AU613713B2 - Treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component - Google Patents
Treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component Download PDFInfo
- Publication number
- AU613713B2 AU613713B2 AU30700/89A AU3070089A AU613713B2 AU 613713 B2 AU613713 B2 AU 613713B2 AU 30700/89 A AU30700/89 A AU 30700/89A AU 3070089 A AU3070089 A AU 3070089A AU 613713 B2 AU613713 B2 AU 613713B2
- Authority
- AU
- Australia
- Prior art keywords
- stream
- hydrocarbonaceous
- distillable
- temperature
- hydrogen
- 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
Links
- 239000002699 waste material Substances 0.000 title claims description 49
- 229910052739 hydrogen Inorganic materials 0.000 claims description 58
- 239000001257 hydrogen Substances 0.000 claims description 58
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 57
- 238000000034 method Methods 0.000 claims description 33
- 239000007788 liquid Substances 0.000 claims description 31
- 150000001875 compounds Chemical class 0.000 claims description 20
- 230000015556 catabolic process Effects 0.000 claims description 11
- 238000006731 degradation reaction Methods 0.000 claims description 11
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 8
- 239000010687 lubricating oil Substances 0.000 claims description 8
- 239000003921 oil Substances 0.000 claims description 8
- 230000008016 vaporization Effects 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 6
- 239000013618 particulate matter Substances 0.000 claims description 5
- 239000002737 fuel gas Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- 239000003245 coal Substances 0.000 claims description 2
- 239000010730 cutting oil Substances 0.000 claims description 2
- 239000002440 industrial waste Substances 0.000 claims description 2
- 150000002902 organometallic compounds Chemical class 0.000 claims description 2
- 239000010914 pesticide waste Substances 0.000 claims description 2
- 239000011269 tar Substances 0.000 claims description 2
- 235000009917 Crataegus X brevipes Nutrition 0.000 claims 1
- 235000013204 Crataegus X haemacarpa Nutrition 0.000 claims 1
- 235000009685 Crataegus X maligna Nutrition 0.000 claims 1
- 235000009444 Crataegus X rubrocarnea Nutrition 0.000 claims 1
- 235000009486 Crataegus bullatus Nutrition 0.000 claims 1
- 235000017181 Crataegus chrysocarpa Nutrition 0.000 claims 1
- 235000009682 Crataegus limnophila Nutrition 0.000 claims 1
- 235000004423 Crataegus monogyna Nutrition 0.000 claims 1
- 240000000171 Crataegus monogyna Species 0.000 claims 1
- 235000002313 Crataegus paludosa Nutrition 0.000 claims 1
- 235000009840 Crataegus x incaedua Nutrition 0.000 claims 1
- 210000002837 heart atrium Anatomy 0.000 claims 1
- 150000003071 polychlorinated biphenyls Chemical class 0.000 description 9
- 238000009835 boiling Methods 0.000 description 8
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 4
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 4
- 229910052793 cadmium Inorganic materials 0.000 description 4
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 4
- 229910052804 chromium Inorganic materials 0.000 description 4
- 239000011651 chromium Substances 0.000 description 4
- 229910052802 copper Inorganic materials 0.000 description 4
- 239000010949 copper Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 229910052725 zinc Inorganic materials 0.000 description 4
- 239000011701 zinc Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- -1 atmospheric residuum Substances 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/22—Separation of effluents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
- C10M175/0041—Working-up used lubricants to recover useful products ; Cleaning by thermal processes by hydrogenation processes
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
Asmocigticn.
F
~I~TOF RECEIP Registered Patent Attorney THE COMMIS1ONER OF PATENTS.
COMMONWEALTH OF AUISTRALIAtj j-37 PATENTS ACT 1952-69 COMPLETE SPECIFICATION
(ORIGINAL)
Class Int. Class Application Number: Lodged: Complete Specification Lodged: Accepted: Published: Pr~ority: 'Related Art: Name of Applicant:
UOP
0 Address of Applicant Actual Inventor: Address for Service: East Algonquin Road, Des United States nf America Plaines, Illinois 60017, TOM N. KALNES and ROBERT B. JAMES, JR.
EDWD. WATERS SONS, 50 QUEEN STREET, MELBOURNE, AUSTRALIA, 3000.
