EP0452409A1 - Process for reprocessing waste oil - Google Patents

Process for reprocessing waste oil

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Publication number
EP0452409A1
EP0452409A1 EP19900902193 EP90902193A EP0452409A1 EP 0452409 A1 EP0452409 A1 EP 0452409A1 EP 19900902193 EP19900902193 EP 19900902193 EP 90902193 A EP90902193 A EP 90902193A EP 0452409 A1 EP0452409 A1 EP 0452409A1
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EP
Grant status
Application
Patent type
Prior art keywords
oil
step
acid
ammonium
method
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.)
Ceased
Application number
EP19900902193
Other languages
German (de)
French (fr)
Inventor
Fritz Basler
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.)
GEUT AG GESELLSCHAFT FUER ENERGIE UND UMWELTTECHNI
Original Assignee
GEUT AG GESELLSCHAFT FUER ENERGIE UND UMWELTTECHNIK
GEUT ENERGIE- UND UMWELTTECHNIK AKTIENGESELLSCHAFT
GEUT GES ENERGIE UMWELTTECH
GEUT EN UND UMWELTTECHNIK AKTI
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

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Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10MLUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0016Working-up used lubricants to recover useful products ; Cleaning with the use of chemical agents
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10MLUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025Working-up used lubricants to recover useful products ; Cleaning by thermal processes

Abstract

Selon un procédé de traitement, notamment de déshalogénation d'huiles usées, (a) on traite les huiles usées à des températures allant jusqu'à 150°C avec une quantité efficace d'une solution aqueuse d'au moins un acide fort et/ou d'au moins un sel, une base faible et un acide fort ou un précurseur de celui-ci; According to a method of treatment, in particular of waste oils dehalogenation (a) treating the used oil to temperatures up to 150 ° C with an effective amount of an aqueous solution of at least one strong acid and / or at least one salt, a weak base and a strong acid or a precursor thereof; b) on traite le produit ainsi obtenu à des températures élevées avec au moins un liant halogène et c) on sépare l'huile de l'eau et/ou des matières solides contenues dans le produit ainsi obtenu. b) treating the product thus obtained at elevated temperatures with at least one halogen binder and c) separating the water from the oil and / or solids contained in the product thus obtained.

Description

A method for processing of waste oils

The present invention relates to a method for processing, in particular for dehalogenation of waste oils.

The regeneration of waste oils for recovery, the so-called recycling, is both economically and ecologically necessary. It is the use

processed oils (Regeneratöle) as fuel and

Propellants to statutory provisions bound with respect to its content of foreign matter, because the latter are released during combustion in unmodified or modified form, and thereby may be burdened with the air pollutants in an unacceptable manner. Similar

Demands are placed on Regeneratöle, when they are used as base oils for the renewed preparation of lubricating oils.

The foreign substances whose concentration in the

recycled waste oils legal restrictions

subject and must be limited as base oils for technical reasons, when using the Regeneratöle, there are, inter alia, inorganic and organic compounds of metals, sulfur, phosphorus and the halogens, especially chlorine.

The halogen compounds, in particular the

Chlorine compounds, thereby occupy a special position because

1. occurring in the waste oils halogen compounds or their combustion products for humans and the environment are harmful,

2. the legal limits for the chlorine content of fuel oils are very low, and 3. the removal of the high boiling organic

Halogen compounds from waste oils down to residual contents of less than 100 mg of chlorine / kg of oil at a reasonable cost was previously technically almost impossible.

The conventional method for treating waste oil comprising an acid treatment, followed by a

Separation of the acid and a neutralization, and a thermal treatment are expelled by distillation in the volatiles. In certain cases, the oils are distilled himself afterwards. The oils, which are obtained with an average of about 1000 to 10000 mg and more halogen per kg, are freed in such processes only insufficiently from the halogens, if they are not subjected to a final phase to further treatment.

To further removal from the residual halogen

up in the concentration range of 100 mg / kg (expressed as chlorine) waste oils, various methods are known. They consist, for example, in a post-treatment with chlorine binding additives such as alkali or

Alkaline earth metals, alkali or alkaline earth metal hydroxides such as sodium or potassium hydroxide solution or calcium and

Magnesium hydroxide, with alkali metal hydroxides in further

Combination with solubilizers, as well as in a

Hydrogenation.

