WO2008057232A2 - Procédé pour préparer des produits contenant un sel de phosphate - Google Patents

Procédé pour préparer des produits contenant un sel de phosphate Download PDF

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Publication number
WO2008057232A2
WO2008057232A2 PCT/US2007/022598 US2007022598W WO2008057232A2 WO 2008057232 A2 WO2008057232 A2 WO 2008057232A2 US 2007022598 W US2007022598 W US 2007022598W WO 2008057232 A2 WO2008057232 A2 WO 2008057232A2
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Prior art keywords
water
particles
value
predetermined
mixture
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PCT/US2007/022598
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English (en)
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WO2008057232A3 (fr
Inventor
Dustin K. James
Edward C. Jr. Baxter
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Envirofuels, Llc
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Publication of WO2008057232A2 publication Critical patent/WO2008057232A2/fr
Publication of WO2008057232A3 publication Critical patent/WO2008057232A3/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L10/00—Use of additives to fuels or fires for particular purposes
    • C10L10/02—Use of additives to fuels or fires for particular purposes for reducing smoke development
    • 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
    • B01J13/00—Colloid chemistry, e.g. the production of colloidal materials or their solutions, not otherwise provided for; Making microcapsules or microballoons
    • B01J13/0004—Preparation of sols
    • B01J13/0026—Preparation of sols containing a liquid organic phase
    • 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
    • B01J13/00—Colloid chemistry, e.g. the production of colloidal materials or their solutions, not otherwise provided for; Making microcapsules or microballoons
    • B01J13/0086—Preparation of sols by physical processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
    • C10L1/328—Oil emulsions containing water or any other hydrophilic phase
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/003—Additives for gaseous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/12—Inorganic compounds
    • C10L1/1233—Inorganic compounds oxygen containing compounds, e.g. oxides, hydroxides, acids and salts thereof
    • C10L1/125—Inorganic compounds oxygen containing compounds, e.g. oxides, hydroxides, acids and salts thereof water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/12—Inorganic compounds
    • C10L1/1266—Inorganic compounds nitrogen containing compounds, (e.g. NH3)
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/12—Inorganic compounds
    • C10L1/1283—Inorganic compounds phosphorus, arsenicum, antimonium containing compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/12—Inorganic compounds
    • C10L1/1291—Silicon and boron containing compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/14—Organic compounds
    • C10L1/16—Hydrocarbons
    • C10L1/1616—Hydrocarbons fractions, e.g. lubricants, solvents, naphta, bitumen, tars, terpentine
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/14—Organic compounds
    • C10L1/18—Organic compounds containing oxygen
    • C10L1/188—Carboxylic acids; metal salts thereof
    • C10L1/1881—Carboxylic acids; metal salts thereof carboxylic group attached to an aliphatic carbon atom
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/14—Organic compounds
    • C10L1/22—Organic compounds containing nitrogen
    • C10L1/222—Organic compounds containing nitrogen containing at least one carbon-to-nitrogen single bond
    • C10L1/2222—(cyclo)aliphatic amines; polyamines (no macromolecular substituent 30C); quaternair ammonium compounds; carbamates

Definitions

  • the present invention relates to improved processes for making phosphate salt containing products.
  • Phosphate salt containing products are useful for, among other uses, creating derivatized >metal surfaces in engine and combustion chambers and as fuel additives for combustion.
  • these phosphate salt containing products could be produced by a batch process.
  • potassium hydroxide, ammonium hydroxide, water and a phosphoric acid/acetic acid mix could be combined in an acid base reaction in a batch reaction vessel to produce an aqueous phosphate salt containing product.
  • Batch processes suffer from a number of disadvantages.
  • batch processes can be difficult to duplicate, with variations from batch to batch occurring due to different feed rates, changing temperature profiles, different feed stocks, different operators, and possible contamination from other processes that are run in the same equipment.
  • large capital expenditures for equipment are typically used to produce products in a batch operation.
  • large batch reactions are more difficult to control, especially in the case of exothermic acid/base reactions such as those that are sometimes used to prepare phosphate salt containing solutions.
  • the phosphate salts contained in the previous compositions are relatively large, e.g., greater than 5,000 microns. As a result, they take time to dissolve in the fuel or otherwise take longer to combust, thereby reducing the efficacy of the phosphate salt products as fuel additives.
  • TABLE 1 illustrates an example of a raw material balance for a batch process to make a phosphate salt containing solution in accordance with the prior art.
  • FIG. 1 illustrates a process flow diagram corresponding to the raw material balance for a batch process shown in TABLE I.
  • the stream numbers shown in the process flow diagram are the same as those shown in the raw material balance.
  • the acid to base ratio of Stream #1 is 1.95.
  • DI H 2 O is deionized water.