Complete Specification for the invention entitled: TREATING A TEMPERATURE- SENS ITI VE HYDROCARBONACEOUS
WASTE
STREAM CONTAINING A NON-DISTILLABLE COMPONENT The following statement is a full description of this Invention, including the best method of performing It known to us
ST
1Ck "TREATING A TEMPERATURE-SENSITIVE HYDROCARBONACEOUS WASTE STREAM CONTAINING A NON-DISTILLABLE COMPONENT" FIELD OF THE INVENTION The field of art to which this invention pertains is the production of a distillable hydrocarbonaceous product from a temperature-sensitive hydrocarbonaceous waste stream containing a nondistillable component. More specifically, the invention relates to a process using flash vaporization for treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component to produce a distillable hydrocarbonaceous product and a heavy product 15 comprising the non-distillable component while minimizing thermal degradation of the hydrocarbonaceous stream.
BACKGROUND OF THE INVENTION With the advent of recognition of the dangers associated with disposal of waste streams containing hazardous materials, there has been a steadily increasing demand for technology which is capable of treating a temperature-sensitive hydrocarbonaceous waste stream 25 containing a non-distillable component to produce a distilleble hydrocarbonaceous product and a heavy nondistillable product while minimizing thermal degradation of the hydrocarbonaceous feed stream. Such treatment has always been in demand for the preparation and production of various hydrocarbonaceous products but with the increased environmental emphasis for the treatment and recycle of waste hydrocarbonaceous products there is an increased need for improved processes to separate heavy non-distillable components from a distillable hydrocarbonaceous product. For example, during the disposal or recycle of potentially environmentally harmful hydrocarbonaceous waste streams, an important step in the rMe' 2 total solution to the problem is the pretreatment or conditioning of a hydrocarbonaceous stream which facilitates the ultimate resolution to provide product streams which may subsequently be handled in an environmentally acceptable manner. Therefore, those skilled in the art have sought to find feasible techniques to remove heavy non-distillable components from a temperature-sensitive hydrocarbonaceous waste stream to provide a distillable hydrocarbonaceous product. Previous techniques which have been employed include filtration, vacuum wiped film evaporation, solvent extraction, centrifugation, and vacuum distillation.
BRIEF SUMMARY OF THE INVENTION The invention provides an improved process for the production of a distillable hydrocarbonaceous product from a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component by means of contacting the hydrocarbonaceous waste feed stream with a hot hydrogen-rich gaseous stream under j conditions selected to increase the temperature of the feed stream and to flash vaporize at least a portion of the distillable hydrocarbonaceous compounds thereby producing a distillable hydrocarbonaceous product. Important elements of the improved process are the relatively short time that the feed stream is maintained at elevated temperature, the i' avoidance of heating the feed stream via indirect heat exchange and the inhibition of coking reactions provided by the presence of hydrogen.
20 In its broadest aspect the invention provides a process for treating a temperaturesensitive hydrocarbonaceous waste stream containing a non-distillable component to SI' produce a distillable hydrocarbonaceous product and a heavy product comprising said nondistillable component while minimizing thermal degradation of said hydrocarbonaceous waste stream which process comprises the steps of: contacting said waste stream with a hot first hydrogen-rich gaseous stream having a temperature greater than said waste stream in a flash zone at flash conditions thereby increasing the temperature of said waste stream and vaporizing at least a Sportion thereof to provide a vapor stream comprising hydrogen and hydrocarbonaceous compounds and a heavy product stream comprising the non-distillable component; condensing at least a portion of the vapor stream to provide a second hydrogenrich gaseous stream and a liquid stream comprising hydrocarbonaceous compounds; and recovering a distillable hydrocarbonaceous product from the liquid stream.
