Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
  • B01J2/02—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by dividing the liquid material into drops, e.g. by spraying, and solidifying the drops
  • B01J2/04—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by dividing the liquid material into drops, e.g. by spraying, and solidifying the drops in a gaseous medium
• • 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
• • 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
  • F17D1/16—Facilitating the conveyance of liquids or effecting the conveyance of viscous products by modification of their viscosity
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
  • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
  • Y10T137/00—Fluid handling
  • Y10T137/0318—Processes
  • Y10T137/0391—Affecting flow by the addition of material or energy

Definitions

• Frac tionntion is preferably effected by distillation.
• Diluents e.g. low pour point hydrocarbons such as reservoir condensates, can be admixed with the slurry to improve the polyphosphates can be added to increase the waters ability to selectively adhere to the steel pipe and to displace any oil from the surface of the pipe without forming an emulsion.
• Scott et al. in U.S. 3,269,40l teaches facilitating flow of wax-bearing oil in a pipeline by dissolving in the oil, at superatmospheric pressure and while above its pour point, agas, B-gi N 00 flue gas, and hydrocarbons containing less than 3 carbon atoms.
• the gas becomes associated in some way with the wax crystals and prevents the precipitated wax from agglomerating to form strong wax structures.” Also, the gas collects on the surfaces of the wax particles-especially the larger ones-to form films of gas envelopes which isolate the particles from one another and prevents the wax particles from combining.
• solvent liquid cg. water
• the particles can be pumpability thereof.
• aportion e.g. up to 50% by carbon mixtures.
• the hydrocarbon e.g. crude oil, isfirst fractionated into at least two fractions, one fraction is congealed into spherical particles and then slurried with the other fraction'and the slurry transported preferably in a conduit.
• Kells in U.S. 271,080 separates wax from crude oils by pumping the crude oil, egg. in small streams or jets, into the bottom of a tank containing a brine at a temperature sufiiciently low to congeal the'wax. The congealed wax is recovered in the brine.
• Chilton et al. in U.S. 2,821,205 forms a film of water on the interior wall of the pipe to improve the pumpability of viscous oil.
• a light-petroleum or condensed casing-head gas can be mixed with the crude 'oil toreduce the viscosity.
• Agcnts such as phosphatesand above the scasonably ambient temperature of the transcoated with finely divided coating solids such as calcium' carbonate, etc. Watanabe teaches that it is known in the artto' disperse waxy particles by molding, prilling, spray drying,v extruding, etc. i Titus in US.
• Tltenoil shale is first comminuted to a size of -325 meshand .then suspended in a solvent such as crude oil, retorted shale oil, or a fraction thereof.
• Crude oils are particularly useful with'this invention and especially those classified as waxy" crude oils.
• wax is defined as the precipitate which forms after one point above the average minimum temperature'of the.
• Examples of average pour points of crude oils particularly useful with this invention include about -10 to about 200 F. and prefer ably about 0' to about 150 F. l
• the hydrocarbon mixture is first fractionated into at least two fractions, an overheads fraction which has a relatively low pour point (also identified as having a density and viscosity at a given temperature lower than the original hydrocarbon mixture) and a bottoms fraction which has a relatively high pour point (also identified as having a density and viscosity at a given temperature above that of the original hydrocarbon mixture).
• The. bottoms fraction can be any portion of the original hydrocarbon r'nixture; e.g., it can be about 1 to about 80% and preferably about 20 to about 70% and more,
• v I 2 'Fractionation can be accomplished at atmospheric pressure, sub or superatmospheric pressure and atlow and high temperatures by processes such as distillation,
• solvent extraction membrane fractionation, crystallization, or any process which separates the hydrocarbon mixture into at least two fractions.
• up to preferably up to 42% and more preferably up to 33% by volume of the equivalent high pour point'frac tion can be cracked (by thermal, hydrogenation, catalytical or combinations thereof) during fractionationxor before'congelation.
