US2129282A - Refining mineral lubricating oils - Google Patents
Refining mineral lubricating oils Download PDFInfo
- Publication number
- US2129282A US2129282A US64217A US6421736A US2129282A US 2129282 A US2129282 A US 2129282A US 64217 A US64217 A US 64217A US 6421736 A US6421736 A US 6421736A US 2129282 A US2129282 A US 2129282A
- Authority
- US
- United States
- Prior art keywords
- oil
- ether
- propylene glycol
- solvent
- temperature
- 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.)
- Expired - Lifetime
Links
- 239000010688 mineral lubricating oil Substances 0.000 title description 10
- 238000007670 refining Methods 0.000 title description 4
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 87
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 47
- 239000003921 oil Substances 0.000 description 32
- 229960004063 propylene glycol Drugs 0.000 description 29
- 235000013772 propylene glycol Nutrition 0.000 description 29
- RCJVRSBWZCNNQT-UHFFFAOYSA-N dichloridooxygen Chemical compound ClOCl RCJVRSBWZCNNQT-UHFFFAOYSA-N 0.000 description 19
- 239000002904 solvent Substances 0.000 description 19
- 239000001993 wax Substances 0.000 description 15
- 238000000605 extraction Methods 0.000 description 13
- 238000000034 method Methods 0.000 description 13
- 230000008569 process Effects 0.000 description 13
- 239000000470 constituent Substances 0.000 description 11
- PPKPKFIWDXDAGC-IHWYPQMZSA-N (z)-1,2-dichloroprop-1-ene Chemical compound C\C(Cl)=C\Cl PPKPKFIWDXDAGC-IHWYPQMZSA-N 0.000 description 10
- 239000010687 lubricating oil Substances 0.000 description 9
- 239000002480 mineral oil Substances 0.000 description 6
- 238000002844 melting Methods 0.000 description 5
- 230000008018 melting Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 230000006872 improvement Effects 0.000 description 4
- 235000010446 mineral oil Nutrition 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 239000011877 solvent mixture Substances 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 230000001050 lubricating effect Effects 0.000 description 2
- 239000010705 motor oil Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
Definitions
- This invention relates to a process of refining mineral oils and specifically petroleum lubricating oils of the type employed in the lubrication of internal combustion engines and commonly known as motor oils.
- the invention further relates to a process of extracting such oils with a specific solvent, namely, beta beta dichlor diethyl ether, hereinafter referred to as chlor-ether.”
- a specific solvent namely, beta beta dichlor diethyl ether, hereinafter referred to as chlor-ether.
- the present invention relates to an improvement in the use of beta beta dichlor diethyl ether in lubricating oil extraction processes wherein undesirable naphthenic constituents are removed from the parafiinic com*- ponent of the oil.
- One object of the invention is to facilitate the use of said chlor-ether solvent in the extraction of wax-containing lubrieating oil stocks.
- Another object of the invention is to increase the selective solvent action of said solvent by the addition of minor amounts of certain modifying agents.
- midcontinent and Salt Creek lubricating uistillates such as motor oil distillates falling within the viscosity range of 20 S. A. E. number, difiiculty has frequently been encountered with separation of wax in the extraction process.
- the wax will usually crystallize in the form of a thick mush or magma at ordinary temperatures and even at temperatures in the range of 100425 F. This is especially true of the heavier distillates which contain higher melting waxes.
- miscibility temperature of mineral oil and chlor-ether is very materially raised by the addition of propylene glycol.
- the following table shows the effect on the miscibility temperature of chlor-ether and a cylinder stock derived from Salt Creek crude. Three ratios of solvent to oil are given, and temperatures of complete miscibility of oil and solvent are given with and without the addition of 13% by volume of propyleneglycol to the chlor-ether.
- propylene glycol to modify the-solvent action of chlor-ether in this manner I am enabled to carry out my refining operation at temperatures ranging from to 200 F.