These methods have the following disadvantages: they are insufficient (as expressed chloride) to reduce residual halogen content of less than 100 mg / kg. They require very high temperatures, are already on

takes place significant thermal decomposition of the oils. The halogen and the other reaction products can be deposited in a hard form such. B. as difficult to filter or zentrifugierbarer mud incurred. You can create residues which additional

create disposal problems. The added

Halogen binders may also increase the ash content of the recycled oil too strong. Finally, they require special safety equipment and

Precautions due to the chemicals used. The above methods are therefore not suitable to reduce the halogen content of the waste oil in a technically and economically justifiable manner.

The US-PS 39 30 988 discloses a process for

Reduction of the ash content in used lubricating oils, wherein the lubricating oil with an aqueous solution of

Ammonium sulfate and / or ammonium bisulfate is brought into contact for reaction with the metal-containing components of the oil and the formation of metal-containing solids, the reaction mass in an oil phase and an aqueous

Phase containing the solids, is separated and the oil phase is recovered as a product oil with a low ash content. The US-PS 38 79 282 discloses a process for

Reduction of the ash content in used engine oil, wherein the engine oil with an aqueous solution of

Ammonium phosphate is brought into contact for reaction with the oil contained in metal salts of

resulting precipitate is allowed to settle and the oil is separated from water and the precipitate.

The US-PS 41 51 072 discloses a process for obtaining pure lubricating oil from used lubricating oil, wherein said oil with an aqueous solution of an ammonium salt selected from ammonium sulfate, ammonium bisulfate,

Ammonium phosphate, diammonium hydrogen phosphate,

Ammonium dihydrogen phosphate and mixtures is brought thereof in a sufficient amount at a temperature of 60 to 120 ° C in contact with the main portion of the water and the light hydrocarbons is removed from the resulting mixture at a temperature of 110 to 140 ° C, which is the oil phase was separated by filtration , the filtered oil is heated to a temperature of 200-480 ° C and in contact with an adsorbent

The resulting oil with hydrogen and a catalyst is treated, is stripped, the oil thus obtained at a temperature of 280-395 ° C, and thereafter recovered is brought.

DE-AS 25 08 713 discloses a process for

Work-up of used mineral oil by means of pre-coagulation, adsorption, filtration, distillation and post-treatment by hydrogenation, in which the oil dehalogenated according to the pre-cleaning, fractional distillation and hydrogenated. The dehalogenation is carried out by treating the oil with an alkali metal, especially Na or K, an alkaline earth metal,

in particular Mg or Ca, an alkali, alkaline earth or aluminum alkoxide, an alkali metal hydride, or

amide, an organic base, in particular pyridine or piperidine, or with metallic aluminum or

anhydrous aluminum chloride in the absence of air and moisture, at a reaction temperature of 15 to 300 ° C. The DE-OS 36 37 255 discloses a method for

Work-up of used oil wherein the used oil at a pressure of 50 to 250 bar with hydrogen-rich gas

is set to a temperature of 350 to

500 ° C is heated, are separated in a separation zone and solids removed as a sludge, a

vaporized oil-rich phase from the separation zone

the hydrogenated product is mixed with ammonia and degassed, and is separated from the degassed product has a chloride-containing aqueous phase is withdrawn and catalytically hydrogenated at temperatures of 300 to 400 ° C.

The DE-OS 36 21 175 discloses a process for

Dehalogenation of hydrocarbon oils wherein the hydrocarbon oils treated in a homogeneous phase with alkali metal or alkaline earth metal alkylates, whose alkyl groups have 6 to 25 carbon atoms, at 120 to 400 ° C and the

Alkali or alkaline earth metal halides formed are separated after the reaction.

The DE-PS 36 00 024. discloses a method for obtaining high-quality lubricants from waste oils by catalytic hydrotreatment of solids, other dissolved and / or emulsified additives and water liberated and optionally chemically and / or

physically pretreated waste oils containing

Mixtures with hydrogen and / or hydrogen

containing gases and / or hydrogen transferring solvents, in which the hydrogenating treatment in the presence of a commercially available hydrocracking catalyst at temperatures of 350-480 ° C and pressures of 20 to 400 bar is carried out.

Finally, GB-PS 85 67 64 discloses a method of reducing the acidity of used lubricating oil, wherein the oil is treated with ammonia.

The above processes are either too expensive or do not result in sufficient

Processing of these oils. Object of the present invention is to provide a process for working, especially for the dehalogenation of waste oil disposal, in which the foreign substances contained in waste oil, particularly halogens can be easily removed technical and economical manner. This object is achieved by a method of the type mentioned, which is characterized in that a) the used oil at temperatures up to 150 ° C with an effective amount of an aqueous solution of at least one strong acid and / or at least one salt of a weak base and a strong acid or a precursor thereof treated, b) treating the product obtained at elevated temperatures at least one halogen binder, and c) in the thus obtained product separates the oil from the water and / or solids.

