Classifications

• • 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

Definitions

• High viscosity index lubricants as employed for automobile lubrication, present a tremendous problem to the environment.
• Such lubricants commonly contain relatively large amounts of various detergents and extreme pressure additives in the form of polyvalent metal soaps as well as lead compounds, oxidized carbonaceous materials, water, etc. Due to their relatively high content of various additives, used lubricating oils cannot be burned simply without seriously polluting the air. Thus, literally millions of gallonsof used lubricants are discarded annually because there is no economical way to recycle them.
• the quantity of lubricating oil which can be recovered economically by reclaiming procedures has decreased.
• the yield of lubricating oil which can be obtained by reclaiming is in the order of 50 percent or less of the recoverable organic material. Due to the severity of treatment, a substantial quantity of the recoverable organic material in the oil is lost. This makes the reclaiming procedure, less economical and also results in the production of an increased quantity of sludge and byproducts whose disposal causes contamination of the environment.
• the used lubricating oil is first treated with caustic at an elevated temperature such as 400 to 600F. to drive off water and to break soaps in the oil as well as to neutralize the oil. Also, in the course of heating, the light ends are flashed off. and are generally burned. After the heating procedure, the oil is then cooled to about 100F. or less and a small quantity of concentrated sulfuric acid is added. After settling, the bottoms are drawn off which contain an acid sludge comprising sulfuric acid and dissolved sulfonates and oxygenated hydrocarbons. The sludge, which may constitute about 5 to 20 percent by weight of the used oil being treated,
• the top oil is then generally heated and finely divided clay is added at a temperature of about 350F.
• the mixture of clay and top oil is then taken to a temperature of about 600F. in a heater and after being held at this temperature for sufficient time is cooled to about 350F. or less and passed through a filter press.
• Another procedure which has been used for treatment of used lubricating oils involves treatment of the oil'with lime and finely divided clay.
• a still further procedure involves treatment of the oil with a mixture of caustic and sodium silicate. All of the above noted procedures give a yield of purified oil of 50 percent or less based on the weight of the used oil being treated together with the production of 5 to 20'percent of light ends or tops which are burned. Additionally, all of the above procedures produce substantial quantities of sludge which cannot be recycled and must be dumped.
• the present process for the purification of used lubricating oils is economical providing a yield of about percent to about percent or more of the recoverable organic material in the used oil and also produces a very small amount of residue composed of polyvalent metal compounds inadmixture with oxidized hydrocarbons and all of the myriad materials which are found in the sludge from used lubricating oils.
• the process provides a means for substantially reducing environmental pollution resulting from the dumping of waste oil.
• the process provides a new source of high viscosity index oils which are presently in short supply and are urgently needed in industrialized countries for automotive lubrication.
• used lubricating oils which-may be collected from various sources, such as independent service stations throughout a large area, are first admixed with a predominantly hydrocarbon liquid diluent which preferably has a boiling range within the temperature region of about F. to about 550F.
• the liquid diluent may be either aromatic or aliphatic and is mutually soluble with the used hydrocar-- bon lubricating oil undergoing treatment.
• the function of the liquid .diluent in the process is to lower the viscosity of the used lubricating oil and to change the characteristics of the used lubricating oil dispersion to thereby facilitate the contact, with the used lubricating oil in the subsequent steps of the process, of a water miscible alcohol-water mixture.
• Impurities which may be present in the liquid diluent, which may be recycled light ends from the purified lubricating oil, may include, for ex-' boiling hydrocarbon liquids, such asliquid propane, I
• the light or naphtha ends may be recycled to the process to serve as the predominantly hydrocarbon liquid diluent for the used lubricating oils being treated.
• the process will be self-sustaining with sufficient naphtha light ends being supplied through distillation of the purified oil or organic phase to satisfy the need for liquid diluent in diluting the as received used lubricating oil.
• the quantity of the liquid diluent which is employed in diluting the as received used lubricating'oil may be varied in accord with the process.