  • Nano-sized particles for example, particles with sizes less than about 100 nm in diameter
  • Nano-sized particles in liquids are clear, the solid particles being invisible to the eye.
  • One or more of these needs are addressed by the present inventions.
  • the present invention is directed to a process that satisfies at least one of these needs.
  • the present invention provides a continuous process for producing an oil based phosphate containing product.
  • This first embodiment known as the "dry/exothermic" process, includes mixing a predetermined amount of water, [Y]OH, [Z]OH, and AcOH in a first mixer to create a base stream, wherein [Y] is a cation and [Z] is selected from the group consisting Of NH 4 , NHOH and an amine.
  • This base stream is then mixed with an orthophosphoric acid using a second mixer to create a liquid phosphate salt containing solution, wherein the orthophosphoric acid is selected from the group consisting of [Y]H 2 PO 4 , [Y]HPO 4 , [NH 4 J 2 HPO 4 , and combinations thereof, wherein [Y] is a cation.
  • the liquid phosphate salt containing solution is then passed through a pH analyzer in order to determine the pH of the liquid phosphate salt containing solution.
  • the liquid phosphate salt containing solution's pH is then compared to a predetermined liquid phosphate pH value.
  • the present invention also provides a means for adjusting the pH of the liquid phosphate salt containing solution operable to modify the pH of the liquid phosphate salt containing solution within a preselected range of the predetermined liquid phosphate pH value.
  • the value should be around 7.0, with the range being plus or minus about 1.0, more preferably a value of 7.0 with a range of plus or minus about 0.5, and most preferably a value of 7.1 with a range of plus or minus about 0.1.
  • the liquid phosphate salt containing solution is then passed through a suitable drying and granulating chamber to create a water based vapor stream and a substantially water-free solid phosphoric salt product.
  • the substantially water-free solid phosphoric salt product consists of a plurality of particles.
  • This plurality of particles has a distribution of particle sizes, with a substantial amount of the particles having a diameter smaller than about 100 nanometers.
  • an in-line particle classifier is included so that any large particles (particles that exceed a predetermined size in diameter) can be removed from the process stream and be recycled back into the first mixer.
  • the product from the drying and granulating chamber is then mixed with a base stock hydrocarbon using a high shear mixer to form the final product, which is an oil based phosphate containing product.
  • a base stock hydrocarbon using a high shear mixer to form the final product, which is an oil based phosphate containing product.
  • the process is identical to the “dry/exothermic” process up to and including the pH analyzer.
  • the liquid phosphate salt containing solution is mixed with a base stock hydrocarbon using a wet high shear mixer to form an emulsified water-in-oil mixture.
  • This emulsified mixture is then sent to a drying evaporator, wherein a substantial amount of the water is removed, leaving a substantially water-reduced emulsified mixture.
  • the mixture contains an effective amount of water to promote water of hydration. This is particularly important for the stability of the mixture.
  • the process includes a water content analyzer, which determines the water content of the mixture and also provides a means for adjusting the water content of the mixture.
  • the water content analyzer could be in communication with devices that could either alter the flow rate of the inlet stream of the drying evaporator, the residence time of the mixture within the evaporator, or the temperature of the evaporator.
  • the substantially water-reduced emulsified mixture then enters a wet grinder, wherein the suspended phosphate particles are grounded into preferably nanoparticles that are also suspended in the mixture, resulting in an oil based phosphate containing product.
  • This oil based phosphate containing product has a plurality of particles, with a substantial amount of the particles having a diameter of less than about 100 nanometers.
  • a wet particle analyzer is included following this step in order to analyze the diameters of the plurality of particles of the oil based phosphate containing product. More preferably, this wet analyzer would be in communication with a means for adjusting the diameters of the plurality of particles of the oil based phosphate containing product. Possible means for adjusting the diameters include altering the flow rate of the inlet to the wet grinder and/or altering the conditions inside the wet grinder. Again, this entire process is conducted in one continuous fashion.
  • the phosphorus content of the liquid phosphate salt containing solution is measured using a first p-count analyzer and compared to a predetermined liquid phosphate phosphorus value. Additionally, a means for adjusting the phosphorus content of the liquid phosphate salt containing solution that is operable to modify the phosphorus content of the liquid phosphate salt containing solution within a preselected range of the predetermined liquid phosphate phosphorus value is provided.
  • an additional embodiment provides for determining the phosphorus content of the oil based phosphate containing product using a second p-count analyzer and comparing the phosphorus content of the oil based phosphate containing product to a predetermined oil based phosphorus value. Additionally, a means for adjusting the phosphorus content of the oil based phosphate containing product operable to modify the phosphorus content of the oil based phosphate containing product within a preselected range of the predetermined oil based phosphorus value is provided.