It has surprisingly been found that the

Method of the invention allows treatment of waste oil by using small amounts of non-toxic and non-hazardous chemicals without applying pressure at relatively low temperatures. In addition to the

Dehalogenation also held a strong reduction of phosphorus and metal content of the waste oil.

Furthermore, only small quantities of waste occur in the inventive process and produces a low amount of oil loss. A refurbished by the novel process oil is suitable as a precursor for rerefining.

The method of the invention is illustrated.

Step a) of the process according to the invention is preferably carried out in a stripper. Here are generally temperatures of up to 150 ° C, especially from 20 to 150 ° C, particularly preferably from 80 to 120 ° C. The treatment time is preferably 1 to 2 hours. In this step a) the used oil is treated with an effective amount of an aqueous solution of at least one strong acid and / or at least one salt of a weak base and a strong acid or a precursor thereof. The amounts of solution depend on each in used oil

existing foreign substances, and are not generally fen above the equivalent amount of Fremdstof, particularly the halogen compounds. Out

for economic reasons it is preferred to solution a small amount as possible. Thus, in general, amounts below 5 wt .-% aqueous solution, based on the oil, sufficiently. Quantities are more preferably below 0.2 wt .-% is used. There can be used all strong acids for the treatment of the waste oil in step a). Preferably, an aqueous solution of sulfuric acid, sulfurous acid, sulfamic acid, sulfonic acid, phosphoric acid,

phosphorous acid, hypophosphorous acid,

Phosphonic acid, hydrochloric acid, hydrofluoric acid or mixtures thereof. Particularly preferred are sulfuric acid, phosphoric acid, phosphorous acid and

Phosphorous acid. As phosphoric acid, ortho-, meta- and polyphosphoric acid may be used.

The salt of a weak base and a strong acid is preferably an ammonium salt of a strong acid. As ammonium salt are especially ammonium sulfate,

Ammonium bisulfate, ammonium sulfite, ammonium disulfite,

Ammoniumamidosulfat, ammonium thiosulfate,

Ammonium sulfonate, ammonium phosphate,

Diammonium hydrogen phosphate, ammonium dihydrogen phosphate, Ammσniumamidophosphat, ammonium phosphite,

Ammoniumphosphonsäure, ammonium chloride, or mixtures of suitable Ammoniumfluoriü thereof. Particularly preferred are ammonium sulfate, ammonium bisulfate, ammonium sulfite,

Diammonium hydrogen phosphate, ammonium dihydrogen phosphate, ammonium phosphite and Ammoniumphosphonsäure. As

Ammonium phosphite can be used mono-, di- and Triammoniumphosphit.

Further, in step a) a salt of guanidine, an amide such as carbamide or hydrazine, or an alkyl or aryl compound of the above acids such as

be dimethyl phosphite, diethyl or triethyl used.

The step b) of the process according to the invention

preferably a coagulation step. Here, the dissolved and undissolved organic decomposition

Halogen compounds to hydrogen halides which are immediately neutralized by the added halogen binders. The coagulation temperature is preferably 250 to 300 ° C and the treatment time is 0.5 to 24

Hours, more preferably 3 to 24 hours. As

Halogen binder is preferably used ammonia and / or an organic base. Suitable organic bases are urea, guanidine, hydrazine, hydrazine hydrate, a

Carbazide, a semicarbazide, piperazine, phenylenediamine, morpholine, diethanolamine, triethanolamine or a salt of these compounds particularly preferred.

The coagulation can be performed such that the oil is heated in three stages via special

Heat exchanger by largely remains in the respective circuit and is routed through scrubbers. In this stage by the addition of ammonia and / or an organic base, the halogens

(Mainly chloride) blown away than corresponding ammonium compounds and, together with a little water and oil to be found in the condensate of

Disposal is fed, or they fall as

inert / oil-insoluble halogen salts on. Simultaneously, a part of the metal compounds is precipitated, and

various organic acids to carbon reduced.

In the subsequent step c) of the inventive method, the product obtained from the water and / or solids is separated. As it is easy

is sedimented, for example, may be decanted, wherein about 95% of the water and / or the

Solids are separated. Then the oil can be reheated somewhat, depending on the viscosity, for example to a temperature of 60 to 150 ° C, and then filtered, pressed for example by a filter press. The remaining solids are removed.