• the low pour point fraction should have a pour point at least 1. and preferably at least about 5 F. below the average of the minimum temperature range ofjthle transporting system, e.g. a pipeline or a combinationof. pipe- '45 line and tank battery.
• stantially solid particles having an average diameter of. about 0.05 to about 20 or more mm. (millimeters) and, preferably about 0.1 to about 5 mm. and more preferably about 0.5 to about 3 mm.
• the particles are preferably spherical and can be of substantially. uniform or random diameter sizes.
• Comminution is'accornplished by prilling, extruding, molding, shredding, grinding, andlike methods for dispersing or disintegrating the uncongealed or congealed material. Where-shredding or grinding is used, 'comminution preferably takes place .after-congelation. Congealing as used herein includes solidification,
• the high pour point fraction is preferably about'l to about 150 and more preferably about 10 to about 100 F. above its average con'gelation temperature as it'enters the congelation and comminution steps.
• Prilling can be accomplished by spraying the bottoms fraction, into a prilling tower where the prill comes in contact with gas (e.g.'air, N CO naturalgas, or like gases) and/or water.
• gas e.g.'air, N CO naturalgas, or like gases
• theprill is collected in a water bath at the bottom of the tower.
• Air is the preferred gas and is preferably moved through'the prilling tower, bynatural or forced convection, at velocities sufficient to not exceed the drop or settling rate.
• Temperature of the air, entering the prilling tower is preferably aboutl to about 230 and more preferably about 10 to about 150 below the congealing temperature of the prill.
• Temperature of theair leaving the prilling tower is preferably about 230. below to about 150 above and more preferablyabout below to about 10F. above .the average congealing temperature of the high pour point fraction entering the, prilling tower. Water is pref erably sprayed into the tower alongwith the air, the
• the water be sprayed into the tower in a direction normal to the airflow direction.
• Another method for dispersing the high pour point fraction isby extruding or spraying into water, the fraction preferablyat about 5 to about 100 F. and more preferably isv about to about 220? F. above its average 'congelation temperature.
• the water preferably flows countercurrent to the movement of the introduced high pour point fraction and more preferably the water is in'turbulent flow at the injection point of the high pour point fraction.
• the dispersed high pour pointfraction is lthereafter congealed, by admixing cooler water, e.g. at
• a surfactant can be incorporated into the high pour point fraction: before it is congealed, e.g'. it can be ad- 'mixed withthe fraction before or as it enters the prilling tower. Volume amountsof about 0.0001 to about 20% and preferably about 0.001 to about 10%, and more preferably about 0.01 to about 1% by volume, based on the fraction, are useful.
• the surfactant should have sulficieut oleophilic property to solubilize into or act like it is miscible with the fraction.
• surfactant molecules tend to orient their hydrophilic portion radially at thedroplet surface, Theoretically, this ghappensas the droplets of'wax are formed, imparting a more hydrophilic property to the droplet.
• Sorbitan monolaurate is an example of a useful surfactant.
• the surfactant is a petroleum sulfonate preferably having a monovalent cation, e.g.' Na+, and preferably having an-average equivalent weight of about 200 to about 600 and more preferably about 250 to about 500 and most preferably about 350to' about 420.
• the temperature I of the low pour point fraction isap'referably about 30 below ,to' about 30,above'an'd more preferablyabout 20 below to about 20 above the minimum, seasonably ambient temperature of the transportation system. Also, the
• temperatureof thelow pour point fraction during slurrying should be below and preferably at,least about 5 F.
• a liquid diluent such as straight] run gasoline, reservoir condensate,'-or like hydrocarbon, can be admixed with the low pour point fraction either before or after the: slurrying operation-any diluent which is miscible with the low pour pointfraction'and which preferably. has a pour ticles can be coatedwith a solid material. Such inhibits agglomeration of the particles and may permit higher slurry temperatures during transportation. Examples of coatings include those disclosed in US. 3,468,986 to Watanabe.
• the coating can be applied as a spray, either hydrous or anhydrous, or as an aqueous bath containing the solidmaterial.
• useful coating materials include inorganic and organic salts of the metals of Group II, III, IV-A, V, VI, VII, and VIII of the Periodic Table;
• the slurry is pumped through feet of as" p pe in series with 8' of A" tubing at a rate of about 3.7-8.0 g.p.m. (gallons per minute). During pumping, the term pcrature never exceeds 74 F. t v