1 1
**A
I A second embodiment of the invention may be characterized as a process for treating a temperature-sensitive hydrocarbonaceous waste stream containing a nondistillable component to produce a distillable hydrocarbonaceous product and a heavy product comprising said non-distillable component while minimizing thermal degradation of said hydrocarbonaceous waste stream which process comprises the steps of: contacting said hydrocarbonaceous waste stream with a hot first hydrogen-rich gaseous stream having a temperature greater than said hydrocarbonaceous waste stream in a flash zone at flash conditions thereby increasing the temperature of said 1 0 hydrocarbonaceous waste stream and vaporizing at least a portion thereof to provide a vapor stream comprising hydrogen and hydrocarbons and a heavy product comprising said non-distillable component; condensing at least a portion of said vapor stream to provide a second hydrogenrich gaseous stream and a liquid stream comprising fuel gas and distillable hydrocarbonaceous compounds; and recovering a distillable hydrocarbonaceous product from said liquid stream heating at least a portion of said hydrogen-rich gaseous stream and passing the resulting heated stream to step as at least a portion of said hot first hydrogen-rich stream.
0**O A third embodiment of the invention may be characterized as a process for 20 treating a temperature-sensititve hydrocarbonaceous waste stream containing a nondistillable component to produce a distillable hydrocarbonaceous product and a heavy product comprising the non-distillable component while minimizing thermal K i 3 degradation of the hydrocarbonaceous stream which process comprises the steps of: contacting the hydrocarbonaceous stream with a hot first hydrogen-rich gaseous stream having a temperature greater than the hydrocarbonaceous stream in a flash zone at flash conditions thereby increasing the temperature of the hydrocarbonaceous stream and vaporizing at least a portion thereof to provide a vapor stream comprising hydrogen and hydrocarbons and a heavy product comprising the non- 10 distillable component; condensing at least a portion of the vapor stream to provide a second hydrogen-rich e. gaseous stream suitable for recycle and a liquid stream V ea* comprising fuel gas and distillable hydrocarbonaceous compounds; and recovering a distillable 15 hydrocarbonaceous product from the liquid stream.
*ftwhe e odiment of the invention may be characterized as a process for treating a temperaturesensitive hydrocarbonaceous waste stream containing a nondistillable component to produce a distillable hydrocarbonaceous product and a heavy product comprising the non-distillable component while minimizing thermal degradation of the hydrocarbonaceous stream which process comprises the steps of: contacting the hydrocarbonaceous waste stream with a hot first hydrogen- S'*i 25 rich gaseous stream having a temperature greater than the hydrocarbonaceous stream in a flash zone at flash conditions thereby increasing the temperature of the hydrocarbonaceous stream and vaporizing at least a portion thereof to provide a first vapor stream comprising hydrogen and hydrocarbons and a heavy product comprising the non-distillable product; condensing at least a portion of the first vapor stream to provide a second hydrogen-rich gaseous stream suitable for recyle and a liquid stream comprising distillable hydrocarbonaceous compounds and dissolved hydrogen; and separating the liquid stream to provide a full gas L .e L 4 stream and a normally liquid distillable hydrocarbonaceous product.
Other embodiments of the present invention encompass further details such as preferred feedstocks and operating conditions, all of which are hereinafter disclosed in the following discussion of each of these facets of the invention.
j BRIEF DESCRIPTION OF THE DRAWING The drawing is a simplified process flow diagram s e of a preferred embodiment of the present invention.
G
0*e DETAILED DESCRIPTION OF THE INVENTION The present invention provides an improved process for the removal of heavy non-distillable components from a temperature-sensitive hydrocarbonaceous stream. A wide variety of temperature-sensitive 20 hydrocarbonaceous streams are to be candidates for feed S'.i streams in accordance with the process of the present invention. Examples of hydrocarbonaceous streams which are suitable for treatment by the process of the present invention are dielectric fluids, hydraulic fluids, heat 25 transfer fluids, used lubricating oil, used cutting oils, used solvents, still bottoms from solvent recycle operations, coal tars, atmospheric residuum, oils contaminated with polychlorinated biphenyls (PCB), pesticide wastes or other hydrocarbonaceous industrial waste. Many of these hydrocarbonaceous streams may contain non-distillable components which include, for example, organometallic compounds, inorganic metallic compounds, finely divided particulate matter and nondistillable hydrocarbonaceous compounds hydrocarbons or hydrocarbonaceous compounds boiling above the maximum boiling point materials that can be recovered in the overhead from a vacuum fractionation column). The present invention is particularly advantageous when the nondistillable components comprise sub-micron particulate matter and the conventional techniques of filtration or centrifugation tend to be highly ineffective.