Optionally, the obtained in step a) mixture may be cured prior to coagulation. This can

for example, by addition of an additive to improve the separation of oil in the stuf ec), preferably at a temperature of 140 to 200 ° C and about 1 to 2 hours, take place. As additives are preferably

Sodium, potassium or calcium hydroxide, sodium, potassium or Calciumalkoholat, a sodium, potassium or

Calcium salt with an organic acid such as

Sodium ethoxide or sodium stearate, urea, hydrazine, guanidine, a carbazide, or a salt of this compound. If such a courier step is carried out, may in the subsequent coagulation the

Treatment times are reduced.

After the coagulation step a may optionally

Post-treatment of the resulting product before its

Separation take place. In this case, the product of step b) with an effective amount of the aqueous solution a) used in the step, preferably at a temperature of. less than 100 ° C, treated. This post-treatment can be carried out over 1 to 24 hours. Such post-treatment is particularly suitable when

possible small amount of the aqueous solution in step a) is used, such as less than 0.2 wt .-% of the aqueous solution, based on the used oil.

Prior to the treatment of waste oil by the inventive process, any conventional pre-treatment can be carried out. Thus, in a proportion of more than 5% of impurities, for example, a pre-dewatering, as carried out by centrifugation, decantation or distillation.

The water treated by the inventive process oil is particularly suitable for use as a fuel oil or as the base oil for the renewed preparation of lubricating oils.

The following examples illustrate the invention.

example 1

250 g of a Altolgemisches containing 22% water, 15,000 ppm total chlorine and 1.70% ash has been deposited with

offset room temperature with 2.5 wt .-% sulfuric acid (40%) and heated with stirring to 80 ° C, admixed with 1,000 ppm of demulsifier and allowed to stand for 8 hours at this temperature. The supernatant oil was then slowly heated to 150 ° C, were obtained wherein:

4% condensate having a chlorine content of 80,000 ppm and 96% residual oil having a chlorine content of 9350 ppm. The latter was slowly heated to 280 ° C and then bubbled passed a total of 1.5 g of ammonia gas. After 12 hours at this temperature and

Ammonia action, the oil was cooled to 150 ° C and filtered with suction. The filtrate as golden brown clear oil still contained 240 ppm of chlorine, and an ash content of 0.01%. The distillate (2.7%) containing 12400 ppm of chlorine

example 2

300 g of a Altolgemisches used primarily from engine and hydraulic oils having a water content of 3.5%, 3600 ppm total chlorine, 850 ppm phosphorus and 0.88% ash was aqueous sodium at 80 ° C with 2.5 wt .-% of a 40% solution of equal parts Diammoniumsulfit and Ammoniumsulfamid added under stirring and slowly heated without stirring to 150 ° C, or 1 hour at 80 to 120 ° C and 1 hour at 120 to 150 ° C. The residual oil (Organochlorgehalt 2200 ppm) was added rapidly to 280 ° C is further heated, and at 200 ° C dropwise a hot 90 ° C, 75% aqueous solution of equal parts of

Carbamide and diethanolamine (total of 4.0 g) was added. After 4 hours and was cooled at 150 ° C above the suction filtered clear with 1% silicic acid. The filtrate still contained 140 ppm of chlorine, 8 ppm phosphorus and had an ash content of 0.01%.

example 3

1 kg of a Altolgemisches of mainly

Machine oils, containing 1.0% water, 13,700 ppm

Total chlorine, of which 12 mg were PCB (polychlorinated biphenyls), was at 90 ° C with 20 ml of a 10% solution of equal parts of ammonium monohydrogen phosphate,

Ammonium and Diammoniumphosphit

offset, and within 1 hour with stirring to

150 ° C heated. The residual oil containing 13500 ppm of chlorine, was carefully treated with 25 g of a 90 ° C

hot aqueous 75% strength mixture of guanidine, carbamide and diethanolamine and make up to 250 ° C within half an hour

further heated and then a total of 1.2 g of ammonia gas

bubbled up to 330 ° C and a total of 6 hours. The cooled oil was at 100 ° C with 15 ml of the same

treated 10% solution initially used and after 5 minutes mixed with 1000 ppm of a demulsifier, 12

allowed to stand for hours at 90 ° C and decanted the supernatant oil and a. Suction filtered. The clear oil still contained 60 ppm chlorine, of which 10 mg were PCB.

