US3900041A - Modification of particle hardness in waxy crude oil slurries - Google Patents

Modification of particle hardness in waxy crude oil slurries Download PDF

Info

Publication number
US3900041A
US3900041A US468969A US46896974A US3900041A US 3900041 A US3900041 A US 3900041A US 468969 A US468969 A US 468969A US 46896974 A US46896974 A US 46896974A US 3900041 A US3900041 A US 3900041A
Authority
US
United States
Prior art keywords
wax
fraction
particles
temperature
molten
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
Application number
US468969A
Other languages
English (en)
Inventor
Keith M Kersch
George A Pouska
Dennis E Drayer
Jr James E Tackett
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Marathon Oil Co
Original Assignee
Marathon Oil Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Marathon Oil Co filed Critical Marathon Oil Co
Priority to US468969A priority Critical patent/US3900041A/en
Priority to AR258715A priority patent/AR206428A1/es
Priority to DE19752521235 priority patent/DE2521235A1/de
Priority to FR7514578A priority patent/FR2271500B1/fr
Priority to CH599675A priority patent/CH606389A5/xx
Priority to AT353375A priority patent/AT341950B/de
Priority to AU81026/75A priority patent/AU491602B2/en
Priority to IT23163/75A priority patent/IT1037979B/it
Priority to GB19679/75A priority patent/GB1499150A/en
Priority to BR3669/75D priority patent/BR7502885A/pt
Priority to DD185965A priority patent/DD119302A1/xx
Application granted granted Critical
Publication of US3900041A publication Critical patent/US3900041A/en
Assigned to MARATHON OIL COMPANY, AN OH CORP reassignment MARATHON OIL COMPANY, AN OH CORP ASSIGNS THE ENTIRE INTEREST Assignors: MARATHON PETROLEUM COMPANY
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17D—PIPE-LINE SYSTEMS; PIPE-LINES
    • F17D1/00—Pipe-line systems
    • F17D1/08—Pipe-line systems for liquids or viscous products
    • F17D1/088—Pipe-line systems for liquids or viscous products for solids or suspensions of solids in liquids, e.g. slurries