f Once the temperature-sensitive hydrocarbonaceous feed stream is separated into a distillable hydrocarbonaceous product and a heavy non-distillable product, each of these products may be utilized as 10 recovered or may be subsequently treated or processed by ,,oo any known technique or process. If the feed stream contains metallic compounds such as those that contain metals such as zinc, copper, iron, barium, phosphorus, magnesium, aluminum, lead, mercury, cadmium, cobalt, 15 arsenic, vanadium, chromium, and nickel, these compounds will be isolated in the relatively small volume of recovered non-distillable product which may then be treated for metals recovery or otherwise disposed of as desired. In the event that the feed stream contains distillable hydrocarbonaceous compounds which include sulfur, oxygen, nitrogen, metal or halogen components, the resulting recovered distillable hydrocarbonaceous product may be further processed to remove or convert any such components as desired or required.
25 In accordance with the subject invention, a temperature-sensitive hydrocarbonaceous stream containing a non-distillable component is contacted with a hot hydrogen-rich gaseous stream having a temperature greater than the hydrocarbonaceous stream in a flash zone at flash conditions thereby increasing the temperature of the hydrocarbonaceous stream and vaporizing at least a portion thereof to provide a hydrocarbonaceous vapor stream comprising hydrogen and a heavy non-distillable product.
The hydrogen-rich gaseous stream preferably comprises more than about 80 mole hydrogen and more preferably more than about 90 mole hydrogen. The hydrogen-rich gaseous 6 stream is multi-functional and serves as 1) a heat source used to directly heat the hydrocarbonaceous feed stream to preclude the coke formation that could otherwise occur when using an indirect heating apparatus such as a heater or heat-exchanger, 2) a diluent to reduce the partial pressure of the hydrocarbonaceous compounds, 3) a possible reactant to minimize the formation of hydrocarbonaceous polymers, and 4) a stripping medium. In accordance with the subject invention, the temperature-sensitive 10 hydrocarbonaceous feed stream is preferably maintained at a temperature less than about 482 0 F (250°C) before being introduced into the flash zone in order to prevent or a i* minimize the thermal degradation of the feed stream.
Depending upon the characteristics and composition of the 15 hydrocarbonaceous feed stream, the hot hydrogen-rich gaseous stream is introduced into the flash zone at a temperature greater than the hydrocarbonaceous feed stream and preferably at a temperature from about 200 0 F (93 0 C) to about t200F (649 0
C)
During the contacting, the flash zone is preferably maintained at flash conditions which include a temperature from about 150°F (65 0 C) to about 860°F (460 0 a pressure from about atmospheric to about 2000 psig (13788 kPa gauge), a hydrogen circulation rate of S. 25 about 1000 SCFB (168 normal m 3 /m 3 to about 30,000 SCFB (5056 normal m3/m 3 based on the temperature-sensitive hydrocarbonaceous feed stream and an average residence time of the hydrogen-containing, hydrocarbonaceous vapor stream in the flash zone from about 0.1 seconds to about 50 seconds. A more preferred average residence time of the hydrogen-containing, hydrocarbonaceous vapor stream in the flash zone is from about 1 second to about 10 seconds.
The resulting heavy non-distillable portion of the feed stream is removed from the bottom of the flash zone as required to yield a heavy non-distillable product.
The heavy non-distillable product may contain a relatively 7 small amount of distillable components but since essentially all of non-distillable components contained in the hydrocarbonaceous feed stream are recovered in this product stream, the term "heavy non-distillable product" is nevertheless used for the convenient description of this product stream. The heavy non-distillable product preferably contains an atmospheric distillable component of less than about 10 weight percent and more preferably less than about 5 weight percent. Under certain 10 circumstances with a feed stream not having an appreciable amount of liquid non-distillable components, it is contemplated that an additional liquid may be utilized to flush the heavy non-distillables from the flash zone. An *example of this situation is when the hydrocarbonaceous 15 feed stream comprises a very high percentage of distillable hydrocarbonaceous compounds and relatively small quantities of finely divided particulate matter (solid) and essentially no liquid non-distillable component for use as a carrier for the solids. Such a flush liquid may, for example, be a diesel cut boiling in the range from about 500 0 F (260 0 C) to about 700°F (371 0
C),
a high boiling range vacuum gas oil having a boiling range from about 700 0 F (371 0 C) to about 1000 0 F (538 0 C) or a vacuum tower bottoms stream boiling at a temperature 25 greater than about 1000°F (538°C). The selection of a flush liquid depends upon the composition of the hydrocarbonaceous feed stream and the prevailing flash conditions in the flash separator, and the volume of the V flush liquid is preferably limited to that required for removal of the heavy non-distillable component.
