US3926776A - Method and apparatus for wax deoiling - Google Patents

Method and apparatus for wax deoiling Download PDF

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Publication number
US3926776A
US3926776A US484217A US48421774A US3926776A US 3926776 A US3926776 A US 3926776A US 484217 A US484217 A US 484217A US 48421774 A US48421774 A US 48421774A US 3926776 A US3926776 A US 3926776A
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wax
plates
melting point
temperature
constituents
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Roy E Irwin
Alfred Aufhauser
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Priority to US484217A priority Critical patent/US3926776A/en
Priority to CA229,394A priority patent/CA1049435A/en
Priority to IN1230/CAL/1975A priority patent/IN143306B/en
Priority to ZA00754018A priority patent/ZA754018B/xx
Priority to DE19752528185 priority patent/DE2528185A1/de
Priority to BR5144/75D priority patent/BR7503999A/pt
Priority to IT50242/75A priority patent/IT1040735B/it
Priority to AU82601/75A priority patent/AU494383B2/en
Priority to US05/639,201 priority patent/US4013541A/en
Application granted granted Critical
Publication of US3926776A publication Critical patent/US3926776A/en
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    • 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/36—Recovery of petroleum waxes from other compositions containing oil in minor proportions, from concentrates or from residues; De-oiling, sweating