Definitions

  • ABSTRACT Assignee: Marathon Company Findlay- Previously, waxy crude oils have been fractionated Ohm into a wax fraction and a liquid fraction; the wax frac- [22] Filed; May 3 974 tion formed into particles and slurried into the liquid fraction for transportation in pipelines. Particle stabil- [21] App! 468,969 ity is enhanced by extruding molten wax without substantial crystalline structure into a hot wax immiscible 52 us. c1.
  • Waxy hydrocarbons are fractionated into at least two fractions.
  • the wax fraction is congealed and slurried in the fluid fraction prior to storage or transportation.
  • waxy hydrocarbon mixtures at temperatures below the pour point is very difficult.
  • Many methods have been tried to improve the pumpability of waxy crudes, e.g. heat transfer methods, chemical agents to improve fluidity of the mixture, pour point depressants, diluents, etc., but in general these methods have not been commercially acceptable.
  • the oil has been dispersed in water to form a water-external emulsion and the combination pumped at temperatures below the pour point of the crude oil.
  • Patents representative of the art include:
  • Kells, U.S. Pat. No. 271,080 Wax is separated from crude oil by pumping the crude oil, e.g. in small streams of jets, into the bottom of a tank containing a brine at a temperature sufficiently low to congeal the wax which is recovered in the brine.
  • Scott, et al., U.S. Pat. No. 3,269,601 The pumpability of waxy crudes is improved by dissolving in the oil, at superatmospheric pressure and while above its pour point, gases such as N CO flue gas, and hydrocarbons containing 1-3 carbon atoms. The gas becomes associated in some way with wax crystals and prevents the precipitated wax from agglomerating to form strong wax structures.
  • Watanabe Teaches the formation of spherical particles of wax by melting the wax, then dispersing the spheres in water maintained at a temperature above the solidification temperature of the wax and thereafter cooling the dispersion to solidify the dispersed droplets.
  • the particles can be coated with finely divided solids such as calcium carbonate, etc.
  • Watanabe teaches that it is known in the art to disperse waxy particles by molding, prilling, spray drying, extruding, etc.
  • Waxy crudes are transported by first precipitating the wax in the form of large crystals and thereafter transporting the crude oil containing the crystals.
  • the crystals are formed, e.g., by heating the crude oil to 200F. and then cooling at 1F/min to 60F.
  • Scott, U.S. Pat. No. 3,292,647 teaches transportation of waxy crude oils in a pipeline by shearing the crude at a temperature below its pour point to break down the wax and form a fine dispersion, then introducing a gas, e.g. N CO and natural gas, with the sheared crude to prevent regrowth of the wax crystals and thereafter pumping the composition.
  • a gas e.g. N CO and natural gas
  • U.S. Pat. No. 3,804,752 to Merrill, Jr. et a1 teaches transporting waxy crude oils by fractionating the crude into a high pour point fraction and a low pour point fraction, thereafter slurrying the congealed fraction in the low pour point fraction and pumping the slurry.
  • Applicants have discovered an improved process of transporting waxy hydrocarbon mixtures at seasonably ambient temperatures by fractionating the hydrocarbon mixture into at least a relatively high pour point (wax) fraction and a relatively low pour point (liquid) fraction, introducing the wax fraction as droplets, at a temperature above its melting point, into a hot wax immiscible fluid flowing under laminar flow conditions and flowing cocurrent to the wax fraction, and then into a colder wax immiscible fluid to congeal the particles. Thereafter, the wax particles are separated from the wax immiscible fluid and combined with a liquid hydrocarbon and the resulting slurry transported, preferably in a pipeline.
  • wax relatively high pour point
  • liquid relatively low pour point
  • FIG. 1 shows a typical embodiment of the invention wherein the waxy crude oil enters a distillation column and is separated into a low pour point liquid fraction and a high pour point wax fraction.
  • the molten wax fraction is extruded into the bottom and comes in contact with hot water introduced externally and concentric to the wax through the nozzle.
  • Colder water enters at the top and at the bottom of the column.
  • Water effluent exits at the bottom of the column.
  • the extruded wax congeals into beads before it reaches the top of the column.
  • the beads and some of the water flow out of the column into a separator and the beads are recovered. Thereafter, the beads are combined with the liquid fraction to obtain a transportable slurry.
  • FIG. 2 compares the rate of stabilization of two different slurn'es, one containing prills and the other beads.
  • Waxy hydrocarbon mixtures are mixtures containing wax. Some asphaltenes can be tolerated. Wax is defined as the precipitate formed by dissolving one part of hydrocarbon mixture in ten parts of methyl ethyl ketone at about C. and cooling the mixture to 25C.