The resulting hydrocarbonaceous vapor stream comprising hydrogen is removed from the flash zone and at least a portion thereof is condensed to provide a second hydrogen-rich gaseous stream and a liquid stream comprising distillable hydrocarbonaceous compounds.
8 In the drawing, one embodiment of the subject invention is illustrated by means of a simplified flow diagram in which such details as pumps, instrumentation, heat-exchange and heat-recovery circuits, compressors and similar hardware have been deleted as being non-essential to an understanding of the techniques involved. The use of such miscellaneous appurtenances are well within the purview of one skilled in the art of hydrocarbon processing techniques. With reference now to the drawing, 10 a waste oil feed stream having a non-distillable component is introduced into the process via conduit 1 and is contacted with a hot gaseous hydrogen-rich recycle stream which is provided via conduit 7 and hereinafter described.
The waste oil and the hydrogen-rich recycle stream is 15 intimately contacted in hot hydrogen flash separator 2. A hydrocarbonaceous vapor stream comprising hydrogen is removed from hot hydrogen flash separator 2 via conduit 3, cooled in heat-exchanger 4 and introduced via conduit 3 into high pressure vapor/liquid separator 5. A heavy nondistillable stream is removed from the bottom of hot hydrogen flash separator 2 via conduit 6 and recovered. A hydrogen-rich gaseous stream is removed from separator via conduit 7, heated to a suitable temperature in heatexchanger 14 and utilized to contact the waste oil feed 25 stream as hereinabove described. Since hydrogen is lost from the process by means of a portion of the hydrogen being dissolved in the exiting liquid hydrocarbon, it is necessary to supplant the lost hydrogen with make-up hydrogen from some suitable external source, a catalytic reforming unit or a hydrogen plant. Make-up hydrogen may be introduced into the system at any convenient and suitable point, and is introduced in the drawing via conduit 8. A liquid hydrocarbonaceous stream containiq hydrogen in solution is removed from high pressure ivapor/liuid separator 5 via conduit 9 and is introduced into low pressure vapor/liquid separator 10. A I EFncaaa~~~ i, gaseous stream comprising hydrogen and any normally gaseous hydrocarbons present is removed from low pressure vapor/liquid separator 10 via conduit 11 and recovered. A normally liquid distillable hydrocarbonaceous product is removed from low pressure vapor/liquid separator 10 via conduit 12 and recovered. In the event that the waste oil feed stream contains water, this water is recovered from low pressure vapor/liquid separator 10 via conduit 13.
The following example is presented for the 10 purpose of further illustrating the process of the present •,go invention, and to indicate the benefits afforded by the utilization thereof in producing a distillable hydrocarbonaceous product while minimizing thermal degradation of the temperature-sensitive hydrocarbonaceous 15 feed stream containing a non-distillable component.
EXAMPLE
A waste lube oil containing fully divided particulate matter and heavy metals having the characteristics presented in Table 1 and contaminated with 1020 ppm by weight of polychlorinated biphenyl (PCB), as Aroclor, was charged at a rate of 100 mass units per hour to a hot hydrogen flash zone. The hot hydrogen was .I 25 introduced into the hot hydrogen flash zone at a rate of 31 mass units per hour.