Definitions

  • the lower melting point constituents of the confined wax composition become progressively melted responsive to gradual increments of temperature increase and drain transversely along the plates through a distance which is from about 4 to 24 inches and preferably is of the order of 6 to 12 inches so as to become separated from the residual end product wax.
  • the deoiling thus accomplished is much more effective and more rapid as compared with sweating procedures. It compares favorably in these respects to deoil ing by solvent extraction.
  • the installation cost of this process is a fraction of the cost of conventional solvent deoiling.
  • This invention relates to the separation of lower melting point constituents (generally oil and isoparaffins) of a slack wax for the recovery of a deoiled commercially acceptable paraffin wax.
  • the invention makes refined paraffin waxes from slack waxes by a novel method and apparatus requiring a low cost installation and giving yields comparable to those accomplished in a solvent deoiling process.
  • Slack wax is a mixture containing isoparaffins. normal paraffins and also lower melting point constituents usually referred to as oils and naphthenic constituents.
  • the slack wax may contain from about 5% of oil as determined by ASTM test No. D 72l.
  • the wax sweating as heretofore carried out also is inefficient in that the separation of the oil and other lower melting point constituents is far from complete, with the result that in order to reduce the oil content of the hard wax to desired specifications it is not unusual to employ several successive sweating operations.
  • the disadvantages incident to sweating as a method for reducing the amount of low melting point constituents in a wax composition such as slack wax has led the industry to place reliance for the most part on the solvent extraction procedure wherein a wax such as slack wax is dissolved in a solvent such as methylethylketone (or methylisobutylketone) followed by chilling the solution to cause precipitation of the desired portion of the wax which is filtered out using a rotary vacuum filter.
  • solvent extraction does not reduce the oil content of the wax to a sufficient extent in one stage and the wax-rich product resulting from the initial extraction is reslurried at least once with additional solvent followed by cooling and subsequent filtration. By two or more successive operations the resulting product is expected to contain less than l% of oil.
  • the equipment for solvent extraction requires a very substantially greater capital investment.
  • the equipment used for solvent extraction as a matter of economics does not lenc itself to the economic construction of processing equipment for small-scale operation.
  • a still further object of this invention is to provide an economic procedure for deoiling slack wax or similar wax composition which may be employed to advantage as to the production of lubricating oil distillates.
  • the various section units including those for accomplishing distillation, solvent extraction for the removal of low viscosity index oils, dewaxing the extracted oils or raffinates and final finishing by clay treatment of hydrogenation are fairly balanced to capacity in each section to produce the maximum throughput of finished oils.
  • a body of slack wax or the equivalent is confined so as to be caused to occur in the form of a slab which ranges in thickness from about 1/! 6 inch to /2 inch and the width of which is of the order of 4 to 24 inches.
  • the slab is confined between surfaces, the temperature of which is subject to control, and the slab as so confined is so disposed that drainage of oil or other lower melting point constituents occurs across the aforesaid width of the slab provides a depth of about 4 to 24 inches going from the upper margin to the lower margin.
  • the length of the slab is not critical and may be determined according to the desired size of the plant installation. Thus, the length of the slab may range from only a few inches to as long as feet or more.
  • the lower margin of the slab as thus held between the two surfaces is open in order to permit such lower melting point constituents as may become formed to drain therefrom for collection in a suitable receptacle.
  • the upper margin of the device is open so that the space between the surfaces may initially be filled with a charge of slack wax or recycled wax by flowing it in when in the melted state.
  • the slack wax or recycled wax is cooled by means of the conduits to become a solid mass having a temperature usually several degrees lower than the melting point of the wax in process.
  • the temperature of the surfaces which confine the slab of wax is gradually increased from an initial temperature at which the wax is solid through temperatures at which the lower melting point of constituents tend to become selectively melted.
  • An environment is provided wherein the lower melting point constituents as they become reduced to the liquid state find escape paths such that their removal is much more effective and rapid as compared with the wax sweating procedures heretofore used.
  • the thin slabs of oilcontaining wax are confined in the spaces between a succession of plates or sheets which are vertically dis posed and which are spaced from each other so as to afford a battery of cells wherein the spacing between the plates is the aforesaid distance of about 1/ l 6 inch to about V2 inch.
  • the width of each of the plates being such that a slab of wax may be confined between them which. as aforesaid. is of the order of 4 inches to 24 inches in depth from its upper margin to its lower margin.
  • the spaces between the plates are open at the top and at the bottom. While the spacing between the plates may be even less than 1/16 inch. the overall operation becomes more costly. If the spacing exceeds inch.
  • the drainage of the lower melting point constituents becomes less efficient with wider spacing.
  • the spacing between the plates is from about /a inch to A inch.
  • the drainage of the lower melting point constituents becomes less efficient and the yield becomes decreased if the depth of the cell across which drainage occurs is substantially greater than 24 inches.
  • the cells are produced so that the depth across which drainage occurs is of the order ofo inches to 12 inches. In a commercial installation it ordinarily is the case that the cell plates are disposed with the width across which drainage occurs at or close to the true vertical, namely, 90 to the horizontal. However, while this is preferred, it is not critical.
  • the term vertically disposed as used herein and in the claims is to be understood as compre hending any disposition of the plates other than the true vertical so long as the vertical dispostion relative to the horizontal is sufficient to induce effective gravitational drainage of the lower melting point constitu ents leaving the desired hard wax within the cells.
  • the temperature of the plates is controlled by conduits for a temperature-controlling fluid which may be gaseous such as high velocity air but preferably is a fluid such as water.
  • a temperature-controlling fluid which may be gaseous such as high velocity air but preferably is a fluid such as water.
  • These conduits successively traverse the plates of the battery of cells and the cells between the plates and they are distributed about the plates in thermally-conductive relation therewith so that the entire surface of each plate may have its temperature controlled substantially uniformly throughout.