• a particularly practical range of liquid diluent with respect to used oil ranges from about 1:1 to about 1:2 by volume, although other dilutions may be used, if desired, such as. 2:1 or even 4:1depending, for'example, on the solids content and viscosity of the used drain oil undergoing treatment and the efficacy of the diluent liquid in furthering contact by the extraction solvent.
• the size ofthe separation equipment such as distillation columns, etc., must also be proportionately increased which causes an increase in the cost of the processing equipment.
• the diluted lubricating oil is then contacted with a mixture of water, a water miscible alcohol, and a small'quantity of an ammonium or alkali metal base.
• the ammonium or alkali metal base which includes ionizable salts that form the basein situ, functions to displace polyvalent metal ions from the various metallic soaps which are present in the diluted lubricating oil undergoing treatment. As the polyvalent metal ions are displaced from the soaps by the monovalent ammonium or alkali metal cations, the molecular weight of the soaps is decreased.
• the water miscible alcohols which maybe used in this step of the process are methanol, ethanol, isopropyl alcohol, n-propyl alcohol, sec-butyl alcohol, and tert.-butyl alcohol.
• the higher alcohols such as amyl alcohol and also alcohols having a lower water solubility such as n-butyl alcohol, have such a low solubility in water that they are generally ineffective in the present process.
• the water miscible alcohols which are suitable in the process including polyhydric alcohols, generally have a solubility of about percent or more by volume in water.
• percent to about 60 percent by volume of alcohol were generally more effective than mixtures containing either more or less alcohol in relation to the amount of water in the alcohol-water mixture.
• the material undergoing treatment i.e., used lubricating oil
• the specific operating conditions employed may be varied to suit the particular batch of lubricating oil which is being treated. For example, if the batch of lubricating oil undergoing treatment has a relatively high water content, this factor may be taken into consideration in determining the ratio of alcohol to water in treating the lubricating oil after it has been diluted with a predominantly hydrocarbon liquid diluent as described.
• the lubricating oils may, for example, be collected in a relatively large holding tank. When the holding tank is full, representative samples may then be taken and analyzed with a ent process to determine the conditions which provide the greatestreduction in the ash content of the oil being treated and thegreatest yield of purified oil.
• a particularly suitable quantity of the water miscible alcohol-water mixture is about one volume of the mixture for each volume of the dilutedused lubricating oil forone-stage extraction of the diluted lubricating oil.
• the diluted lubricating oil- may be subjected to multiple-stage extraction with a water miscible alcoholwater mixture, as described, and also the quantity of the alcohol-water mixture may be varied, for example, from about one-half volume of alcohol-water mixture to two volumes of the diluted lubricating oil to higher volume ratios in excess of 1:1.
• the volume of the water miscible alcohol-water mixture is kept as low as possible since this simplifies the subsequent processing steps in terms of equipment size, cost, etc.
• ammonium carbonate, sodium carbonate, potassium carbonate, lithium carbonate, and sodium hydroxide have all been employed and found suitable.
• sodium carbonate and sodium phosphate are preferred.
• the carbonate and phosphate anions are particularly effective in reducing the solubility of the polyvalent metal cations which are displaced from the metallic soaps in the diluted lubricating oil by the nonvalent ammonium and alkali metal ions, and in reducing the efficacy of the non-ionic dispersants remaining in the oil to maintain the micellular configuration necessary to keep the solids and sludge in dispersed form in the diluted oil.
• closely related anions such as the bicarbonate ion, were found to be less effective in the process than the carbonate ion.
• the quantity of the ammonium or alkali metal base which is used v is sufficient to displace the polyvalent metal ions from the soaps within the oil but that the base not be present in any great excess of that amount.
• a diluted used lubricating oil containing onehalf volume of used lubricating oil admixed with onehalf volume of a liquid predominantly hydrocarbon diluent
• a 50:50 volume ratio water miscible alcohol-water mixture it was found that the use of one gram of an alkali metal base, e.g., sodium carbonate, for each 100 mls. of the alcohol-water mixture gave satisfactory results.
• Agitation is generally employed during the treatment of the diluted lubricating oil with the alcohol-water mixture containing an ammonium or alkali metal base.
• the agitation may be provided by mixing within a large vessel through use of a mixing impeller,
• a continuous, metered in-line mixing device such as a gear pump or homogenizer, or by using any other mixing procedure.