4 I TABLE 1 WASTE LUBE OIL FEEDSTOCK PROPERTIES (5375-45) Specific Gravity 600F (15 0
C)
Vacuum Distillation Boiling Range, (ASTM D-1160)
IBP
.0 40% 50% 60% 70% .5 Over Bottoms .8827 OF 1 0
C
0 .00. 0 o 00 0*4 a so 0 *0 B. S 5*a
S
0940 9
BOSS
OB a #5a 09 338 516 628 690 730 750 800 831 882 170) (269) (331) (367) (388) (399) (421) (444) (474) 1020 863 416 1 21 Sulfur, weight percent Polychlorinated Biphenyl Concentration, wppm Lead, wppm Zinc, wppm Cadmium, wppm Copper, wppm Chromium, wppm The waste lubo oil was preheated to a temperature of <482oF (<250 0 C) before introduction into the flash zone which temperature precluded any significant detectable thermal degradation. The waste lube oil was intimately contacted in the flash zone with a hot hydrogen-rich gaseous stream having a temperature upon introduction into the flash zone of >748 0 F (>398 0 In addition, the hot hydrogen flash zone was operated at conditions which included a temperature of 748 0 F (398 0 a pressure of 500 psig (3447 kPa gauge), a hydrogen circulation rate of 18000 SCFB (3034 normal m 3 /m 3 and an average residence Im I m
I
IEO=II~E-~--snL-I;I~nsY-rii-~^~_NI---CIP I I
I
11 time of the vapor stream of 5 seconds. A hydrocarbonaceous vapor stream comprising hydrogen was recovered from the flash separation zone, cooled to 77 F and introduced into a high pressure separator. An overhead gas stream containing 100% hydrogen in an amount of 31 mass units per hour was recovered from the high pressure separator and found to be suitable for recycle to i the flash zone. A liquid stream was removed from the high Ipressure separator and introduced into a low pressure S. 10 separator to provide a fuel gas stream containing hydrogen S and a small amount of light hydrocarbons and a liquid bottoms stream in the amount of 88 mass units per hour having the characteristics presented in Table 3.
S *o 04 S!i i 12 TABLE 3 ANALYSIS OF LOW PRESSURE SEPARATOR BOTTOMS
STREAM
Specific Gravity 60oF (15 0 C) 0.866 Vacuum Distillation Boiling Range, o F C C (ASTM D-1160) IBP 225 (107) 433 (223) 538 (280) 10 30% 633 (334) 702 (372) 50% 741 (394) 60% 770 (410) 70% 801 (427) 15 80% 837 (447) 896 (479) 943 (506) EP 982 (527) Over 97 Bottoms 3 Sulfur, weight percent 0.31 Polychlorinated Biphenyl Concentration, wppm 1143 *199 I 25 Lead, wppm 3.7 Zinc, wppm Cadmium, wppm <0.04 Copper, wppm 0.1 Chromium, wppm 0.6 A non-distillable liquid stream was recovered from the bottom of the flash separation zone in an amount of 12 mass units per hour and having the characteristics presented in Table 4.
T AM 13 TABLE 4 ANALYSIS OF NON-DISTILLABLE STREAM Specific Gravity 60°F (15°C) 0.9 Polychlorinated Biphenyl Concentration, wppm 110 In summary, this example demonstrated that a waste lube oil having a non-distillable component and containing 1020 wppm of polychlorinated biphenyl and 1306 wppm heavy metals lead, zinc, cadmium, copper and chromium was separated into a distillable hydrocarbonaceous stream containing 98.6 weight percent of 6* the polychlorinated biphenyl contained in the waste lube oil and a heavy stream comprising essentially all of the non-distillable component of the waste lube oil including i 15 99.5 weight percent of the heavy metals. The analysis of the overhead gas stream showed that the temperaturesensitive waste lube oil did not experience any significant amounts of undesirable thermal cracking with i i I the accompanying formation of normally gaseous hydrocarbonaceous compounds.