  • the conduits typically are in the form of pipes about A inch to A inch in internal diameter and distributed so that there are sufficient pipes to maintain rapid heat transfer.
  • the conduits are supplied with the tempera ture-Controlling fluid in any suitable way. as by the employment of a header that is connected with a source which supplies fluid at the desired temperature for use during the different phases of the deoiling pro cess. Similarly.
  • the conduits discharge into a complementary header from which the fluid may be returned so as to be recycled.
  • the plates may be made of any suitable structural heat-conductive material. Ordinarily the plates are in the form of sheets of a metal such as tinned copper, tinned brass. aluminum. stainless steel. or protected iron. Best results are obtained by the use of a material having a high degree of thermal conductivity. Plates or sheets of tinned copper or of aluminum are preferred. For similar reasons the conduits preferably are made from tinned copper or aluminum.
  • the battery of cells may be filled with the wax when it is at a temperature somewhat above its melting point.
  • the wax-receiving receptacle below the battery of cells is adapted and arranged so that it may be filled with cold water to a level at or slightly above the lower margin of the plates.
  • the wax because of its lesser specific gravity floats on the water and likewise becomes cooled sufficiently to solidify.
  • the plates themselves at this stage are maintained at a temperature below the melting point of the wax. The wax, therefore. fills the interstices between the plates and becomes solidified.
  • the water is drained from the receptacle and the temperature of the plates is gradually increased so as to cause the lower melting point constituents to drain off to the desired extent. These constituents are collected and removed for further processing.
  • the residual wax from which the oil has been largely removed may now be recovered by heating the plates to a temperature sufficiently above the melting point of the wax to cause the wax to melt relatively rapidly and so that it may be collected and separately recovered.
  • While the practice of this invention is to be regarded as generally applicable to the removal of lower melting point constituents from certain wax compositions. it is especially adapted for us in connection with the deoiling of slack wax of the type that occurs during the production of lubricating oil distillates.
  • slack waxes usually have a melting point in the range from about ll2 to F.
  • the oil content may be from about 5% to about 30%.
  • the amount and nature of the lower melting point constituents such as oil and isoparaffins varies depending on the source from which the slack wax was obtained, and the method of refining.
  • the objective of the complete de oiling procedure is to recover the hard wax, generally normal paraffins wherein the oil content has been reduced to a prescribed value such as /z% to 1%.
  • the slack wax is heated to a temperature of about 15F above its melting point.
  • the wax-receiving receptacle is filled with water at a temperature below the melting point of the wax. e.g. about 70'F. to a level at or just above the bottom margins of the cells.
  • cooling water at a tempeature of about 50F to about 80F below the melting point of the wax is caused to flow through the conduits in the cell battery.
  • the temperature of the confined solidified wax may. for example. be from about lF to about 20F below its melting point.
  • the removal of the lower melting point constituents is initiated by causing the temperature of the cell plates to be gradually increased. e.g. at the rate of about lF to about F per hour. and this is continued until the temperature reaches a predetermined maximum which may. for example. be from about 2F to about 5F below the melting point of the wax.
  • a predetermined maximum which may. for example. be from about 2F to about 5F below the melting point of the wax.
  • the oil and any other lower melting point constituents find avenues for readily draining through channels adjacent the plate surfaces, leaving the harder wax behind. During this period the separated oil is collected in the waxreceiving pan and is removed to a suitable container.
  • the plates are then heated rapidly to a temperature of about l0F to about F above the melting point of residual hard wax. Under these conditions the cells are rapidly cleared and the deoiled wax is collected in the waxreceiving pan and recovered.
  • the oil content of the original slack wax may be reduced by 40% 80% of the original oil content. This may be accomplished in about 12 hours creating by-product in the form of foots oil (heating oil or cracking stock).
  • the loss in the form of foots oil may be in the order of to 50% of the weight of the original slack wax.
  • the foots oil is largely a combination of oils and isoparaffins.
  • the reduction of oil content accomplished varies with the original oil content of the slack wax.
  • High oil contents in slack waxes. such as 30%, are less responsive to treatment than those having an oil content of 7% to 20%.
  • As an oil content in the hard wax of less than 1% is desirable, the best ultimate yields of hard wax are obtainable by a second deoiling treatment carried out substantially in the same manner as the first deoiling treatment. Since the oil content in the hard wax has been substantially reduced by the first treatment. the amount of foots oil produced is much less in the second treatment.
  • the decrease in weight in the second deoiling treatment will be substantially less than in the primary treatment.
  • each operation requiring about l2 hours duration, it is possible to reduce the oil content of the residual hard wax to around 0.3% to 0.9%.
  • the results may vary depending upon the original composition of the slack wax and the nature of the crystal structure produced in changing the slack wax from liquid phase to solid phase in the cells.
  • the yields of hard wax with a certain oil content are of the same order as those obtained by the solvent extraction process but use much less costly processing equipment.
  • the recovered wax. after conventional finishing treatment fully meets industrial specifications for a wax of the type in question.
  • FIG. 1 is a perspective view of a battery ofwax deoiling cells embodying and using the invention
  • FIG. 2 shows a section taken on the line 2--2 of FIG. 1 in combination with the tray that is used therewith to provide the deoiling unit;
  • FIG. 3 is a section on an enlarged scale. with the central portion broken away. taken on the line 3-3 of FIG. 2;
  • FIG. 4 is a diagrammatic representation of the deoil' ing unit comprising a single cell battery and tray together with accessory supply and product recovery equipment which illustrates the practice of this inven tion in a typical wax deoiling procedure;
  • FIG. 5 is an end elevation that is illustrative of a typical arrangement of a plurality of the deoiling units suitable for a commercial installation.
  • the cell battery is indicated generally by the reference character 10. It comprises a succession of sheets or plates 11 which extend between the side bars 12. In the illustrative embodiment shown. the plates are spaced from each other by a distance of /s inch and the width from top to bottom is 8 inches. Twenty-gauge aluminum sheeting. for example. affords a preferred material for the cell plates.