  • waxy hydrocarbon mixtures include crude oils, shale oil, tar sand oil, fuel oil, gas oil and other waxy hydrocarbon mixtures and mixtures of two or more of the same type or different hydrocarbon mixtures. Waxy crude oils are particularly useful in this invention. Examples of average pour points of waxy hydrocarbon mixtures particularly useful with this invention include about 10 to about 200F., preferably about 0 to about 150F., and more preferably 75 to about 150F.
  • the hydrocarbon mixture is separated into at least two fractions, a liquid overheads fraction which has a relatively low pour point (referred to as the liquid fraction) and a wax bottoms fraction which has a relatively high pour point (referred to as the wax fraction).
  • the wax fraction is about 1 to about 80% and preferably about 5 to about 70% and more preferably about 10 to about 60% by weight of the original hydrocarbon fraction. Fractions other than the mentioned fractions can be obtained and used for other purposes.
  • Fractionation can be by any process which separates the hydrocarbon mixture into high and low pour point fractions.
  • a part of the wax fraction can be cracked and/or hydrogenated during fractionation or before congelation.
  • the molten wax is preferably about to about 175F. and more preferably about 20 to about 150F. and most preferably about 50 to about 125F. above its melting point (as defined by inverse cooling curve in Characterization of Petroleum Waxes, S. W. Ferris, Chapter 1 of The Proceeding of the ASTM TAPPI Symposium on Petroleum Waxes, Feb. 18-21, 1963, Special Technical Association Publication, STAP, No. 2) as it is dispersed into the column.
  • the temperature of the molten wax be high enough that there is substantially no crystalline structure (including hydrocarbons other than wax) within the molten wax and that maximum durability or integrity of the resulting wax particles is obtained-see Example IV for working example of this preferred temperature range. If the wax fraction has not been cooled to a temperature below the above preferred temperature range since coming from the distillation column, it can be introduced into the column and still obtain durable wax particles.
  • the molten wax is cooled in two stages. First, the wax is dispersed into a hot wax immiscible fluid (coolant) at a temperature which relatively slowly cools the wax to form smooth, substantially round, preferably spherical, shells around the dispersed wax particles. Then, the particles are passed into a colder coolant to substantially complete the solidification of the particles.
  • a hot wax immiscible fluid coolant
  • the coolant should have a temperature above the pour point of the wax, but below the wax temperature'
  • the coolant is at least about 5 to about 150F. and preferably about to about 10F. and more preferably about to about 80F. below the molten wax temperature as it is dispersed into the column.
  • Examples of useful temperature include at least 140F. and preferably about 180F. when the coolant is water.
  • the wax composition and equipment design will control the amount of temperature differential between the molten wax and the coolant. If the coolant is too cold, the extruding wax will be filamentary and if the temperature is too hot, the flow path required to form the spherical shell will be excessive. Agglomeration indicates too little cooling and dimpling indicates excessive coolant-to-wax temperature differential (i.e. differential cooling temperature change is too sudden and too large).
  • the coolant can be introduced through an annular nozzle so that it flows cocurrent and concentric to the wax.
  • the velocity of the wax and coolant is preferably the same and more preferably is within the laminar flow region. Different flow rates can cause turbulence, reduce the size and roughen the surface of the sphere.
  • Single hole nozzles are useful and with this type of nozzle the coolant can flow concentric and cocurrent to the wax by thermal convection currents.
  • the cooled wax particles should have an average diameter of about 0.05 or less to about 20 or more mm. and preferably about 0.1 to about 10 mm. and more preferably about 1 to about 8 mm.
  • the particles are preferably spherical, but can be elongated and can be of either substantially uniform or random diameter sizes.
  • the physical shape and size is affected by the temperature and flow rate of the hot coolant and the molten wax and by introducing the coolant concentric to the nozzle(s).
  • the wax particles then come in contact with a colder wax immiscible fluid (colder coolant) to obtain a substantially solidified particle.
  • the colder Coolant can be about ambient temperature and is preferably about 3 to about F. below the solidification temperature of the wax.
  • the particles follow a sufficiently long flow path to substantially solidify the wax droplets. ltis preferred that the temperature differential between the inlet cold coolant and the outlet fluid in the column be large enough to obtain maximum utilization of the enthalpy of the liquid.
  • Temperature change from the hot coolant to the colder coolant can be controlled by introducing the coolants at one or more places within the tower and by regulating either heat input or output in the column by heat exchangers, etc.