  • an additional embodiment provides for determining the phosphorus content of the emulsified water-in-oil mixture using a second wet p-count analyzer and comparing the phosphorus content of the emulsified water-in-oil mixture to a predetermined emulsified water-in-oil phosphorus value. Additionally, a means for adjusting the phosphorus content of the emulsified water-in-oil mixture operable to modify the phosphorus content of the emulsified water-in-oil mixture within a preselected range of the predetermined water-in-oil phosphorus value is provided.
  • the present invention includes a method, called a "salts form,” of producing phosphate salt appropriate for dispersal into a base stock hydrocarbon using a continuous process.
  • a salts form of producing phosphate salt appropriate for dispersal into a base stock hydrocarbon using a continuous process.
  • the “exothermic” embodiments have a “wet” and a “dry” version, so too does the “salts form” of the process.
  • the primary difference between the “exothermic” and “salts form” embodiments being the ingredients mixed.
  • water is mixed with various salts, rather than aqueous solutions, to create an intermediate solution.
  • These salts include [Y]H 2 PO 4 , [Y] 2 HPO 4 , [NH 4 ] 2 HPO 4 , [X]C 2 H 3 O 2 , [NR 4 ] 2 HPO 4 , [Y] 2 NH 4 PO 4 , [Y][NH 4 ] 2 PO 4 , and [Z] 2 B 4 O 7 , wherein [Y] is a cation, [X] is a cation and/or NH 4 , R is hydrogen and/or an alkyl group, and [Z] is a cation.
  • the intermediate solution (which is analogous to the liquid phosphate salt containing solution of the exothermic embodiments), passes through a pH analyzer in order to determine the pH of the intermediate solution.
  • the intermediate solution's pH is then compared to a predetermined liquid phosphate pH value.
  • the present invention also provides a means for adjusting the pH of the intermediate solution operable to modify the pH of the intermediate solution within a preselected range of the predetermined liquid phosphate pH value.
  • the process preferably includes utilization of a phosphate salt containing solution containing [Y]H 2 PO 4 , [Y] 2 HPO 4 , and water or other solvents as components of an intermediate solution, where Y is a cation.
  • the cationic portion of the salt components can be any cation, with potassium being a preferred cation.
  • the preferred components would be KH 2 PO 4 , K 2 HPO 4 , and water.
  • the intermediate solution is mixed with a carrier fluid.
  • the carrier fluid is any fluid operable to maintain the salts in at least a partially dispersed state within the carrier fluid. Another group of preferred cations would be the alkali metals of Group IA of the Periodic Table of Elements.
  • orthophosphoric acids include pyrophosphoric acids, which are the condensed analogs of orthophosphoric acid.
  • the PO 4 3' becomes P 2 O 7 2' or other condensed phosphates. Therefore, [Y]H 2 PO 4 , [Y]HPO 4 and [NH 4 J 2 HPO 4 are precursors to pyrophosphoric acids.
  • the use of the pyrophosphoric form is therefore encompassed within the definition of the orthophosphate form, which can be expressed as [Y]H 2 PO 4 , [Y]HPO 4 and [NH 4 J 2 HPO 4 and in similar form.
  • the phosphate salt containing solution is used to create a dry product through the addition of [NH 4 J 2 HPO 4 to the intermediate solution of [Y]H 2 PO 4 , [Y]HPO 4 , and water or other solvent.
  • Yet another embodiment includes the addition of NH 4 C 2 H 3 O 2 where C 2 H 3 O 2 - ion is an acetate group such that the solution contains [Y]H 2 PO 4 , [Y]HPO 4 , [NH 4 J 2 HPO 4 , NH 4 C 2 H 3 O 2 and water.
  • ammonium compounds being defined as those compounds containing NHx groups, the nitrogen in the solution is essentially all in the form of ammonium ions. There is at most a negligible amount of free ammonia.
  • aqueous boron salt containing products may also be utilized.
  • the invention preferably includes a boron-containing salt that includes [Z] 2 B 4 O 7 , wherein Z is a cation.
  • Ammonium is a preferred inorganic cation.
  • Alkali metals are another preferred inorganic cation, more preferably those alkali metals with atomic weights under 50.0. This creates a boron salt appropriate for dispersal into a hydrocarbon base stock hydrocarbon and is encompassed in the term dry product.
  • Another embodiment of the present invention includes making the phosphate salt containing product in a continuous process, drying the continuously made phosphate salt containing product in a continuous process, and continuously suspending the resulting solid in base stock hydrocarbon to make an oil based phosphate containing product.
  • Another embodiment of the present invention includes mixing and grinding the solid forms of the phosphorous salts, i.e., solid K 2 HPO 4 , KH 2 PO 4 , KOAc, K 2 (NH 4 )PO 4 , and K(NH 4 ) 2 PO 4 to a powder in a continuous process, and continuously suspending the powdered product in base stock hydrocarbon.