  • the plates 11 and the cell spaces between them are traversed by a plurality of conduits for a temperature-controlling fluid which ordinarily is water. In the embodiment shown. the conduits are copper tubes having an inside diameter of about Vs inch. These conduits are distributed throughout the lateral area of the plates 11 and since they are in heat-conductive relation therewith. the temperature of the plates 11 may be controlled and adjusted sub stantially uniformly throughout.
  • the conduits 13 open into a header l4 and at the other end they open into a header 15 so that the temperature-controlling fluid may be caused to flow through the conduits 13 from one header to the other.
  • the cell battery is carried within the wax-receiving tray 16, which is sloped downwardly toward its center as indicated in FIG. 2 in order to facilitate the withdrawal of liquid material from the tray.
  • the tray may be made of appropriate material. eg steel plate with a rust-resistant coating or stainless steel.
  • the first step in carrying out the invention using the exemplified equipment shown in the drawings is to fill the lower portion of the tray 16 with water at a temperature below the melting point of wax.
  • Water is supplied from any available source such as the water main l7 and by opening the valves 18 and 19 the water is directed by the line 20 into the tray 16.
  • the level of the water 21 in the tray 16 is determined by the level ofthe outlet line 22, which directs any overflow to the settling tank 23 and which is steanrtraced. as partially indicated at 23A.
  • This line preferably is steamtraced so as to minimize the possibility of blockage due to any wax particles that might flow into this line.
  • the valves 18 and 19 are closed. As aforesaid.
  • this water level is at or slightly above the bottom margins of the plates It in the cell battery It).
  • Slack wax obtained from storage (not shown) is pumped by line 24 into the wax-heating tank 25 wherein the wax is heated to a temperature above the melting point of the wax by the employment of a suitable heating element such as the steam coil 26.
  • the desired temperature may be maintained by the use of the temperature controller 27 which controls the action of the valve 28 so as to supply the amount of heat required to maintain the wax at the desired tempera ture.
  • the wax When the wax has attained the proper temperature it is pumped by pump 29 through the line 30. which is steanvtraccd as indicated partially at 30A, to the distributor pipe 31 which distributes the melted wax over the extent of the cell battery so as to till all of the cells.
  • Uniform filling of the individual cells is promoted by the provision in the plates 11 of openings 32 which permit the wax to ilovv from one cell to the other so that the wax in the various cells will assume the same level
  • any excess wax is permitted to drain from the battery 10 through the line 33 to the overflow slack wax tank 34 wherein the desired temperature is maintained by the heating unit in the form of steam coil 35 subject to the temperature controller 36 which controls the operation of the valve 37.
  • the overflow wax is pumped from the overflow tank 34 to the waxheating tank through the line 38 by the pump 39.
  • the cold water 21 in the tray 16 the level of which is at or slightly above the lower margin of the plates of the cell battery. serves to float the wax during its solidification and cause it to be retained confined between successive plates of the battery.
  • the cold water is likewise circulated through the conduits in the battery of cells. the entire mass of wax within the respective cells becomes converted to the solid state as the result of cooling the wax to a temperature below the melting point of the wax.
  • the circulation of the cold water is stopped and the water 21 in the tray 16 is drained out through the line 48 controlled by the valve 49 and is directed by line 22 to the settling tank 23.
  • the wax in the battery of cells has now been prepared for the removal of the lower melting point constituents of the wax by appropriate and controlled heat treatment.
  • the water in the tank 42 is ini- Ill tially brought to a temperature which. for example. may be about It] below the melting point of the wax.
  • the heating element 50 which is in the form ofa steam coil.
  • the temperature of the water in the tank 42 may be controlled by the temperature controller 51 which regulates the valve 52. as desired. for admitting steam from the steam line 53 in sufficient amount to maintain the desired water temperature.
  • These controls for the water in the water tank 42 are arranged so as to gradually increase the water temperature at a predetermined rate which ordinarily varies from about 1 to about 5 per hour.
  • the lower melting point constituents such as oil and isoparaffins begin to drain from the wax mass transversely across the width of the plates 1 1 so as to flow down by gravity and drop from the lower margins of these plates into the tray below.
  • flow from the tray 16 is permitted to occur only through line 54 controlled by the valve 55 which is open. thereby allowing the oil mixture to be discharged into the foots oil storage tank 56.
  • the gradual heating of the wax is continued until the residual wax has the composition that is sought to be obtained.
  • This composition corresonds with that which has been found to be desirable as the result of prior laboratory evaluations. Once the correct composition has been predetermined by laboratory evaluation, commercial operations can readily be controlled accordingly so as to obtain the desired composition of the retained wax.
  • the valve 55 controlling the removal of the foots oil is closed and the temperature of the water from the water tank 42 that is flowed through the battery 10 is rapidly increased to a temperature sufficiently above the melting point of the wax that remains in the battery so that the cells will become substantially cleared of any retained wax.
  • the melted wax is drained from the tray 16 through the steamtraced line 57 upon opening the valve 58, which is closed as soon as the tray has been completely drained.
  • the finished wax is directed by the line 57 into the finished wax-holding tank 61 from which it may be pumped by the pump 59 in line 60 for such working up as may be desired.
  • a wax deoiling chamber 64 having thermally insulated walls 65 and operatively connected by suitable valve-controlled conduits under common control to common supply sources of water and wax and to common receivers for the different effluents. as illustrated hereinabove and in FIGS. 1-4 in connection with a single unit. If desired, trays 66 may be provided to catch any accidental spillage.
  • the chamber 65 desirably is within a larger building 67 the walls of which likewise preferably are provided with thermal insulation.
  • a 2-inch layer of polyurethane foam provides satisfactory thermal insulation for both the building 67 and for the wax deoiling chamber 65, respectively.
  • the insulation is desirable in order to obtain better temperature control during the various stages of the deoiling procedure.
  • the building 67 provides protection not only for the operator but also for the supply tanks, receiving receptacles, pumps, control devices, etc., that have been described hereinabove.
  • the chamber 64 may be supplied with observation windows 68 the upper one having an observation platform 60 associated therewith.
  • the atmosphere within the building 67 may be kept fresh for breathing by maintaining the pressure of the atmosphere in the building 67 slightly higher than that of the atmosphere in deoiling chamber 64 so that. to the extent that there may be any seepage, the air will seep into the chamber 64 from the building 67 with concomitant expulsion in corresponding amount of contaminated air from the chamber 64 through the outlet duct 70 and to the outside atmosphere.