  • the temperature change can be a gradual change or a combination of a gradual change in the bottom of the column and an abrupt. change in the top of the column, or any desired modification thereof.
  • the coolant and/or the colder coolant can be any fluid that is substantially immiscible with the wax at the extruding or dispersing temperature.
  • examples include alcohols, ketones, esters, and other polar or semipolar organic compounds.
  • the coolants are water. Also, it can be a combination of two or more coolants.
  • solidification includes congealing, crystalization and making into a consistency like jelly.
  • the solidified particle has at least a hard veneer on the wax particle.
  • the interior of the particle can be fluid, but is preferably substantially solid.
  • a surfactant can be incorporated into the molten wax. Volume amounts of 0.001 to about 20% and preferably about 0.01 to about 10% and more preferably about 0.1 to about 1%, by volume based on the fraction, are useful.
  • useful surfactants include fatty acids, e.g. containing about 10 to about 20 carbon atoms and preferably the monovalent cationcontaining salts thereof. Sorbitan monolaurate is an example of a useful surfactant.
  • the surfactant is a petroleum sulfonate and more preferably one conetc.
  • the liquid fraction or a liquid hydrocarbon is introduced into the top of the column to physically remove the wax particles.
  • an interface between the coolant and the liquid hydrocarbon is maintained at a point below the elevation in the column at which the particles are removed. The particles tend to accumulate at the interface.
  • the liquid hydrocarbon (this term is defined to include the liquid fraction) should be at least about 5 and more preferably at least about 30 and most preferably at least about 70F. below the solution temperature of the solidified wax particles when the liquid hydrocarbon is slurried with the particles.
  • Solution temperature is defined as that temperature at which a major portion of the particles are in solution of the liquid hydrocarbon.
  • the temperature of the liquid hydrocarbon is such that the resulting slurry temperature is preferably about 5 to about 10F. above and more preferably to about F. above the minimum seasonably ambient temperature of the transportation system. Also, it is preferred that the temperature of the liquid hydrocarbon during slurrying is about 30F. and more preferably about 70F. below the solu-.
  • the liquid hydrocarbon should be at least about 5 and more preferably at least about 30 and most preferably at least about 70F. below the solution temperature of the particles in the liquid hydrocarbon and have a pour point at least 1 and preferably at least 5F. and more preferably at least about 15F. below the average temperature of the transportation system.
  • the temperature of the liquid hydrocarbon be low enough during the slurrying operation to provide a slurry temperature preferably about F. below to about 10F. above and more preferably at about the minimum seasonably ambient temperature of the transportation system.
  • a liquid and/or gaseous diluent such as straight run gasoline, reservoir condensate or light hydrocarbon can be admixed with the liquid hydrocarbon before, during or after the slurrying operation.
  • Any diluent is useful as long as it is miscible with the liquid hydrocarbon, has a pour point below the minimum temperature of the transportation system and does not readily solubilize the wax particles or cause any reaction to substantially increase the solubility of the wax particles in the liquid hydrocarbon.
  • Crude oils can be used as the diluent, but preferably the crude oil has a wax concentration less than about l0%-the wax can be in crystalline form.
  • a gaseous diluent it is preferred that it be dissolved in the slurry at transportation condition to prevent cavitation of pumps.
  • Concentrationof the wax particles in the slurry is preferably about 1 to about 60% or more and preferably about 5 to about 55% and most preferably about 20 to about 45% by weight.
  • the temperature of the slurry during transportation is preferably below the solution temperature of the wax particles at all times.
  • the slurry can stand temperatures higher than the solution temperature of the wax for short periods of time so long as substantial amounts of the wax particles are not reliquefied. But if the temperature does exceed the solution temperature, the slurry can still be effectively transported in a pipeline as long as the temperature does not cycle more than preferably about 3SF. below the highest temperature reached by the slurry during transportation. Also, as long as the temperature is increasing during the pipelining, even above the solution temperature, there is no detrimental effect. However, when the temperature decreases to more than about 10F below the highest transportation temperature, then large pressure drops occur if the particle solution has been substantial.
  • Transportation system includes tanks, tank trucks, tank trailers, tank barges, ships or tankers, pipelines, pipelines and tank batteries, or holding tanks and combinations thereof.