• the agitation of the diluted lubricating oil and alcohol-water mixture is generally carried out until an emulsion forms which indicates that the dilutedoil has been thoroughly contacted with the alcohol-water mixture.
• the emulsion is generally unstable and is broken during the subsequent centrifuging step. If the emulsion is not broken during centrifuging, this is undesirable since the process yield is reduced by trapping of recoverable oil in the emulsion phase. It is preferred that the formation of a stable emulsion which is not broken by centrifuging be kept to a minimum. This may be accomplished by taking representative samples of the used oil being treated and then varying the process parameters on a small scale to determine the optimum yield conditions. By determining the optimum processing conditions for a particular used oil, the formation of a stable emulsion may be minimized to provide the I maximum yield of recoverable organic material in the oil.
• the resulting mixture is then fed to a centrifuge for separation of the sludge from the lubricating oil and also separation of the alcohol-water mixture from the organic mixture of liquid diluent and lubricating oil.
• Industrial centrifuges are well known and any of the various types of centrifuges may be used in the present process.
• the resultant mixture is simply fed into the centrifuge with the sludge depositing out on the walls of the centrifuge while the alcohol-water mixture is taken off through one outlet and the organic mixture of liquid diluent and lubricating oil is removed through another outlet.
• the sludge formed on the interior of the centrifuge may be removed by back-washing or by spraying 'the interior of the centrifuge bowl with a jet of water.
• the alcohol-water stream which is taken from the centrifuge contains ammonium or alkali metal soaps.
• the mixture of water miscible alcohol and water may be recycled directly'to the process for use in treatment of used lubricating oil diluted with a predominantly hydrocarbon liquid, as described.
• the alcohol-water stream may also first be subjected to a clean-up operation before return to the process. Any conventional procedure may be used for cleaning the alcohol-water stream to remove alkali metal soaps such as acidificationand extraction of the organic acids, ion exchange, or distillation of the alcohol followed by addition of fresh make up water to the alcohol, etc.
• nantly hydrocarbon liquid diluent may be used as a low ash fuel or the mixture may be separated through conventional distillation.
• the naphtha fraction from the distillation may, as described previously, be recycled for use in the process in diluting the used lubricating oil.
• the purified lubricating oil fraction from the distillation may be used as the base stock in compounding new lubricating oils.
• a convenient and accurate way of measuring the effectiveness of the present process in terms of the purity of the lubricating oil obtained is to compare the ash content of the as is used lubricating oil with the ash content of the purified lubricating oil product obtained from the process.
• the present process may provide areduction in the ash content of the oil of to percent. For example, an ash content of about 2 percent in the as received used oil was reduced to about 0.2 percent in the purified oil.
• there is a reduction in the additive content of the oil which simplifies further processing of the purified oil using conventional refinery procedures.
• the residue from the process which consists of the various materials that are present in the sludge of a used lubricating oil may constitute about'3 percent by weight of the as received used lubricating oil.
• the residue is only a very small fraction of the weight of the used lubricating oil.
• the residue from the process has a high metallic content, predominantly lead, and, thus, represents a potentially valuable source of metals.
• the process'residue from all the used oil would be quite sizable in terms of total weight of metals, even though the residue represents only a small percentage by weight of the used lubricating oil being treated.
• the residue may be processed, where economically feasible, to recover its metal fractions.
• the method of centrifuging used was a modification of ASTM method Dl796-62. In centrifuging, 100 ml.
• cone shaped tubes (described in the ASTM method) were first filled with the resultant mixture formed from the diluted drain oil and the mixture of alcohol with water. The cone shaped-tubes and their contents were then whirled in a Precision Oil Centrifuge (Catalog No.
• the contents of the tubes had separated into several layers.
• a layer of sludge which had been removed from the drain oil by the process of the invention.
• Above the lower sludge layer was a water miscible alcohol-water layer and above this layer was an organic layer containing a purified organic phase of the predominantly hydrocarbon liquid diluent with the purified drain oil. This upper layer is termed the organic layer.
• an emulsion or dispersion formed which was not completely broken by the centrifuging and which appeared within the organic or the alcohol-water phase or as a layer at the interface between the organic layer and the alcohol-water layer.