  • EXAMPLE The following example using laboratory-scale tests illustrates the utility and advantages of this invention in comparison with conventional sweating and in comparison with the solvent extraction method for the removal of oil and isoparaffins, essentially the same slack wax starting material being used in each case.
  • the wax used in each test was typical slack wax having an oil content of 8-9% (ASTM-D-72I-68), a melt point of I23.8F (ASTM-D-87-66) and a penetration at 77F of 30/32 (ASTM-D-I 321-70).
  • a battery of I44 cells was employed made up using aluminum plates of 26 gauge separated from each other by I/ I2 inch and traversed by conduits '74 inch in inside diameter for the flow therethrough of the water used to control the temperature of the plates.
  • the cell battery which was used contained I44 cells defined by vertical plates, the vertical dimension being such as to be confined between each pair of plates a body of wax substantially 8 inches in depth from the upper margin to the lower margin. For laboratory use, the plates were substantially I inches in horizontal length.
  • the wax was introduced into the cells in the manner hereinabove described when at a temperature of I40F and it was reduced to the solid state by cooling to IOOF.
  • the deoiling was accomplished by increasing the temperature of the temperature-controlling water at the varying rate of 1F to F per hour over a period of 12 hours. At the conclusion of the 12-hour period, deoiling was discontinued and the residual hard wax was recovered by raising the temperature of the temperature-controlling water to 150F at which the residual hard wax became melted and was drained from the cells. The cell battery was then charged a second time with the slack wax having the properties aforesaid and the deoiling was carried out in the same way so as to obtain a second quantity of the residual wax. The two quantities of 10 deoiled wax were then commingled and the commingled quantities of slack wax were subjected to deoiling following the same regime.
  • a sweating pan was used of the type currently employed by oil refineries that employ this sweating procedure.
  • a block of solidifled slack wax measuring 8 X 8 X 8 inches and having the properties aforesaid was supported so as to permit drainage and was exposed to gradually increasing temperature in a temperature-controlled oven wherein the temperature was increased at the rate of about /z"F to 5F per hour from a starting temperature of I05F. the total sweating period being 30 hours.
  • methylethylketone-toluol was used as the solvent and conventional plant solvent dewaxing procedure was adapted to a laboratory-scale operation suitable for application to slack wax having the properties hereinabove mentioned.
  • this procedure an amount of 50 grams of slack wax was weighed and added to grams of a 50% MEK 50% toluol mixture in a flask. The temperature was raised until the wax was completely dissolved in the MEK-toluol mixture. With vigorous stirring of the mixture. the flask was cooled at a rate of about 2F per minute until a uniform mixture resulted. At this point. temperature reduction rate was increased until the temperature was lowered to 40F or 50F.
  • a glass funnel with a fritted glass bottom was covered with medium filter paper for the following procedure.
  • the funnel discharged the filtrate into an Erlenmeyer flask with a side neck which was connected to a vacuum pump and receiver.
  • the funnel was maintained at a constant temperature of 50F. while the slurry was filtered through the filter paper in the funnel.
  • a wax cake was formed. removed from the funnel and weighed. The cake was then heated under vacuum until all the ketone mixture was distilled. The yield of wax was then determined by weighing.
  • the second solvent extraction was then carried out in the same manner as described above for the primary solvent operation. The yield of weight of the wax was determined, after which a laboratory analysis determined oil content. penetration and melting point of the wax.
  • a method of separating lower melting point components from higher melting point components of a wax composition which comprises confining in the solid state between opposed surfaces :1 body of wax about lflo to about 2 inch in thickness with an upper margin disposed above its lower margin for permitting selective drainage of melted components of said wax composition to drain toward said lower margin.
  • said body of was being from about 4 to about 24 inches in depth from said upper margin toward said lower mar gin. gradually raising the temperature of said surfaces through a temperature range during which lower melting point constituents selectively drain from said body of wax leaving residual higher melting point wax in the solid state in the space between said surfaces. recovering the drained lower melting point constituents and thereafter melting and recovering said higher melting point constituents separated from said lower melting point constituents.
  • said wax composition is slack wax containing normal paraffin wax and other constituents of lower melting point and wherein during said gradual heating said lower melting point constituents are selectively drained from normal paraffin wax retained between said surfaces.
  • ln wax de-oiling apparatus for separating lower melting point constituents from higher melting point constituents which comprises a succession of plates having vertically disposed spaces therebetween. a plurality of conduits that successively pass through said plates in thermally-conductive relation therewith, means for directing a temperature-controlling liquid through said conduits and means for regulating the tempertaure of said liquid.
  • the improvement which comprises a battery of said plates which are spaced from each other by a distance between H l6 inch and about V2 inch and which are adapted to confine between them a body of wax composition about 4 to about 24 inches in width extending upwardly from adjacent the lower margin.
  • means for emptying said cold water from said tray when the wax composition in the spaces between said plates is in said solid state means for thereafter gradually increasing the temperature of said temperture-control liquid with concomitant gradual heating of the wax composition in the spaces between said plates to a temperature at which the lower melting point constituents drain into said tray leaving the higher melting point constituents retained between said plates and means for directing away and recovering said lower melting point constituents drained into said tray.
  • said means for regulating the temperature of said temperature-control liquid is adapted to raise the temperature of said plates to a temperature at which the residual higher melting point constituents are melted and drain into said tray. and means for directing away and recovering said higher melting point constituents drained into said tray separately from said lower melting point constituents.
  • Apparatus according to claim 7 wherein said battery and said tray are disposed within a first chamber and wherein a said second chamber is disposed about said first chamber.
  • Wax de-oiling apparatus wherein said plates have a plurality of openings therein which permit passage of molten wax from one space to an adjoining space between said plates thereby facilitating the distribution of molten wax among the spaces between said plates when said plates are being filled UNITED STATES PATENT AND TRADEMARK OFFICE CERTIFICATE OF CORRECTION PATENTNO.: 6,776