Example 4 In this Example, the same starting oil unfiltered waste oil was investigated with a chlorine content of 1,840 mg / kg and an ash content of 0.37% respectively. The procedure was varied in the added agent, while the other conditions, namely temperature and treatment time) were kept constant in the process steps a) and b.

The step a) has been carried out by treatment of the waste oil at 70 ° C before stripping to 140 ° C. Step b) was over five hours at 280 ° C.

In Table 1, the added in steps a) and b) compounds as well as the particular after performing these steps in the filtered oil chlorine content and ash content as well as the filterability of the oil after coagulation for five hours at 280 ° C are given.

From the results of the table can be the following

Draw conclusions:

If the waste oil in any of the steps a) and b) an inventively used agent added (test 1), a certain dehalogenation of waste oil takes place, but the ash content remains high. A treatment of the waste oil according to step b) of the process according to the invention, but without the addition of an aqueous solution of a strong acid and / or a salt of a weak base and a strong acid in step a), (experiment 2), leads to the same result as in The first attempt

Chlorine content of the waste oil is reduced to some extent, while the ash content is not reduced. This

Experiment shows that the sole carrying out step b) of the process according to the invention does not lead to the desired dehalogenation of waste oils. Rather, a destabilization of the organochlorine compounds, which are then almost completely removed in step b) takes place already in step a) (Experiment 4). In Experiment 3, the used oil was treated according to step a) of the inventive method, while in step b) no halogen binder was added. In this case, although a sufficient reduction of the ash content is achieved; the chlorine content is, however, only minimally reduced.

In summary it can be said that a

satisfactory dehalogenation and ash removal and demetallization of waste oil both steps a) and b according to the invention are necessary), with both levels influence each other and lead to a uniform technical success. The chemical treatment in step a) is used both for demetallization and the destabilization of the chlorine compounds. The demetallization is still ongoing after step a), but it requires the heat treatment in step b) to achieve complete de-metallization and to obtain a filterability of the used oil. Furthermore, the dehalogenation is accomplished after stage a) only to the extent as in the used oil

precipitated existing chlorides and low boiling halogenated solvents are distilled off via the vapor phase. thereafter, the residual halogen content in the oil comes only from organic and dissolved compounds which remain stable without the treatment in step a), typically up to cracking temperatures of above 350 ° C. The treatment in step a) at temperatures below 150 ° C causes a

Destabilization of these halogen compounds, so that it at temperatures of about

250 ° C split off hydrogen halide. Remains of this hydrogen halide in the oil mixture, the reaction is partially reversible, and the dehalogenation is low.

Tabel le 1 Ausgangsol: unfiltered waste oil

Chlorine content (mg / kg): 1870 Ash content (%): 0, 37

Chlorine content (mg / kg) Ash content (%) Filtrier¬

Test step a) step b) after after after after bility

Step a) step b) step a) step b)