  • the solid powdered product includes nano- sized phosphate salt particles.
  • Another embodiment of the present invention includes using liquid phosphate salt containing solution in a continuous process to make solid phosphate salt containing product via continuous drying, and subsequently directly using this product as an additive to fuel products.
  • Another embodiment of the present invention includes using liquid salts phosphate salt containing product made in a continuous process to make solid phosphate salt containing product via a continuous drying process, and directly using the resulting solid product as an additive in solid fuel products.
  • Another embodiment of the present invention includes mixing and grinding the solid forms of the phosphate salt containing product phosphorous salts, i.e., solid K 2 HPO 4 , KH 2 PO 4 , KOAc, K 2 (NH 4 )PO 4 , and K(NRj) 2 PO 4 to a powder in a continuous process, and directly using the powdered product as an additive to solid fuel components.
  • the solid powdered product includes nano-sized phosphate salt particles.
  • FIG. 1 is a simplified flow diagram of a process for production of a phosphate salt containing product in accordance with a prior art process
  • FIG. 2 is a simplified flow diagram of the "dry" embodiment of a continuous process for production of an oil based phosphate containing product according to an embodiment of the present invention
  • FIG. 3 is a simplified flow diagram of the "wet" embodiment of a continuous process for production of an oil based phosphate containing product according to an embodiment of the present invention
  • FIG. 4 is a simplified flow diagram of at least a portion of a continuous process for production of a liquid phosphate salt containing solution according to an embodiment of the present invention
  • FIG. 5 is a simplified flow diagram of at least a portion of a continuous process for production of a liquid phosphate salt containing solution in accordance with another embodiment of the present invention.
  • FIG. 6 is a simplified flow diagram of at least a portion of a continuous process for production of a liquid phosphate salt containing solution in accordance with another embodiment of the present invention.
  • FIG. 7 is a simplified flow diagram of a process for drying a phosphate salt containing product to produce a solid product in accordance with an embodiment of the present invention.
  • the liquid phosphate salt containing solution [42] is fed into a liquid phosphate salt containing solution run down tank [60].
  • the liquid phosphate salt containing solution run down tank [60] is provided to minimize the impact of variations upstream.
  • the liquid phosphate salt containing solution [42] moves from the liquid phosphate salt containing solution run down tank [60] and into a drying chamber [70].
  • a drying operation is used to treat the liquid phosphate salt containing solution [42] to produce a substantially water free solid phosphate salt product [74].
  • the process steps as disclosed in the cited literature include atomization of the solution; spray-air contact; drying of droplets/sprays; and separation and recovery of dried product. It is understood that there are many variations in these basic steps that are all intended to be part of this disclosure.
  • Other drying technologies that are intended to be included in this disclosure include drying on inert particles (including coal or other solid fuel particles); impinging stream drying; drying in pulsed fluid beds; superheated steam drying; airless drying; drying in mobilized bed; drying with shock waves; vacuum jet drying system; contact-sorption drying; sonic drying; pulse combustion drying; and heat-pump drying.
  • Some selected techniques for drying and dewatering include the Carver-Greenfield process; drying in a plasma torch; displacement drying; vapor drying; slush drying; atmospheric freeze-drying; radio frequency drying with 50-Ohm technology; radio- frequency-assisted heat pump drying; radio-frequency-vacuum drying; microwave- convective drying; microwave-vacuum drying; filter mat drying; spray-fluid bed-vibrated fluid bed drying; combined filtration and drying; and other hybrid technologies.
  • a preferred method of drying is spray drying.
  • a water based vapor stream [72] is removed, leaving a substantially water free solid phosphate salt product [74].
  • the substantially water free solid phosphate salt product [74] then enters a particle classifier [80], wherein overly large particles [81] are removed and recycled back into the process, preferably at or before the first mixer [30].
  • the large particles [81] can be fed into a grinder (not shown) and then introduced back into the process just after the drying chamber [70].
  • Suitable mechanical processes for the grinding can include, but are not limited to, ball or media mills, cone and gyratory crushers, disk attrition mills, colloid and roll mills, screen mills and granulators, hammer and cage mills, pin and universal mills, impact mills and breakers, jaw crushers, jet and fluid energy mills, roll crushers, disc mills, and vertical rollers and dry pans.
  • the substantially water free solid phosphate salt product [74] now enters a high shear mixer [90] where it is mixed with a base stock hydrocarbon stream [88] to form an oil based phosphate containing product [92].
  • dispersants [86] are also added into the high shear mixer [90].
  • a second p-count analyzer [100] is provided in order to determine that the proper amount of phosphorus is in the oil based phosphate containing product [92].