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US484217A 1974-06-28 1974-06-28 Method and apparatus for wax deoiling Expired - Lifetime US3926776A (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US484217A US3926776A (en) 1974-06-28 1974-06-28 Method and apparatus for wax deoiling
CA229,394A CA1049435A (en) 1974-06-28 1975-06-16 Method and apparatus for wax deoiling
IN1230/CAL/1975A IN143306B (ar) 1974-06-28 1975-06-21
DE19752528185 DE2528185A1 (de) 1974-06-28 1975-06-24 Verfahren zum abtrennen der niedriger schmelzenden von den hoeher schmelzenden komponenten eines paraffingemisches und einrichtung zu seiner durchfuehrung
ZA00754018A ZA754018B (en) 1974-06-28 1975-06-24 Method and apparatus for wax deoiling
BR5144/75D BR7503999A (pt) 1974-06-28 1975-06-26 Processo para separacao,em uma composicao de parafina,de componentes de ponto de fusao superior;e aperfeicoamento em aparelho de desoleificacao de parafina
IT50242/75A IT1040735B (it) 1974-06-28 1975-06-26 Procedimento ed apparecchio per la rimozione di componenti a basso punto di fusione da cere
AU82601/75A AU494383B2 (en) 1974-06-28 1975-06-30 Method for wax deoiling
US05/639,201 US4013541A (en) 1974-06-28 1975-12-09 Method and apparatus for wax deoiling