1 2% H 2 O 540 345 0.36 0.38 good

2 2% H 2 O NH 3 gas 540 290 0.36 0.39 good bubbled

2% H 2 O

0.1% H 2 SO 4

3 0.25% H 3 PO 3480300 0.14 <0.01 good

0.25% Guanidintbluol- sulfonic acid

2% H 2 O

0.1% H 2 SO 4 NH 3 gas 480 40 0, 14 <good 4 0.01 0.25 6 H bubbled 3 PO 3

0.25% Guanidintoluol- sulfonic acid

Claims

claims
1. A method for processing, in particular for
Dehalogenation of waste oil, characterized in that a) the used oil at temperatures up to 150 ° C with an effective amount of an aqueous solution of at least one strong acid and / or at least one salt of a weak base and a strong acid or a precursor thereof treated, b) treating the product obtained at elevated temperatures at least one halogen binder, and c) in the thus obtained product separates the oil from the water and / or solids.
2. The method according to claim 1, characterized in that step a) is carried out in a stripper.
3. The method according to claim 1 or 2, characterized
in that the step a) is carried out at a temperature of 20 to 150 ° C.
4. The method according to any one of claims I to 3, characterized in that step a) is carried out over 1 to 2 hours.
5. The method according to any one of claims 1 to 4, characterized in that step a) with an amount of up to 5 wt .-% of the aqueous solution, based on the oil, is carried out.
6. The method according to any one of claims 1 to 5, characterized in that step a) with an aqueous solution of sulfuric acid, sulfurous acid,
Sulfamic acid, sulfonic acid, phosphoric acid,
phosphorous acid, hypophosphorous acid,
Phosphonic acid, hydrochloric acid, hydrofluoric acid or mixtures thereof is carried out.
7. The method according to any one of claims 1 to 5, characterized in that step a) with an aqueous
Solution of an ammonium salt of a strong acid or a precursor thereof is performed.
8. The method according to claim 7, characterized in that, as ammonium salt ammonium sulfate, ammonium bisulfate, ammonium sulfite, ammonium disulfite, Ammoniumamidosulfat, ammonium thiosulfate, ammonium sulfonate, ammonium phosphate, diammonium hydrogen phosphate, ammonium dihydrogen phosphate, Ammoniumamidophosphat, ammonium phosphite
Ammoniumphosphonsäure, ammonium chloride or
Ammonium fluoride is used.
9. The method according to any one of claims 1 to 5, characterized in that step a) with an aqueous
Solution from a guanidinium salt, an amide, a
Alkyl or aryl compound of a strong acid or a precursor thereof is performed.
10. The method according to any one of claims 1 to 9, characterized in that step b) is carried out at a temperature of 200 to 350 ° C.
11. The method according to any one of claims 1 to 10, characterized in that step b) is carried out for 0.5 to 24 hours.
12. The method according to any one of claims 1 to 10, characterized in that the stage b) is carried out for 3 to 24 hours.
13. The method according to any one of claims 1 to 12,
characterized in that) ammonia and / or an organic base is used as the halogen binding agent in step b.
14. The method according to claim 13, characterized in that, as organic base, urea, guanidine, hydrazine, hydrazine hydrate, a carbazide, a semicarbazide
Piperazine, phenylenediamine, morpholine, diethanolamine,
Triethanolamine or a salt of these compounds
is used.
15. The method according to any one of claims 1 to 14, characterized in that the step c) by
Sedimentation and / or filtration is carried out.
16. The method according to any one of claims 1 to 15, characterized in that the step c) at a
Temperature is carried out from 60 to 150 ° C.
17. The method according to any one of claims 1 to 16, characterized in that a conventional pre-purification of the waste oil is performed prior to step a).
18. The method according to claim 17, characterized in that the preliminary cleaning is carried out by draining.
19. A method according to any one of claims 1 to 18, characterized in that a curing is carried out between step a) and b).
20. The method according to claim 19, characterized in that the curing is carried out by contacting the product of step a) with at least one additive for improving the releasability of the oil in step c) is treated.
21. The method according to claim 19 or 20, characterized
in that the curing is carried out at a temperature of 140 to 200 ° C.
22. The method according to any one of claims 19 to 21, characterized in that, the curing is carried out over 1 to 2 hours.
23. The method according to any one of claims 19 to 22, characterized in that as an additive sodium, potassium or calcium hydroxide, sodium, potassium or
Calciumalkoholat, sodium, potassium or Calciurnsalze with organic acids, urea, hydrazine, guanidine, a carbazide, or a salt of these compounds is used.
24. The method according to any one of claims 1 to 23, characterized in that) and c an after-treatment is carried out between the step b).
25. The method according to claim 24, characterized in that the after-treatment is carried out by the
Product of step b) is treated with an effective amount of the aqueous solution used in step a).
26. The method according to claim 24 or 25, characterized
in that the after-treatment at a
Temperature is performed below 100 ° C.
27. The method according to any one of claims 24 to 26, characterized in that the aftertreatment is carried out over 1 to 24 hours.
EP19900902193 1989-01-04 1990-01-03 Process for reprocessing waste oil Ceased EP0452409A1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
DE19893900159 DE3900159A1 (en) 1989-01-04 1989-01-04 A method for processing of waste oils
DE3900159 1989-01-04

Publications (1)

Publication Number Publication Date
EP0452409A1 true true EP0452409A1 (en) 1991-10-23

Family

ID=6371593

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Country Status (7)

Country Link
US (1) US5057207A (en)
EP (1) EP0452409A1 (en)
JP (1) JPH04504432A (en)
CN (1) CN1043954A (en)
CA (1) CA2007062A1 (en)
DE (1) DE3900159A1 (en)
WO (1) WO1990007566A1 (en)

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WO1990007566A1 (en) 1990-07-12 application
CA2007062A1 (en) 1990-07-04 application
DE3900159A1 (en) 1990-07-05 application
JPH04504432A (en) 1992-08-06 application
CN1043954A (en) 1990-07-18 application
US5057207A (en) 1991-10-15 grant

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