  • the second p-count analyzer [100] is in communication with control valves that can control the flow rates of the base stock hydrocarbon stream [88] and the substantially water free solid phosphate salt product [74].
  • the liquid phosphate salt containing solution [42] is fed into a liquid phosphate salt containing solution run down tank [60].
  • the liquid phosphate salt containing solution run down tank [60] is provided to minimize the impact of variations upstream.
  • the liquid phosphate salt containing solution [42] moves from the liquid phosphate salt containing solution run down tank [60] and into a wet high shear mixer [71], where it is mixed with a base stock hydrocarbon stream [88] to form an emulsified water-in-oil mixture [73].
  • dispersants [86] are also added into the wet high shear mixer [71].
  • a second wet p-count analyzer [83] is provided in order to determine that the proper amount of phosphorus is in the emulsified water-in-oil mixture [73].
  • the second wet p-count analyzer [83] is in communication with control valves that can control the flow rates of the base stock hydrocarbon stream [88] and the liquid phosphate salt containing solution [42].
  • the emulsified water in oil mixture [73] then enters a drying evaporator [91], where a substantial amount of water is removed in the form of a water based vapor stream [72], leaving a substantially water free emulsified mixture [93] as the product stream of the drying evaporator.
  • a water content analyzer [101] is provided to determine the water content of the substantially water free emulsified mixture [93]. Furthermore in one embodiment, the water content analyzer [101] is in communication with a control valve that controls the flow rate of the emulsified water-in-oil mixture into the drying evaporator [91].
  • substantially water free emulsified mixture [93] Other possible methods for controlling the amount of water in substantially water free emulsified mixture [93] include adjusting the temperature of the drying chamber [70] or adding more water directly into the substantially water free emulsified mixture (not shown).
  • the substantially water free emulsified mixture [93] then travels to a wet run down tank [1 1 1]. From the wet run down tank [1 1 1] the substantially water free emulsified mixture [93] travels into a wet grinder [121] where the particles are ground, preferably into nanoparticles, to form an oil based phosphate containing product [92].
  • a wet particle analyzer [131] is provided to determine the particle sizes of the plurality of particles within the oil based phosphate containing product [92].
  • a means for adjusting the diameters of the plurality of particles is provided by adjusting the flow of the substantially water free emulsified mixture [93].
  • FIGS 4 - 6 are all embodiments of the continuous process to produce the liquid phosphate salt containing solution [42] that is the inlet stream for both FIG. 2 and FIG. 3.
  • a continuous process is advantageously provided for producing a liquid phosphate salt containing solution [42].
  • a pipe [1] is used for the reaction; water [2] and KOH [4] are introduced into the pipe [1] and fed through a first premixer [10].
  • NH 4 OH [6] is added to the pipe [1] and fed through a second premixer [20].
  • AcOH [8] is introduced into the pipe [1] and fed into a first mixer [30], creating a base stream [32].
  • H 3 PO 4 is fed into the pipe [1] and fed into a second mixer [40] to form a liquid phosphate salt containing solution [42].
  • a pH analyzer [50] is provided in order to determine the pH of the liquid phosphate salt containing solution [42], and it is in communication with the feed pumps (not shown) of KOH [4], NH 4 OH [6], and/or AcOH [8], so that the pH of the liquid phosphate salt containing solution [42] is within the range of about 6.0 to about 8.0, more preferably about 6.5 to about 7.5, and most preferably about 7.0 to about 7.2.
  • the phosphorus content of the liquid phosphate salt containing solution [42] is measured using a first p-count analyzer [55].
  • the first p-count analyzer [55] is in communication with the feed pump of the H 3 PO 4 feedstock (not shown), so that it can adjust the flow rate of H 3 PO 4 so that it is within a preselected range of a predetermined liquid phosphate phosphorus value.
  • the liquid phosphate salt containing solution [42] then travels to a liquid phosphate salt containing solution run down tank [60] as shown in FIGS. 2 - 3.
  • All feedstocks are fed into the pipe [1] by feed pumps (not shown) at a rate such that the desired ratios of components are obtained in the final product.
  • the pipe [1] is constructed of a material appropriate for the reaction, and the diameter of the pipe can be varied to allow for the volume of the feedstocks. Scaling up the process can be accomplished, for example, by adding a second parallel process stream or upsizing the equipment to allow for greater flow rates.
  • the continuous process is preferably based on the material balance and process flow diagram for the prior art batch process, as shown in FIG. 1.
  • approximately 935 gallons per hour (gph) of water is pumped into the inlet of the pipe.
  • approximately 569 gph of 45% KOH is added.
  • the KOH is mixed with the flowing water by the use of a first premixer [10], which is preferably an inline, static mixer.
  • a first premixer which is preferably an inline, static mixer.
  • Some amount of heat evolution from the process is caused by the heat of solution of the KOH.