I 4t*
Claims (4)
1. A process for treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component to produce a distillable hydrocarbonaceous product and a heavy product comprising said non-distillable component while minimizing thermal degradation of said hydrocarbonaceous stream which process comprises the steps of: contacting said waste stream with a hot first hydrogen-rich gaseous stream having a temperature greater than said waste stream in a flash zone at flash conditions thereby increasing the temperature of said waste stream and vaporizing at least a portion thereof to provide vapor stream comprising hydrogen and hydrocarbonaceous compounds and a heavy product stream comprising the non-distillable component; condensing at least a portion of the vapor stream to provide a second hydrogen- rich gaseous stream and a liquid stream comprising hydrocarbonaceous compounds; and recovering a distillable hydrocarbonaceous product from the liquid stream. A process for treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component to produce a distillable hydrocarbonaceous product and a heavy product comprising said non-distillable component while minimizing thermal degradation of said hydrocarbonaceous waste stream which process comprises the steps of: contacting said hydrocarbonaceous waste stream with a hot first hydrogen-rich gaseous stream having a temperature greater than said hydrocarbonaceous waste stream in a flash zone at flash conditions thereby increasing the temperature of said hydrocarbonaceous waste stream and vaporizing at least a portion thereof to provide a vapor stream comprising hydrogen and hydrocarbons and a heavy product comprising said non-distillable component; condensing at least a portion of said vapor stream to provide a second hydrogen- rich gaseous stream and a liquid stream comprising fuel gas and distillable hydrocarbonaceous compounds; and recovering a distillable hydrocarbonaceous product from said liquid stream heating at least a portion of said hydrogen-rich gaseous stream and passing the resulting heated stream to step as at least a portion of said hot first hydrogen-rich stream.
II, s Z/ .4
3. The process of claim 1 or claim 2 wherein said temperature-sensitive hydrocarbonaceous waste stream comprises dielectric fluids, hydraulic fluids, heat transfer fluids, used lubricating oil, used cutting oils, used solvents, still bottoms from solvent recycle operations, coal tars, atmospheric residuum, PCB-contaminated oils, pesticide wastes or other hydrocarbonaceous industrial waste, and said non-distillable component comprises organometallic compounds, inorganic metallic compounds, finely divided particulate matter or non-distillable hydrocarbonaceous compounds.
4. The process of claim 1 or claim 2 wherein said temperature-sensitive hydrocarbonaceous waste stream is introduced into said flash zone at a temperature less than 482 0 F (2500C), and wherein the temperature of said hot first hydrogen-rich stream is from 200°F (93°C) to 1200°F (6490C). The process of claim 1 or claim 2 wherein said flash conditions include a temperature from 150 0 F (650C) to 860 0 F (460 0 a pressure from atmospheric to 2000 psig (13788 kPa gauge), a hydrogen circulation rate of 1000 SCFB (168 normal m 3 /m 3 to 30,000 SCFB (5056 normal m 3 /m 3 based on said temperature-sensitive r hydrocarbonaceous waste stream, and an average residence time of said vapor stream in I said flash zone from 0.1 seconds to 50 seconds. S* I JATED this 3rd day of June, 1991. uoP WATERMARK PATENT TRADEMARK ATTORNEYS I THE ATRIUM 290 BURWOOD ROAD HAWTHORN VICTORIA 3122 JL AUSTRALIA I i*i LCG/RHB/ML 00 9* 4 909 9
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US7680487A | 1987-07-23 | 1987-07-23 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU3070089A AU3070089A (en) | 1990-08-30 |
| AU613713B2 true AU613713B2 (en) | 1991-08-08 |
Family
ID=22134287
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU30700/89A Ceased AU613713B2 (en) | 1987-07-23 | 1989-02-24 | Treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP0301758B1 (en) |
| AU (1) | AU613713B2 (en) |
| DE (1) | DE3861646D1 (en) |
| ES (1) | ES2020603B3 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0306164B1 (en) * | 1987-08-13 | 1992-10-14 | Uop | Hydrogenating a temperature sensitive hydrocarbonaceous waste stream |
| EP1296714B1 (en) | 2000-06-22 | 2009-08-26 | University Of Iowa Research Foundation | Combination of CpG and antibodies directed against CD19,CD20, CD22 or CD40 for the treatment or prevention of cancer. |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4265773A (en) * | 1979-06-28 | 1981-05-05 | Chevron Research Company | Process of preparing molybdenum complexes, the complexes so-produced and lubricants containing same |