• the slurry After pumping, the slurry is examined and it appears the beads are not substantially sheared and are not in solution with the overheads fraction.
• EXAMPLE II overheads temperature of 500 F. at the end point and and other aluminum silicates, limestone, etc. Calcium carbonnie is a preferred coating material.
• a gas miscible with the low pour point fraction but preferably immiscible with the congealed fraction can be admixed with the slurry to reduce the viscosity thereof.
• the gas may be liquid at the temperature and pressure of the transportation system.
• miscible gases include CO lower hydrocarbons containing less than 4 carbon atoms, etc.
• the miscible gas can be injected into the slurry under conditions such that the gas is present in concentrations greater than that at atmospheric conditions.
• the mixture is saturated with CO, at superatmospheric pressures.
• the slurry can be transported in bulk, e.g. tank car, tank truck, tank trailer, tank, barge, tanker or like means, but is preferably transported in a conduit, such as a pipeline. or course, the conduit or pipeline system will have tank batteries, i.e. collection or holding tanks, associated with it.
• the slurry can be transported under laminar, transitional (e.g. ReyncldsNumber range of about 2000 to about 4000) or turbulent flow conditions inthe conduit.
• Turbulent flow conditions may be preferred where it is desired to maintain thecongealed particlesin a homogeneous dispersed state.
• the slurry is preferably transported in a conduit wherein the average msximum'temperature of the conduit in at least its major initial length is below the solution temperature of the congealed fraction.
• the average maximum temperature oi the conduit is preferably at least about 1 F. below and more'preferably at least about, 5F. below the average solution temperature of the congealed fraction within the slurry-solution temperature as used herein means the temperature at which substantially all of the congealed particles are in solution within the continuous phase of the slurry.
• the average temperatu're of the conduit should not be below the average pour point of the low pour point fraction and preferably is at least about 1 F. and more preferably at least about 5 F. above this pour point- Working examples:
• a waxy crude oil from the Altamont Field in Utahsv Uinta Basin has an average API gravity of about 40? and has an average pour point of about 110 F. This crude tion).
• the final overheads temperature on the distillation column is 266 F. and the final temperature of the bottoms fraction (i.e. high pour point fraction) is 581 F.
• Pour point of the bottoms fraction is 118 F.
• the bottoms fraction is prilled by sprayingit at a temperature of 160 F. into the atmosphere (air at 80 F.) through a a bottoms temperature of about 700 F. at the end point.
• Pressure of the distlllationcolumn is about 632 mm.
• Thebottoms fraction is separated and sent to a prilhng tower.
• Average V 80% by'weig ht. .oil is distilled such that 32% by weight ofthe crude is taken as an overheads fraction (i.e.-low pour point fractemperature of air entering the tower is about F. and the average temperature of air leaving is about F.-- average velocity otthe air is about 2 rib/sec.
• About 200 gab/hr. of water is sprayed (atomized) into the, lower section of the tower to facilitate congelation of the pull.
• the prill tells about 27 feet to the bottom of the prilling tower where it is collected in water maintained at 60-6$ F.
• the average diameter size of the prill is about 0.8- 1.25 mm.
• the aqueous suspension of the prill is separated into water and the prill. Thereafter, the prill is slurried with the overheads fraction at about 40 F. The slurry is transported in a pipeline at. temperatures not exceeding 75 F.
• a processfor transporting a hydrocarbon mixture as a slurry comprising fractionating the hydrocarbon mixture into at least a relatively low pour point fraction and a relatively high p'our pointf fraction, substantially congealing at least a portion of the relatively high pour point fraction to obtain congealed particles and thereafter slurryin'g the congealed particlesin the relatively low pour point fraction at a temperature below about the solution temperature or the congealed particles in the low pour point fraction-and transporting the slurry vin the transportation system.
• the recess oi claim 15 wherein the average diameter at e congealed particles is about 0.1 to about 5 32.
• the process oi claim 15 wherein the congealed particles are. substantially coated with calcium carbonate.
• the process of. elaiml a wherein the concentra tion at the congealed particlesin the slurry is about 10% to about by weight;