  • Static mixers are well known in the art.
  • approximately 442 gph of 28.4% NH 4 OH is added to the flowing stream.
  • the stream passes through a second premixer [20], which is preferably an inline static mixer. Then approximately 76 gph of acetic acid is added to the stream and the mixture flows through a first mixer [30] to provide further mixing. Then approximately 492 gph of 75% H3PO4 is added to the stream. After passing through a second mixer [40], the pH of the product is monitored at the end of the pipe. An electronic feedback control loop (not shown) is used to control the pumping rate of the KOH, NH 4 OH, and/or acetic acid so that the pH stays within control parameters and no solids precipitate out of the mixture.
  • the diameter of the pipe at each addition point is preferably increased to allow for the added materials.
  • the flow rate is preferably increased at each addition point. Using such a process, approximately 2,513 gph of product can be made.
  • FIG. 5 shows an alternate embodiment of the portion of the continuous process to produce the liquid phosphate salt containing solution [42] of the present invention.
  • the water [2] (approximately 935 gph), KOH [4] (approximately 599 gph), NH 4 OH [6] (approximately 442 gph), and AcOH [8] (approximately 76 gph) are all added continuously using pumps (not shown) into a first mixer [30], which is preferably a stirred mixing vessel, and a continuous basic (pH> 7) takeoff stream is pumped through a pipe into which the acidic H 3 PO 4 [9] (approximately 492 gph) is added via a pump (not shown).
  • the mixture After mixing the acid with the base solution, the mixture passes through a second mixer [40], which is preferably a static mixer, to ensure adequate reaction of the raw materials.
  • the pH of the liquid phosphate salt containing solution [42] is monitored at the end of the pipe and An electronic feedback control loop (not shown) is used to control the pumping rate of the KOH, NH 4 OH, and/or acetic acid so that the pH stays within control parameters and no solids precipitate out of the mixture.
  • the phosphorus content of the liquid phosphate salt containing solution [42] is measured using a first p-count analyzer (not shown).
  • the first p-count analyzer is in communication with the feed pump of the H 3 PO 4 feedstock (not shown), so that it can adjust the flow rate of H 3 PO 4 so that it is within a preselected range of a predetermined liquid phosphate phosphorus value.
  • the liquid phosphate salt containing solution [42] then travels to a liquid phosphate salt containing solution run down tank [60] as shown in FIGS. 2 - 3. About 2,513 gph of liquid phosphate salt containing solution [42] can be made. Heating or cooling means can be added to the mixing vessel or the reaction pipe in order to achieve the desired temperature of the product.
  • FIG. 6 shows an additional embodiment by which a continuous process can be accomplished; for instance, each raw material could be added into sequential tanks that are connected by an overflowing stream.
  • first stirred tank [1 1] Into the first stirred tank [1 1] would be pumped approximately 935 gph of water [2] along with approximately 569 gph of 45% KOH [4]. The first tank [1 1] would overflow into a second stirred tank [21 ], to which approximately 442 gph of 28.4% NH 4 OH [6] is added. The contents of the second stirred tank [21] would then overflow into a third tank stirred tank [31] to which approximately 76 gph of AcOH [8] would be added.
  • the contents of the third stirred tank [31] would overflow into the fourth stirred tank [41] in which 492 gph of 75% H 3 PO 4 [9] would be added.
  • a pH analyzer [50] would be used to monitor the pH of the product overflowing from the last tank and an electronic feedback loop (not shown) could be used to control the addition rate of the KOH, NH 4 OH, and/or acetic acid such that the pH of the product would be within the preferred range of about 6 to about 8, more preferably from about 6.5 to about 7.5, most preferably from about 7.0 to about 7.2. At a pH above or below this range solid precipitants might form at room temperature.
  • the phosphorus content of the liquid phosphate salt containing solution [42] is measured using a first p-count analyzer (not shown).
  • the first p-count analyzer is in communication with the feed pump of the H 3 PO 4 feedstock (not shown), so that it can adjust the flow rate of H 3 PO 4 so that it is within a preselected range of a predetermined liquid phosphate phosphorus value.
  • the liquid phosphate salt containing solution [42] then travels to a liquid phosphate salt containing solution run down tank [60] as shown in FIGS. 2 - 3.
  • the volume of each tank can be adjusted so as to allow the correct residence time for the reaction to take place.
  • Each tank can be individually cooled or heated as the process conditions require.
  • FIG. 7 represents an enlarged view of an embodiment of the drying chamber [70] from FIG. 2.
  • the liquid phosphate salt containing solution [42] to be dried is introduced into the drying chamber [70] that is heated and or under vacuum.
  • the liquid phosphate salt containing solution [42] can be preheated and can be under pressure.