  • the transportation system is a pipeline or a pipeline plus tanks.
  • the slurry can be transported under laminar flow, transitional flow (e.g. Reynolds Nos. about 2000 to about 4000) or turbulent flow conditions in the conduit. It is preferably transported under laminar and transitional flow conditionsturbulency within the pipeline tends to break apart and solubilize the wax particles in the liquid hydrocarbon of the slurry.
  • transitional flow e.g. Reynolds Nos. about 2000 to about 4000
  • turbulent flow conditions in the conduit. It is preferably transported under laminar and transitional flow conditionsturbulency within the pipeline tends to break apart and solubilize the wax particles in the liquid hydrocarbon of the slurry.
  • the slurry is preferably transported in a conduit wherein the average maximum temperature of the conduit is below the average solution temperature of the wax particle in the liquid hydrocarbon.
  • the average temperature of the conduit is desirably not below the average pour point of the liquid hydrocarbon and preferably is at least about 20F. and more preferably at least about 25F. above this pour point.
  • a gas soluble in the liquid hydrocarbon can be added to the slurry to facilitate pumpability.
  • gases include CO hydrocarbons containing less than about 3 carbon atoms, N flue gases and like gases.
  • the gas is immiscible with the wax particles.
  • the wax particles can also be coated with solid materials or other agents to inhibit agglomeration and to permit higher slurry transportation temperatures.
  • a waxy crude oil (having an average pour point 1 15F.) is distilled into a liquid fraction (average pour point 17F.) and a wax fraction (average pour point F., melting point F.).
  • the wax fraction is stored at ambient temperature and thereafter is heated 7 to and maintained at 200F. for at least 2 hours; it is then fed at a rate of 300 lbs/hrinto a manifoldcontaining 37 nozzles positioned in the bottom of-an 8 in. dia. X 7 feet water column.
  • the nozzles are" spaced /2 inch apart. Each nozzle is 1.375 inches long with a 0.08 inch diameter hole drilled lengthwise 1.275 inches deep. Wax is fed into the side of the nozzle from the manifold.
  • Hot water is flowed cocurrent to the wax and concentric to the nozzles at a rate of 0.75 gal/min and at an initial temperature of 180F.
  • Cold water at 45F. is introduced peripherally into the top of the column and flows to the bottom of the column by free convection.
  • Water may be drawn off the bottom of the column if additional cooling is needed.
  • the cocurrent water and beads exiting the top of the column have an average temperature of 80F.
  • the average diameter of the congealed beads is about 3/16 inch.
  • a slurry is obtained by stirring sufficient amounts of the beads into a holding tank with the liquid fraction to obtain a bead concentration of 27.5%.
  • the slurry is then pumped through a 6 inches diameter pipeline at 38F. without difficulty.
  • Example I The wax of Example I that has been stored at ambient temperature is prilled by introducing molten wax through 19 nozzles (inside diameter 0.035 inch) at 200F. and at a rate of 190 lbs/hr into a prilling tower.
  • the prills fall approximately 25 feet through a 2 foot inside diameter prilling tower and are cooled with a fine mist of water.
  • the prills are collected at the bottom of the prilling tower and separated from the water. Thereafter, a slurry is obtained by combining the prills with the liquid fraction from Example I at a concentration of 27.5%.
  • Disintegration 7r Disintegration after agitation after agitation Sample (Two Hours) (Three Hours) Slurry l (Beads) 74 82 Slurry 2 (Prills) 89 92 EXAMPLE IV TABLE 2 7c Disintegration after agitation (Three Hours) 7: Disintegration after agitation Sample (Two Hours) ,Slurry containing beads obtained from Example IV 44. 6]
  • FIG. 2 illustrates the data obtained by this example. These data are obtained in a pipeline having an inside diameter of 2 inches and a length of feet and the slurriesare run therethrough at the same temperature. These data show that the prill slurry and the bead slurry stabilize to the same pressure drop, but that the bead slurry stabilizes at a slower rate than does the prill slurry. This is significant in terms of slurry pumping horsepower requirement. 1
  • a process for transporting waxy petroleum crudes by fractionating the crude into at least a wax fraction and a liquid fraction, forming substantially round particles of wax, slurrying the wax particles in a liquid hydrocarbon comprised of the liquid fraction and transporting the slurry, the steps comprising introducing molten wax having no substantial crystalline structure into a hot, wax immiscible fluid flowing cocurrent to the introduction of the molten wax and at flow rates sufficient to form substantially round particles having a substantially smooth outer shell and thereafter introducing the wax particles into a colder wax immiscible fluid at a sufficiently low temperature to substantially solidify the wax particles.
  • waxy hydrocarbon mixture has an average pour point within the range of about 75 to about 150F.

