction fed to the reactor 13 is cleaner.
  • the fact that the flow being treated in the reactor 13 is cleaner causes a significant extension of the useful life of the catalyst used in this step; given that, although used in small quantities, the catalysts for hydrorefining are normally based on precious metals, a certain cost saving is achieved, increased by the reduction of performance interruptions due to catalyst replacement.
  • Fig. 3 represents the block diagram of a further alternative embodiment. Even in this case, the steps already described in relation to fig. 1 will carry the same reference numbers and will not be further described. This embodiment depends on a patent application recently filed by the same Applicant.
  • the oil to be treated exiting through pipeline 4 from the column 2 for flash distillation, is divided into two flows 4A and 4B, which feed respective decanters 5A and 5B, entirely similar to the decanter 5 described with reference to fig. 1 .
  • the fraction to be regenerated comes out from the decanters 5A, 5B through the pipelines 26A, 26B, and is fed to centrifugal separators 27A, 27B.
  • the part still to be treated (oil to be regenerated) is carried by pipelines 28A, 28B, which then gather in the pipeline 28, to a decanter 29.
  • the useful fraction output from the decanter 29 is then fed to the heat exchanger 7, usually an oven, where it is brought to a temperature higher than 300°C, typically between 350° and 400°C.
  • the fraction is then fed to the packed distillation column 8.
  • the column 8 is operated so as to have a tail pressure comprised between 10 and 20 mbar and a head pressure comprised between 2.5 and 9.5 mbar, in order to collect the best product.
  • pressure is adjusted, rather than by the ejectors commonly used for this purpose, by a liquid-ring pump. In this way, besides saving on costs related to steam and eliminating the need to manage a dedicated steam cycle, flows and pressure are more regular compared to what could be previously achieved with ejectors.
  • the column 8 outputs the useful product flows, through the pipelines 9, 10, 11 and 12, which go to the next step of hydrorefining, into the reactor 13; the produced lubricant bases are extracted from the reactor 13 through the pipeline 14.
  • a liquid-ring pump to adjust pressure inside the column 8, the fraction fed to the reactor 13 is particularly clean and the life of the catalyst contained in the reactor 13 is significantly extended.
  • Column 8 also outputs the tail flow from the pipeline 15. This flow, containing the bitumen fraction, is joined by flows 30 and 31, output from centrifugal separators 27A, 27B and containing the solid sediments separated from the oil in regeneration.
  • the pipeline 15 carries the bituminous fluid to the mixer 16 and from here, via the pipeline 17, to the grinding unit 18.
  • the liquid fraction obtained after grinding is collected from the pipeline 19 and sold.
  • the solid fraction is collected from the pipeline 20, which is divided into two flows 20A, 20B, respectively feeding decanters 5A, 5B.
  • the system used to implement the process according to the present invention is of the type comprising a flash distillation column 2, a number of decanters 5 or 5A, 5B, a packed distillation column 8 and a hydrorefining reactor 14 and also comprises a unit 18 for grinding the bitumen fractions and any process sediments.
  • the grinding unit 18 is a ball mill.
  • bitumen fraction that leaves the process through pipeline 19 has improved characteristics compared to that obtained by the processes of regeneration of waste oils according to the prior art.
  • this bitumen - also thanks to its carbon black content - in addition to the common uses of bituminous fractions, such as the preparation of roads and the like, is also suitable for more refined uses.
  • this bitumen is mixed with polyethylene (for example, low-density polyethylene) or polypropylene, for example by making 10% bitumen and 90% polymer mixtures, it can be used for the creation of master batches. For example, it is possible to easily obtain a film thickness of about 60 microns.
  • bitumen may be used for the production of inks, such as, for example, heatset or coldset inks.
  • the process and the plant according to the present invention allow to obtain a higher lubricant base yield (as seen, it changes from 60% by weight to about 67-70% by weight), increasing the enhancement of the initial waste and reducing process waste. Such enhancement is further increased by the fact that, as seen, even the least valuable product - bitumen - is enhanced.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Claims (4)