- the propylene glycol prevents the chlor-ether from dissolving, at these relatively high temperatures, excessive amounts of those hydrocarbons which are desired in the rafilnate, yet it does not prevent the solution of naphthenic constituents of the oil in the solvent.
- the efl'ect of the addition of propylene glycol to chlor-ether may also be observed by referring to the accompanying drawing which forms a part of this specification.
- the graph shows the results of extracting a mineral lubricating oil distillate of 60 S; A. E. viscosity range derived from Salt Creek crude. It will be noted from the chart that for a given yield of rafllnate oil, the permissible temperature of operation is greatly increased by the addition of propylene glycol. Thus, at a 75% yield, chlor-ether requires a temperature of 112 F. whereas chlor-ether with 8% propylene glycol requires a temperature of about 138 F., well above the melting point of this 'waxy oil. Likewise, 12% propylene glycol permits a temperature of 158 F. with this same yield.
- the upper layer consisting of substantially pure propylene glycol.
- the solvent In carrying out my process I prefer to analyze the solvent before use to determine the amount of propylene glycol modifying agent which is present and then adjust the concentration by adding to the solventsupply'the necessary amount of either chlor-ether or propylene glycol.
- I may also initially extract a wax-containing oil at an elevated temperature above the melting point of the wax using between 10% and 30% of propyleneglycol in the solvent mixture. I may then cool the extract phase to a comparatively low temperature of the order of 50 1''. to: 90 F. whereupon propylene glycol and a further quantity of oil or raflinate is caused to separate.
- This second rainnate fraction maythen be further treated in the process or it may be disposed of as a second grade lubricating oil having intermediate viscosity index.
- beta beta dichlor diethyl ether wherein the oil is intimately contacted with the ether and the oil and ether are separated in two phases in which the heavier ether phase contains dissolved undesirable naphthenic constituents of the oil, the improvement comprising avoiding difllculties resulting from the separation of solid paraflin wax as a third phase in the process by adding between 5% and 20% of propylene glycol to the beta beta dichlor diethyl ether whereby the miscibility temperature of said ether and said lubricating oil is raised substantially above the melting point of said waxy oil, and conducting the extraction at a temperature between the melting point of said waxy oil and the said miscibility temperature,
Description
P 1938- J. M. PAGE, JR 2,129,282
REFINING MINERAL LUBRICATING OILS I Filed Feb. 17, 1936 8 F? I g grill, s g Q) gtjg" I h Y w {)2 z I a E 7 1 2 A g 8 g g g 1 N v a 0 :2, K R a Vie Z ff INVENTO James Morris DagQ BY B JQ DMMW ATTORNEY Patented Sept. 6, 1938 PATENT OFFICE 2,129,282 marmmc MINERAL LUBRICATING on.s
James Morris Page, In,
Casper, Wyo., assignor to Standard Oil Company, Chicago, 111., a corpo ration of Indiana Application February 1'1, 1936, Serial No. 64,217
5 Claims.
This invention relates to a process of refining mineral oils and specifically petroleum lubricating oils of the type employed in the lubrication of internal combustion engines and commonly known as motor oils. The invention further relates to a process of extracting such oils with a specific solvent, namely, beta beta dichlor diethyl ether, hereinafter referred to as chlor-ether." The use of this solvent for the extraction of mineral lubricating oils has been previously described in United States Patent. No. 2,003,238, entitled Process of separating mineral oils" by H. T. Bennett, filed June 23, 1933.
More particularly, the present invention relates to an improvement in the use of beta beta dichlor diethyl ether in lubricating oil extraction processes wherein undesirable naphthenic constituents are removed from the parafiinic com*- ponent of the oil. One object of the invention is to facilitate the use of said chlor-ether solvent in the extraction of wax-containing lubrieating oil stocks. Another object of the invention is to increase the selective solvent action of said solvent by the addition of minor amounts of certain modifying agents. In the extraction of midcontinent and Salt Creek lubricating uistillates such as motor oil distillates falling within the viscosity range of 20 S. A. E. number, difiiculty has frequently been encountered with separation of wax in the extraction process. Where the distillate contains over 5% of paraflin wax and frequently as much as 10 or 15% thereof, the wax will usually crystallize in the form of a thick mush or magma at ordinary temperatures and even at temperatures in the range of 100425 F. This is especially true of the heavier distillates which contain higher melting waxes.