Landscapes

  • Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Public Health (AREA)
  • Water Supply & Treatment (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US468969A 1974-05-13 1974-05-13 Modification of particle hardness in waxy crude oil slurries Expired - Lifetime US3900041A (en)

Priority Applications (11)

Application Number Priority Date Filing Date Title
US468969A US3900041A (en) 1974-05-13 1974-05-13 Modification of particle hardness in waxy crude oil slurries
AR258715A AR206428A1 (es) 1974-05-13 1975-01-01 Proceso para el transporte de crudos de petroleo parafinosos por fraccionamiento del crudo en por lo menos una fraccion de parafina y una fraccion liuqida
BR3669/75D BR7502885A (pt) 1974-05-13 1975-05-09 Processo de modificacao da dureza de particulas em suspensoes de oleo cru parafinico para o transporte de petroleo parafinico
CH599675A CH606389A5 (de) 1974-05-13 1975-05-09
AT353375A AT341950B (de) 1974-05-13 1975-05-09 Verfahren zur aufbereitung von wachshaltigen roholen
AU81026/75A AU491602B2 (en) 1974-05-13 1975-05-09 A process for preparing a waxy petroleum crude oil for transportation
DE19752521235 DE2521235A1 (de) 1974-05-13 1975-05-09 Verfahren zum transport wachsartiger rohoele
GB19679/75A GB1499150A (en) 1974-05-13 1975-05-09 Process for the production of pumpable slurries from waxy hydrocarbon mixtures
FR7514578A FR2271500B1 (de) 1974-05-13 1975-05-09
IT23163/75A IT1037979B (it) 1974-05-13 1975-05-09 Modifica di durezza di particelle in sospensioni di petrolio grezzo ceroso
DD185965A DD119302A1 (de) 1974-05-13 1975-05-12

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US468969A US3900041A (en) 1974-05-13 1974-05-13 Modification of particle hardness in waxy crude oil slurries

Publications (1)

Publication Number Publication Date
US3900041A true US3900041A (en) 1975-08-19

Family

ID=23861924

Family Applications (1)

Application Number Title Priority Date Filing Date
US468969A Expired - Lifetime US3900041A (en) 1974-05-13 1974-05-13 Modification of particle hardness in waxy crude oil slurries

Country Status (10)

Country Link
US (1) US3900041A (de)
AR (1) AR206428A1 (de)
AT (1) AT341950B (de)
BR (1) BR7502885A (de)
CH (1) CH606389A5 (de)
DD (1) DD119302A1 (de)
DE (1) DE2521235A1 (de)
FR (1) FR2271500B1 (de)
GB (1) GB1499150A (de)
IT (1) IT1037979B (de)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4050742A (en) * 1976-11-04 1977-09-27 Marathon Oil Company Transporting heavy fuel oil as a slurry
US5039258A (en) * 1988-12-02 1991-08-13 Energiagazdalkodasi Intezet Hydraulic transporter with united streaming reversing means
US5254177A (en) * 1992-02-10 1993-10-19 Paraffin Solutions, Inc. Method and system for disposing of contaminated paraffin wax in an ecologically acceptable manner
US6313361B1 (en) 1996-02-13 2001-11-06 Marathon Oil Company Formation of a stable wax slurry from a Fischer-Tropsch reactor effluent
WO2008056250A2 (en) * 2006-11-09 2008-05-15 Vetco Gray Scandinavia As Sub-cooled hydrocarbon production method and system including maceration of precipitates
US20100012325A1 (en) * 2008-07-17 2010-01-21 Vetco Gray Scandinavia As System and method for sub-cooling hydrocarbon production fluid for transport
US10190062B2 (en) 2015-07-02 2019-01-29 Cenovus Energy Inc. Bitumen processing and transport
CN118070612A (zh) * 2024-03-13 2024-05-24 东北石油大学 基于cfd-dem模型的含蜡原油细观尺度力链网络结构表征方法

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3468986A (en) * 1966-11-15 1969-09-23 David J Watanabe Method for producing a solid particulate material
US3804752A (en) * 1972-09-18 1974-04-16 Marathon Oil Co Transporting hydrocarbon mixtures as a slurry

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3468986A (en) * 1966-11-15 1969-09-23 David J Watanabe Method for producing a solid particulate material
US3804752A (en) * 1972-09-18 1974-04-16 Marathon Oil Co Transporting hydrocarbon mixtures as a slurry