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US484217A US3926776A (en) 1974-06-28 1974-06-28 Method and apparatus for wax deoiling

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US05/639,201 Continuation-In-Part US4013541A (en) 1974-06-28 1975-12-09 Method and apparatus for wax deoiling

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BR (1) BR7503999A (ar)
CA (1) CA1049435A (ar)
DE (1) DE2528185A1 (ar)
IN (1) IN143306B (ar)
IT (1) IT1040735B (ar)
ZA (1) ZA754018B (ar)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4013541A (en) * 1974-06-28 1977-03-22 Irwin Roy E Method and apparatus for wax deoiling
EP0892033A1 (de) * 1997-07-16 1999-01-20 Sulzer Chemtech AG Verfahren und Vorrichtung zur Gewinnung von Paraffin oder Paraffinfraktionen

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1898930A (en) * 1927-07-08 1933-02-21 Indo Burma Petroleum Company L Apparatus for sweating or treating paraffin wax or the like

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1898930A (en) * 1927-07-08 1933-02-21 Indo Burma Petroleum Company L Apparatus for sweating or treating paraffin wax or the like

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4013541A (en) * 1974-06-28 1977-03-22 Irwin Roy E Method and apparatus for wax deoiling
EP0892033A1 (de) * 1997-07-16 1999-01-20 Sulzer Chemtech AG Verfahren und Vorrichtung zur Gewinnung von Paraffin oder Paraffinfraktionen
US6074548A (en) * 1997-07-16 2000-06-13 Schumann Sasol Gmbh & Co. Kg Process for obtaining paraffin or paraffin fractions
CN1085242C (zh) * 1997-07-16 2002-05-22 舒曼·萨索尔股份有限两合公司 获取石蜡或石蜡馏份油的方法及设备

Also Published As

Publication number Publication date
BR7503999A (pt) 1976-06-29
CA1049435A (en) 1979-02-27
IN143306B (ar) 1977-10-29
DE2528185A1 (de) 1976-01-15
ZA754018B (en) 1976-06-30
IT1040735B (it) 1979-12-20
AU8260175A (en) 1977-01-06

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