When extracting such wax-containing oils with beta beta dichlor diethyl ether it is usually necessary to maintain the temperature of the oil undergoing extraction below F. in order to obtain a satisfactory yield of refined lubricating oil,
or raflinate, having the desired viscosity index.'
It is, accordingly, not feasible to carry out the extraction process at a temperature sufllciently high to maintain the wax in liquid form.
I have now discovered that the extraction of mineral lubricating oils with chlor-ether is greatly improved by incorporating in the chlOr-ether a small amount, usually from2 to 20%, but possibly as much as 30%, or propylene glycol. I have found that propylene glycol is miscible with chlorether to a very considerable extent as shown by the following table which indicates the solubility Propylene glycol in mixture,
' Temperature percent The lowering of the miscibility temperature at concentrations of propylene glycol in excess of about 16% is due to the reduction in the proportion of water in the mixture.
I have also found that the miscibility temperature of mineral oil and chlor-ether is very materially raised by the addition of propylene glycol. The following table shows the effect on the miscibility temperature of chlor-ether and a cylinder stock derived from Salt Creek crude. Three ratios of solvent to oil are given, and temperatures of complete miscibility of oil and solvent are given with and without the addition of 13% by volume of propyleneglycol to the chlor-ether.
By using propylene glycol to modify the-solvent action of chlor-ether in this manner I am enabled to carry out my refining operation at temperatures ranging from to 200 F. The propylene glycol prevents the chlor-ether from dissolving, at these relatively high temperatures, excessive amounts of those hydrocarbons which are desired in the rafilnate, yet it does not prevent the solution of naphthenic constituents of the oil in the solvent.
As an example of the use of my new modified chlor-ether solvent, two volumes of pure chlorether to one volume of Salt Creek cylinder stock were used in an extraction carried out at -F. A yield of rafiinite oil of 58.2% was obtained, the oil having a viscosity index of 88. In comparison with this two volumes of chlor-ether solvent containing 13%, by volume, of propylene glycol was applied to one volume or the same oil at the same temperature and a yield of 80% of raffinate oil was obtained, the oil having a viscosity index of 85.2, only slightly lower than the viscosity index obtained without the use of propylene glycol. It is characteristic of my process that, when conditions are selected such that the yield of raflinate oil obtained is greatly increased, the viscosity index is adversely affected only a very little, if at all. Not only is the yield increased but the selectivity of the solvent at relatively high extraction temperatures is also improved and a sharper separation is obtained between the undesired naphthenic constituents of the oil and the desirable parailinic hydrocarbons.
The efl'ect of the addition of propylene glycol to chlor-ether may also be observed by referring to the accompanying drawing which forms a part of this specification. The graph shows the results of extracting a mineral lubricating oil distillate of 60 S; A. E. viscosity range derived from Salt Creek crude. It will be noted from the chart that for a given yield of rafllnate oil, the permissible temperature of operation is greatly increased by the addition of propylene glycol. Thus, at a 75% yield, chlor-ether requires a temperature of 112 F. whereas chlor-ether with 8% propylene glycol requires a temperature of about 138 F., well above the melting point of this 'waxy oil. Likewise, 12% propylene glycol permits a temperature of 158 F. with this same yield.
One of the advantages, of my process results from the fact thatthe solubility of propylene glycol in beta beta dichlor diethyl ether is very small at low temperatures and therefore I may separate the propylene glycol from the chlorether by cooling to 34 F. or lower, for example, to 20 F. When water is present in the chlor ether solvent, it is not necessary to cool as low as this, and with chlor ether saturated with water, separation of propylene glycol (and water) occurs at about 80 F. In this case, cooling below 80 F., for example to F., will result in separation of the glycol.