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4050742A (en) * 1976-11-04 1977-09-27 Marathon Oil Company Transporting heavy fuel oil as a slurry
US5039258A (en) * 1988-12-02 1991-08-13 Energiagazdalkodasi Intezet Hydraulic transporter with united streaming reversing means
US5254177A (en) * 1992-02-10 1993-10-19 Paraffin Solutions, Inc. Method and system for disposing of contaminated paraffin wax in an ecologically acceptable manner
US6313361B1 (en) 1996-02-13 2001-11-06 Marathon Oil Company Formation of a stable wax slurry from a Fischer-Tropsch reactor effluent
WO2008056250A2 (en) * 2006-11-09 2008-05-15 Vetco Gray Scandinavia As Sub-cooled hydrocarbon production method and system including maceration of precipitates
WO2008056250A3 (en) * 2006-11-09 2008-07-03 Vetcogray Scandinavia As Sub-cooled hydrocarbon production method and system including maceration of precipitates
GB2456954A (en) * 2006-11-09 2009-08-05 Vetco Gray Scandinavia As Sub-cooled hydrocarbon production method and system including maceration of precipitates
US20100012325A1 (en) * 2008-07-17 2010-01-21 Vetco Gray Scandinavia As System and method for sub-cooling hydrocarbon production fluid for transport
US8256519B2 (en) 2008-07-17 2012-09-04 John Daniel Friedemann System and method for sub-cooling hydrocarbon production fluid for transport
US10190062B2 (en) 2015-07-02 2019-01-29 Cenovus Energy Inc. Bitumen processing and transport
US10793786B2 (en) 2015-07-02 2020-10-06 Cenovus Energy Inc. Bitumen processing and transport
CN118070612A (zh) * 2024-03-13 2024-05-24 东北石油大学 基于cfd-dem模型的含蜡原油细观尺度力链网络结构表征方法

Also Published As

Publication number Publication date
ATA353375A (de) 1977-06-15
FR2271500B1 (de) 1978-02-03
CH606389A5 (de) 1978-10-31
AU8102675A (en) 1976-11-11
AT341950B (de) 1978-03-10
BR7502885A (pt) 1976-03-23
AR206428A1 (es) 1976-07-23
DE2521235A1 (de) 1975-11-27
FR2271500A1 (de) 1975-12-12
GB1499150A (en) 1978-01-25
IT1037979B (it) 1979-11-20
DD119302A1 (de) 1976-04-12

Similar Documents

Publication Publication Date Title
US5244937A (en) Stable nonagglomerating aqueous suspensions of oil soluble polymeric friction reducers
CA1273261A (en) Preparation of emulsions
US4725287A (en) Preparation of stable crude oil transport emulsions
US3846279A (en) Method for making and slurrying wax beads
US3910299A (en) Transportation of waxy hydrocarbon mixture as a slurry
US3900041A (en) Modification of particle hardness in waxy crude oil slurries
EA001538B1 (ru) Неводные суспензии, снижающие сопротивление течению углеводородов в трубопроводах
US3006354A (en) Method for transporting liquids through pipelines
WO2007037799A1 (en) Stabilized polymer drag reducing agent slurries
US3900391A (en) Method of making a pumpable slurry from waxy crude oil
CA1279280C (en) Choke cooling waxy oil
US3880177A (en) Method for transporting waxy hydrocarbon mixtures
US4050742A (en) Transporting heavy fuel oil as a slurry
US4013544A (en) Method for making and slurrying wax beads
US3853356A (en) Method of pumping waxy crude oil
US3804752A (en) Transporting hydrocarbon mixtures as a slurry
CA1279281C (en) Turbine cooling waxy oil
USRE30281E (en) Transportation of waxy hydrocarbon mixture as a slurry
US3735770A (en) Method for increasing the mobility of waxy crude oils
CA1047073A (en) Process for reducing the settling rate of comminuted porous solids in a water-solids slurry
CA1046443A (en) Preventing agglomeration of particles dispersed in hydrocarbon
Iqbal et al. Emulsion Solidification: Influence of the Droplet Size of the Water‐in‐Oil Emulsion on the Generated Particle Size
CA1163785A (en) In-line slush making process
CA1041142A (en) Method of transporting waxy crude oils
US2968066A (en) Formation of solid beads by congelation of suspended liquid droplets

Legal Events

Date Code Title Description
AS Assignment

Owner name: MARATHON OIL COMPANY, AN OH CORP

Free format text: ASSIGNS THE ENTIRE INTEREST IN ALL PATENTS AS OF JULY 10,1982 EXCEPT PATENT NOS. 3,783,944 AND 4,260,291. ASSIGNOR ASSIGNS A FIFTY PERCENT INTEREST IN SAID TWO PATENTS AS OF JULY 10,1982;ASSIGNOR:MARATHON PETROLEUM COMPANY;REEL/FRAME:004172/0421

Effective date: 19830420