  • the liquid phosphate salt containing solution [42] is introduced into the drying chamber [70] preferably through spray nozzles that convert the liquid phosphate salt containing solution [42] into fine droplets. As the fine liquid droplets enter the drying chamber [70], the liquid portion of the solution is evaporated from the surface of the droplet and a plurality of particles form, producing a substantially water free solid phosphate salt product [74].
  • the water based vapor stream [72] is removed from the top portion of the chamber and the substantially water free solid phosphate salt product [74] collects at the bottom portion of the drying chamber [70].
  • the water based vapor stream [72] removed from the drying chamber [70] can be condensed and recycled back to the front of the operation to provide water of dilution for the substantially water free solid phosphate salt product [74].
  • Other volatile components of the liquid phosphate salt containing solution [42] such as acetic acid or ammonia can also be condensed along with the water, or the vapors can be separated through the use of a distillation column [75] to provide purified components of water [76] and recovered raw materials [77]. Each of these purified components can then be reintroduced into the front end of the process to make phosphate salt containing solution.
  • the liquid phosphate salt containing solution [42] can be heated under pressure in the line leading to the drying chamber [70]. Once introduced via spray into the drying chamber [70] under vacuum, the liquid portion of the liquid phosphate salt containing solution [42] would flash off and be condensed in the condenser while the solid portion of the liquid phosphate salt containing solution [42] would be collected as the substantially water free solid phosphate salt, product [74] at the bottom of the drying chamber.
  • the preferred temperature range of the liquid phosphate salt containing solution [42] for the operation of the drying process is from 25 0 C to 300 0 C; more preferably from 75 0 C to 200 0 C; most preferably from 100 0 C to 19O 0 C.
  • the preferred pressure of the liquid phosphate salt containing solution [42] stream before entering the drying chamber [70] includes any pressure that would maintain the liquid phosphate salt containing solution [42] in its liquid state, depending on the temperature of the stream.
  • the substantially water free solid phosphate salt product [74] which will be a mixture of several different salts, can still contain water as water of hydration; such water of hydration can be necessary for the stable formation of such salt mixtures.
  • the substantially water free solid phosphate salt product [74] can also contain portions of other volatile products such as acetic acid and ammonia. It is anticipated that volatile components such as water, ammonia, acetic acid, and any other components that can be found to be useful as a component of the final product of the process can be introduced separately in make-up streams [44] into the drying chamber [70] so as to maintain the appropriate concentration of such component in the final product of the inventive process. It is also anticipated that chemical additives that can be beneficial to the handling of the solid product can be introduced into the drying chamber [70], for instance flow improvers and additives that reduce the formation of dust.
  • the liquid phosphate salt containing solution [42] can contain ammonia and it can be necessary for the final solid product to contain ammonia, either as free ammonia or as a salt.
  • the drying process may inadvertently lead to removal of most of the ammonia; this ammonia can be restored into the final product by introducing a stream of pure ammonia or ammonium hydroxide, or other ammonia-containing feedstock, into the drying chamber at such a concentration as to produce a substantially water free solid phosphate salt product [74] that contains the appropriate amount of ammonia.
  • water or steam can be introduced into the drying chamber to ensure that the dried substantially water free solid phosphate salt product [74] contains the appropriate amount of water of hydration, if necessary.
  • the excess water, ammonia, or other product can be recovered with the water vapor from the chamber and recycled to the front end of the process.
  • the liquid phosphate salt containing solution [42] is produced continuously; the liquid product is then fed into a continuous process for making a substantially water free solid phosphate salt product [74]; the substantially water free solid phosphate salt product [74] is then either used as is, or mixed into a liquid petroleum or other combustible base oil or solid fuel for delivery into an engine or other combustion power device such as a furnace or boiler.
  • the liquid phosphate salt containing solution is introduced into a continuous process to make liquid hydrocarbon- based phosphate salt containing product by removing the water from the liquid phosphate salt containing solution. Removal of the water can be accomplished using methods known in the art, such as via thin film evaporation or other means of distillation, as a continuous process. These two processes are preferred because the heat of solution plus the heat of reaction produced in making the liquid phosphate salt containing solution can be used in the next step of the process, either the spray drying step, or the water stripping step, thereby conserving energy.
  • phosphate salt containing product is such a small portion of the final liquid oil based phosphate containing product
  • a very small continuous phosphate salt containing product reactor train could be used to make a very large volume of liquid hydrocarbon-based phosphate salt containing product.
  • the particles could be formed in-situ to produce particles of intermediate size in the desired matrix.
  • the initial particles are formed by dissolving the desired salts or, other hydrocarbon in soluble compounds, in a water parent solution. This solution is then emulsified with a carrier fluid, which can be the final desired matrix. The emulsion is then dehydrated with heat or vacuum or both to produce the initial particle dispersion.