| EP0149862A1 (en) * | 1983-11-23 | 1985-07-31 | Kinetics Technology International B.V. | Process for re-refining spent lubeoils |
| EP0228651A1 (en) * | 1986-01-02 | 1987-07-15 | RWE-Entsorgung Aktiengesellschaft | Process for obtaining high-grade lubricants from spent oils |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1182377B (en) * | 1962-01-09 | 1964-11-26 | Hans Joachim Kettlitz Mineralo | Process for the regeneration of used oils |
| US4151072A (en) * | 1977-05-16 | 1979-04-24 | Phillips Petroleum Company | Reclaiming used lubricating oils |
| US4265733A (en) * | 1979-11-01 | 1981-05-05 | Phillips Petroleum Company | De-ashing lubricating oils |
-
1988
- 1988-07-20 ES ES88306665T patent/ES2020603B3/en not_active Expired - Lifetime
- 1988-07-20 DE DE8888306665T patent/DE3861646D1/en not_active Expired - Fee Related
- 1988-07-20 EP EP88306665A patent/EP0301758B1/en not_active Expired - Lifetime
-
1989
- 1989-02-24 AU AU30700/89A patent/AU613713B2/en not_active Ceased
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4265773A (en) * | 1979-06-28 | 1981-05-05 | Chevron Research Company | Process of preparing molybdenum complexes, the complexes so-produced and lubricants containing same |
| EP0149862A1 (en) * | 1983-11-23 | 1985-07-31 | Kinetics Technology International B.V. | Process for re-refining spent lubeoils |
| EP0228651A1 (en) * | 1986-01-02 | 1987-07-15 | RWE-Entsorgung Aktiengesellschaft | Process for obtaining high-grade lubricants from spent oils |
Also Published As
| Publication number | Publication date |
|---|---|
| AU3070089A (en) | 1990-08-30 |
| EP0301758B1 (en) | 1991-01-23 |
| ES2020603B3 (en) | 1991-08-16 |
| EP0301758A1 (en) | 1989-02-01 |
| DE3861646D1 (en) | 1991-02-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0390985B1 (en) | Treating a temperature-sensitive hydrocarbonaceaous stream | |
| US5843384A (en) | Plant for purifying spent oil | |
| US5013424A (en) | Process for the simultaneous hydrogenation of a first feedstock comprising hydrocarbonaceous compounds and having a non-distillable component and a second feedstock comprising halogenated organic compounds | |
| US5302282A (en) | Integrated process for the production of high quality lube oil blending stock | |
| US5244565A (en) | Integrated process for the production of distillate hydrocarbon | |
| JPS58129094A (en) | Prevention of polymer formation in naphtha fraction | |
| HU213650B (en) | Process to re-refine used oils | |
| EP0360406B1 (en) | Treating a temperature-sensitive hydrocarbonaceous stream containing a non-distillable component | |
| EP1712608B1 (en) | Method for regenerating used oils by demetallization and distillation | |
| US4840721A (en) | Process for treating a temperature-sensitive hydrocarbonaceous stream containing a non-distillable component to produce a hydrogenated distillable hydrocarbonaceous product | |
| US4486299A (en) | Removing NH3 and H2 S from aqueous streams | |
| AU4315299A (en) | Method for obtaining base oil and removing contaminants and additives from used oil products | |
| US4148717A (en) | Demetallization of petroleum feedstocks with zinc chloride and titanium tetrachloride catalysts | |
| AU613713B2 (en) | Treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component | |
| US7241377B2 (en) | Salt bath refining | |
| US5028313A (en) | Process for treating a temperature-sensitive hydrocarbonaceous stream containing a non-distillable component to produce a distillable hydrocarbonaceous product | |
| CA1209512A (en) | Used oil re-refining | |
| AU613714B2 (en) | Treating a temperature-sensitive hydrocarbonaceous waste stream to produce a hydrogenated distillable and reusable hydrocarbonaceous product stream | |
| US5102531A (en) | Process for treating a temperature sensitive hydrocarbonaceous stream containing a non-distillable component to product a distillable hydrocarbonaceous product | |
| US5384037A (en) | Integrated process for the production of distillate hydrocarbon | |
| EP2809746B1 (en) | Process for contacting one or more contaminated hydrocarbons | |
| US4490245A (en) | Process for reclaiming used lubricating oil | |
| EP0344376A1 (en) | Process for converting heavy hydrocarbons to lighter hydrocarbons | |
| JPH0220593A (en) | Conversion of heavy hydrocarbon to lighter hydrocarbon | |
| US5176816A (en) | Process to produce a hydrogenated distillable hydrocarbonaceous product |