On cooling two layers are formed, the upper layer consisting of substantially pure propylene glycol. In carrying out my process I prefer to analyze the solvent before use to determine the amount of propylene glycol modifying agent which is present and then adjust the concentration by adding to the solventsupply'the necessary amount of either chlor-ether or propylene glycol.
I may also initially extract a wax-containing oil at an elevated temperature above the melting point of the wax using between 10% and 30% of propyleneglycol in the solvent mixture. I may then cool the extract phase to a comparatively low temperature of the order of 50 1''. to: 90 F. whereupon propylene glycol and a further quantity of oil or raflinate is caused to separate.
This second rainnate fraction maythen be further treated in the process or it may be disposed of as a second grade lubricating oil having intermediate viscosity index.
Having thus described my invention, what I claim is:
1. The process of extracting undesirable constituents from wax-containing mineral lubricating oils which comprises intimately contacting the oil with a solvent comprising beta beta dichlor diethyl ether and from 2-30% 'of propylene glycol, maintaining the temperature of the conamass:
tactlng operation above the solidifying point of said wax-containing lubricating oil, separating said solvent and undesirable oil constituents from the reflnedmineral lubricating oil and thereafter recovering said solvent from said refined mineral oil and said undesirable oil constituents.
2. In the process of extracting undesirable naphthenic constituents from wax-containing mineral lubricating oils with beta beta dichlor diethyl ether, the improvement comprising incorporating in said ether 2-20% of propylene glycol and maintaining the temperature of said extraction operation above the miscibility temperature of said ether and said mineral oil but below the miscibility temperature of said mineral oil and said ether containing said propylene glycol.
3. In the process of: extracting undesirable naphthenic constituents from mineral lubricating oils wherein the oil is intimately contacted with beta beta dichlor diethyl ether and the undesirable constituents are removed as an extract in solution in said ether, the improvement comprising adding to said ether from 5 to 30% of propylene glycol, conducting the extraction at a temperature above the.solidifying point of the oil, separating the oil-solvent mixture into a raffinate fraction and an extract fraction, cooling said extract fraction to a temperature below 80 F. whereby said propylene glycol is caused to separate from said extract fraction and separating and recovering said propylene glycol for use, in further extraction-of additional quantities of mineral lubricating oil.
4. In the process of extracting undesirable naphthenic constituents from mineral lubricating oils wherein the oil is intimately contacted with a solvent comprising beta beta dichlor di ethyl ether, the oil and solvent mixture are permitted to separate into a raflinate fraction and an extract fraction, the raflinate fraction is sub iected to distillation to recover said solvent for reuse and produce a refined lubricating oil, andv 5. In the process of extracting lubricating oils' containing paraflin wax. with beta beta dichlor diethyl ether wherein the oil is intimately contacted with the ether and the oil and ether are separated in two phases in which the heavier ether phase contains dissolved undesirable naphthenic constituents of the oil, the improvement comprising avoiding difllculties resulting from the separation of solid paraflin wax as a third phase in the process by adding between 5% and 20% of propylene glycol to the beta beta dichlor diethyl ether whereby the miscibility temperature of said ether and said lubricating oil is raised substantially above the melting point of said waxy oil, and conducting the extraction at a temperature between the melting point of said waxy oil and the said miscibility temperature,
- whereby said wax is prevented from crystallizing as a separate phase from said mixture.
' JAMES MORRIS PAGE, JR.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US64217A US2129282A (en) | 1936-02-17 | 1936-02-17 | Refining mineral lubricating oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US64217A US2129282A (en) | 1936-02-17 | 1936-02-17 | Refining mineral lubricating oils |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2129282A true US2129282A (en) | 1938-09-06 |
Family
ID=22054355
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US64217A Expired - Lifetime US2129282A (en) | 1936-02-17 | 1936-02-17 | Refining mineral lubricating oils |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2129282A (en) |
-
1936
- 1936-02-17 US US64217A patent/US2129282A/en not_active Expired - Lifetime
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