• the yield of recoverable organic material in volume percent of the drain oil was determined by measuring the volume of the purified organic layer and subtracting the volume of the hydrocarbon liquid diluent from this volume. The remaining volume, which is the volume of the recovered organic material from the drain oil, was then divided by the original volume of the drain oil to determine the percent yield of recoverable organic material. In some instances, as indicated in the tables, the yield of recoverable organic material from the drain oil was observed to be in excess of 100 percent. In these instances, a dispersion or emulsion was observed and there had obviously been a transfer of material into the organic layer which produced the high reading;
• the sample from the organic phase was then analyzed to determine its solids content and the ash content of the solids.
• the ash content of the purified drain oil was then converted to an ash content based on the weight of the original drain oil by multiplying the ash content of the solids by the percent solids in the original oil. This, then, permitted a direct evaluation of the process in terms of the percentage reductionwhich was obtained in the ash content.
• a 10 gram sample was weighed into a soft, crimped aluminum dish having a diameter of 2% inches, a depth of /8 inches and a finger-grip handle.
• the dish was placed on a Corning Pyroceram 600-watt hotplate with a temperature dial set to produce a surface temperature of approximately 450F. and preheated to the operating temperature. Heating at about 450F. was maintained for 1 hour, after which the dish was removed, cooled to ambient temperature, and reweighed. The precent of solids was then determined by dividing the final weight of thc residue by the weight of the sample and multiplying by 100.
• the ash content of the drain oil or the purified organic layer was determined by ASTM method D482- 63. In determining ash, the analytical problems which of the used drain oil with that of the purified organic liquid. 1
• the method for determining ash consists of weighing a sample of the material to be ashedinto a ml. porcelain crucible. The material in the crucible is then ignited and allowed to burn until only ash and carbon remain. The carbonaceous residue is then reduced to an ash by heating in a muffle furnace at 775C, followed by cooling and weighing.
• the ash content primarily indicates the metals content of the sample expressed in terms of the inorganic salts of the metals which are predominantly phosphates, oxides, silicates, sulfates, etc.
• the solids content and the ash content of the used drain oil were determined as a percentage of the weight of the drain oil sample.
• the ash content of the purified organic layer was also determined as a percentage basedon the solids content of the sample from the purified organic layer.
• the weight of solids of the purified organic layer was determined and these solids were then burned to determine the ash content of the solids.
• the ash content of the purified organic layer expressed as a percent of the solids in the sample, is then converted to weight percent ash based on the used drain oil by multiplying by the percent of solids in the used oil.
• the basis for the'conversion of the ash in the purifiedorganic layer to percent ash based on the used drain oil is based on the fact that the ash is contained in the solids and the total solids content of both the drain oil and the purified organic layer is relatively constant and is only slightly affected by the present process.
• the liquid hydrocarbon diluent in the sample from the purified organic layer is driven off.
• the solids which remain are those obtained from the used drain oil being treated.
• the heating at about 450F. drives off the light fractions as well as any water present in the drain oil.
• the solids which remain are largely hydrocarbons which have a boiling point in excess of 450F., and these solids are almost entirely recovered by the present process.
• the weight of the solids which are removed is very small in comparison to the total weight of solids composed mainly of hydrocarbons whose boiling point is in excess of 450F.
• the assumption that the solids content from the drain oil remains fixed throughout the process is reasonably valid and any errors resulting from this approximation are within an error of about percent of the observed values, i.e., i 0.05
• Examples l3 are each concerned with a drain oil having an ash content of 1.44 percent by weight.
• the ash content was reduced to 0.84 percent, based on theweight of original drain oil, while in Example 2 the ash content was reduced to 0.28'percent.
• the striking effect of adding a base to the alcohol-water mixture is illustrated by the results of Example 2 in which all of the process conditions were otherwise the same as in Example 1.
• Example 3 illustrates the effectof dilution in which 50 mls.
• drain oil were admixed with 50 mls. of naphtha diluent and then centrifuged directly without being contacted by the alcohol-water mixture.