Landscapes

• Engineering & Computer Science (AREA)
• Health & Medical Sciences (AREA)
• Public Health (AREA)
• Water Supply & Treatment (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Pipeline Systems (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Priority Applications (31)

Applications Claiming Priority (1)

Publications (1)

Family

ID=23114965

Family Applications (1)

Country Status (30)

Cited By (9)

Family Cites Families (3)

• 1972
  • 1972-09-18 US US00290205A patent/US3804752A/en not_active Expired - Lifetime
• 1973
  • 1973-07-24 CA CA177,169A patent/CA988559A/en not_active Expired
  • 1973-07-25 ZA ZA00735094A patent/ZA735094B/xx unknown
  • 1973-07-28 IN IN1756/CAL/1973A patent/IN140919B/en unknown
  • 1973-07-30 IT IT2729673A patent/IT998303B/it active
  • 1973-08-07 ZM ZM12273A patent/ZM12273A1/xx unknown
  • 1973-08-16 IL IL4300773A patent/IL43007A/xx unknown
  • 1973-08-17 AU AU59360/73A patent/AU474877B2/en not_active Expired
  • 1973-08-22 DE DE2342411A patent/DE2342411C3/de not_active Expired
  • 1973-08-24 GB GB4023073A patent/GB1421803A/en not_active Expired
  • 1973-08-27 FR FR7330935A patent/FR2200476B1/fr not_active Expired
  • 1973-08-29 CH CH1240673A patent/CH574582A5/xx not_active IP Right Cessation
  • 1973-08-30 OA OA55003A patent/OA04550A/xx unknown
  • 1973-09-11 BR BR704273A patent/BR7307042D0/pt unknown
  • 1973-09-12 EG EG36373A patent/EG10902A/xx active
  • 1973-09-14 TR TR1799173A patent/TR17991A/tr unknown
  • 1973-09-14 DD DD17350073A patent/DD106609A5/xx unknown
  • 1973-09-17 SU SU1975878A patent/SU495847A3/ru active
  • 1973-09-17 NO NO362873A patent/NO140241C/no unknown
  • 1973-09-17 SE SE7312624A patent/SE387610B/xx unknown
  • 1973-09-17 CS CS640573A patent/CS183712B2/cs unknown
  • 1973-09-17 BG BG2455273A patent/BG22846A3/xx unknown
  • 1973-09-17 PL PL1973165264A patent/PL84449B1/pl unknown
  • 1973-09-17 HU HUMA002504 patent/HU171302B/hu unknown
  • 1973-09-18 AT AT803473A patent/AT340556B/de not_active IP Right Cessation
  • 1973-09-18 RO RO7610373A patent/RO74156A/ro unknown
  • 1973-09-18 JP JP10461073A patent/JPS534644B2/ja not_active Expired
  • 1973-09-18 NL NL7312843A patent/NL157705B/xx not_active IP Right Cessation
• 1975
  • 1975-01-23 BE BE152628A patent/BE824685Q/xx active
• 1977
  • 1977-12-30 MY MY41/77A patent/MY7700041A/xx unknown

Also Published As

Similar Documents

Legal Events