  1. Verfahren für die Aufbereitung von Altölen, umfassend einen Schritt einer Flash-Destillation des aufzubereitenden Öls, einen Schritt eines Dekantierens der schweren Fraktion, einen Schritt einer Destillation in einer gepackten Destillationssäule, erlaubend eine Herstellung einer Ölfraktion, die zu einer Hydroraffination gesendet werden kann, und einer Bitumenfraktion, dadurch gekennzeichnet, dass die Bitumenfraktion gemahlen wird, die nach dem Mahlen erhaltene flüssige Fraktion getrennt und als Bitumen gesammelt wird und die verbleibende Feststofffraktion getrennt und rezirkuliert wird zu dem Schritt eines Dekantierens der schweren Fraktion.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass dem Mahlschritt der Bitumenfraktion ein Mischungsschritt vorangestellt wird.
  3. Verfahren nach Anspruch 1 und 2, dadurch gekennzeichnet, dass es einen Mikrofiltrationsschritt des aus der gepackten Säulendestillation resultierenden Produkts bereitstellt, dessen Sediment zu dem Mahlschritt gesendet wird.
  4. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass, vor dem gepackten Säulendestillationsschritt, ein Zentrifugalseparationsschritt bereitgestellt wird, und dass der Druck innerhalb der gepackten Destillationssäule durch eine Flüssig-Ringpumpe eingestellt wird.
EP16164521.3A 2015-05-28 2016-04-08 Verfahren zur aufbereitung von altöl Active EP3098291B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL16164521T PL3098291T3 (pl) 2015-05-28 2016-04-08 Proces regeneracji olejów odpadowych

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
ITUB2015A001298A ITUB20151298A1 (it) 2015-05-28 2015-05-28 Procedimento di rigenerazione di olii usati

Publications (2)

Publication Number Publication Date
EP3098291A1 EP3098291A1 (de) 2016-11-30
EP3098291B1 true EP3098291B1 (de) 2018-10-17

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EP16164521.3A Active EP3098291B1 (de) 2015-05-28 2016-04-08 Verfahren zur aufbereitung von altöl

Country Status (7)

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EP (1) EP3098291B1 (de)
DK (1) DK3098291T3 (de)
ES (1) ES2706480T3 (de)
IT (1) ITUB20151298A1 (de)
LT (1) LT3098291T (de)
PL (1) PL3098291T3 (de)
PT (1) PT3098291T (de)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT201700042853A1 (it) * 2017-04-19 2018-10-19 Viscolube S R L Processo per la rigenerazione di olii usati
IT201900000613A1 (it) * 2019-01-15 2020-07-15 Itelyum Regeneration S R L Processo di valorizzazione di scarti della rigenerazione di olii usati
IT202000001357A1 (it) * 2020-01-24 2021-07-24 Itelyum Regeneration S P A Valorizzazione dei sottoprodotti di un processo di rigenerazione di olii usati
IT202100031700A1 (it) * 2021-12-17 2023-06-17 Itelyum Regeneration S P A Processo di recupero di un complesso di rifiuti

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IT1255534B (it) 1992-09-30 1995-11-09 Processo di riraffinazione di oli usati
IL110104A (en) 1994-06-23 1999-07-14 Corex Technologies 1993 Ltd Process for the reclamation of used lubricating oils
US6319394B2 (en) 1999-02-16 2001-11-20 Miami University Method of removing contaminants from petroleum distillates
CA2396206A1 (en) 2002-07-30 2004-01-30 Nouredine Fakhri Process for the treatment of waste oils
FR2845689B1 (fr) 2002-10-10 2005-01-28 Totalfinaelf France Procede et dispositif pour le traitement d'huiles lubrifiantes usagees

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Also Published As

Publication number Publication date
PT3098291T (pt) 2019-01-24
DK3098291T3 (en) 2019-02-04
EP3098291A1 (de) 2016-11-30
ITUB20151298A1 (it) 2016-11-28
ES2706480T3 (es) 2019-03-29
LT3098291T (lt) 2019-02-11
PL3098291T3 (pl) 2019-05-31

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