• this reduction in ash was far less than that obtained, for example, in Example 2 where were admixed with 50 mls. of an alcohol-water mixture containing 1 gram of a base and subjected to further centrifugation.
• the second stage of the procedure produced a reduction in the ash content from 0.20 weight percent to 0.16 weight percent based on the weight of the original drain oil.
• Example 5 the hydrocarbon diluent was deleted while increasing the quantity of the alcohol-water mixture and the ash content of the drain oil was reduced to 1.10 percent. Similarly, in Example 6, both the quantity of the drain oil and the hydrocarbon diluent were decreased-while increasing the weight of the alcoholwater mixture and decreasing the quantity of the base.
• Drain oil (mls.) 25 25 25 25 25 25 25 25 25 25 25 25 25 Naphtha diluent (mls.) 25 25 25 25 37 25 25 25 25 25 25 25 25 Vol. percent isopropanol 50 50 50 40 60 50 50 50 50 50 50 in water. 1Sopropanol-water(mls.) 50 50 50 50 50 50 50 50 1.0 gm. NaHCO; Na. .SO (NHJ CO (NHJgCOa (NHJZCOJ Na PO, Na i-IP04 Na CO K CO Li COa NaOH Base (100 m1. ale-water) g 1 Recovery of drain oil-vol. 90 96 90 82 94 90 92 86 -64 percent. Ash of recovered drain oilv 0.81 0.81 0.66 0.93 0.67 0.38 0.47 0.30 0.33 0.89 0.85
• Drain Oil (mls.) 25 50 25 25 50 Hydrocarbon Diluent Kerosene Xylene Xylene Dehydrated Dehydrated Overhead Overhead Diluent (mls.) 25 50 25 25 50 50% (vol.) Isopropyl Alcohol-Water (mls.) 50 50 O .0 Na,co, (gm/100ml Ale-Water) l 0 I l 0 Recovery of Drain Oil-Vol.% 82 96 98 I00 Ash of Recovered Drain Oil- Wt.% 0.24 0.94 0.26 0.26 0.92- Dispersion-Organic Layer None Yes None None None Yes Dispersion-Alcohol Layer None None None Table VIII'illustrates the results obtained from Examples 37-41 in which the hydrocarbon diluent was varied.
• Example 37 mls. of kerosene was utilized as the diluent and the drain oil, after treatment, had an ash content of 0.24 percent by weight based on the used oil.
• Example 38 xylene was employed as a diluent, but the diluted drain oil was not contacted with a water-alcohol mixture as required in the process. As illustrated, xylene, while 'a good diluent, was not effective to produce the desired reduction in the ash content of the oil in theabsence of the contacting step with a water-alcohol mixture.
• Example 39 xylene was used as the diluent and the diluted oil was then treated with an alcohol-water mixture in accord with the process. This provided a reduction in the ash content to 0.26 percent.
• Examples 40 and 41 demonstrate the use of a dehydrated overhead from a drain oil as the hydrocarbon diluent.
• Example 40 with contact of an alcoholwater mixture containing a base, the ash was reduced to 0.26 percent based on the used oil being treated.
• Example 4 the mixture of overhead and drain oil was centrifuged but the diluted oil was not contacted with the alcohol-water mixture.
• Example 41 demonstrates that simple dilution with the hydrocarbon diluent was not effective in reducing the ash content to the desired levels.
• Table IX illustrates the characteristics of the hydrocarbon diluents referred to in the various examples previously described. As indicated by Table IX and the expresent process in reducing the content of these metals, the metals analysis set forth in Table X .was conducted on a drain oil in its as is condition and on the purified drain oil after treatment according to the present process.
• the used drain oil which was employed in a number of the previously described examples, contained 1.73 percent by weight of ash while the purified oil was obtained using the process conditions set forth'in Ex.- ample 33.
• the metals content shown for the purified oil is corrected to the weight of the usedoil in the same manner as described previously.
• a method of purifying a used lubricating oil comprising;
• centrifuging to remove sludge and metal compounds from the oil and to separate the diluted oil phase from the alcohol-water phase.
• water-miscible alcohol is methanol, ethanol, isopropyl alcohol, npropyl alcohol, sec-butyl alcohol or tert-butyl alcohol.
• a method of purifying a used lubricating oil comprising:
• alkali metal base is sodium carbonate, potassium carbonate, or sodium phosphate.
• a method of purifying a used lubricating oil comprising: 1 v

Landscapes

• 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)
• Lubricants (AREA)
• Fats And Perfumes (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Priority Applications (6)

Applications Claiming Priority (1)

Publications (1)

Family

ID=23444260

Family Applications (1)

Country Status (6)

Cited By (24)

Families Citing this family (3)

Citations (3)

• 1973
  • 1973-06-04 US US00366733A patent/US3819508A/en not_active Expired - Lifetime
• 1974
  • 1974-05-29 CA CA201,164A patent/CA1016153A/en not_active Expired
  • 1974-05-31 FR FR7419052A patent/FR2231742B1/fr not_active Expired
  • 1974-06-03 GB GB2449074A patent/GB1445264A/en not_active Expired
  • 1974-06-04 DE DE2426969A patent/DE2426969C3/de not_active Expired
  • 1974-06-04 JP JP6328174A patent/JPS5422448B2/ja not_active Expired

Patent Citations (3)

Also Published As

Similar Documents