  • the final concentration of total phosphorous in the substantially water free solid phosphate salt product [74] is preferably about 1 to 20% by weight.
  • a preferred concentration of total phosphorous in the substantially water free solid phosphate salt product [74] is about 5-17% by weight.
  • a most preferred concentration of total phosphorous in the substantially water free solid phosphate salt product [74] is about 8 to 15% by weight.
  • the final concentration of total phosphorous in the oil based phosphate containing product is preferably about 3,500 ppm; a more preferred concentration is between 1 ,000 and 3,000 ppm.
  • liquid phosphate salt containing solution wi th the base stock hydrocarbon to make an emulsified water-in-oil mixture continuously could be conveniently accomplished by passing the mixture through a static mixer in a pipe, much as described for the mixing of the ingredients in the continuous production of liquid phosphate salt containing solution. Therefore, one embodiment of the present invention includes the continuous production of liquid phosphate salt containing solution in a pipe by adding the raw materials at various feed points in the pipe, mixing the raw materials using static mixers, and then feeding the finished liquid phosphate salt containing solution into a second pipe system where it can be mixed with the dispersants and base stock hydrocarbon for making the emulsified water-in-oil mixture.
  • a static mixer can be used to achieve the production of the microemulsion in the mixture.
  • the microemulsion is preferably pumped into a stripping column where the water is removed from the emulsified water-in-oil mixture.
  • Another embodiment of the present invention includes the production of liquid phosphate salt containing solution in a continuous process in a pipe as described above, followed by feeding the continuously produced liquid phosphate salt containing solution, internally heated by the reaction of the various feedstocks, into a spray drying unit where additional heating can be used to produce the substantially water free solid phosphorous salt product continuously.
  • This substantially water free solid phosphorous containing product can be used as is, mixed with solid fuel, mixed with liquid hydrocarbon or other base stock.
  • the solid can be further ground or milled in order to achieve the production of small nanometer-sized particles that can be used as is or mixed with a base stock hydrocarbon.
  • the substantially water free solid phosphorous salt product can be milled or ground to provide phosphate salt particles having sub-micron and below sized particles.
  • the optimal particle size would range from 2 microns to less than 1 micron, preferably from less than 1 micron to less than 100 nanometers in diameter.
  • the nano-sized particles of the solid product can then be added directly to the combustion chamber of the hydrocarbon fuel.
  • the nano-sized particles of substantially water free solid phosphorous salt product can be dispersed or suspended in a carrier fluid, or dispersion liquid. In so doing, it is known that particles of less than 10 nm in diameter can be dispersed in liquids and are not visible to the naked eye.
  • Methods of producing solid nano-sized particles are disclosed in US 6,548,039 and US 6,440,383, the disclosures of which are incorporated herein by reference.
  • the present invention relates to sub-micron and smaller particles, e.g., nano-sized particles, used in the dry state as combustion catalysts or modifiers to improve combustion resulting in reduced emissions or improved fuel economy or both.
  • the particles preferably have a particle with a size of less than 1 micron, more preferably less than 0.1 micron and most preferably less than 0.01 micron.
  • Particle size actually refers to a particle size distribution with the specified size being the average of the distribution.
  • the average can be either a number average which is calculated based on the number of particles in each fraction of the distribution or weight average which is calculated from the weight of the particles in each fraction of the distribution.
  • the ratio of the weight average particle size to the number average particle size is the dispersity.
  • Dispersity is a measure of the broadness of the distribution. It is preferred that the particle size distribution be as narrow as possible in order to achieve optimum performance. A particle dispersity of less than 5 is preferred. A dispersity of less than 3 is more preferred. And, a dispersity of less than 2 is most preferred.
  • the substantially water free solid phosphate salt product can be dissolved in a volatile solvent in which it is soluble and then spray dried to produce the dried particle.
  • the particle can be further reduced in size if necessary by any of the methods described above.
  • the desired chemical composition of the particle can be formed in-situ by reaction of precursor chemicals in a volatile solvent in which the final product is soluble.
  • the solution can then be spray dried and reduced as above.
  • the particle size is preferably less than 1 micron and the particles are in the dry state.
  • the chemical composition of the plurality of particles of the substantially water free solid phosphate salt product can be any inorganic salt or compound that provides a catalytic effect in hydrocarbon combustion processes such that the combustion emissions are reduced or fuel economy is improved, or both.
  • the chemical composition preferably does not include the elements of platinum, palladium or cerium.
  • Preferred chemical compositions are any of the alkali metal salts of phosphoric acid.
  • Other preferred compositions are any of the ammonium salts of phosphoric acid.
  • the particles can be mixtures of ammonium and alkali metal salts of phosphoric acid.
  • the particles can be alkali metal or ammonium salts or mixtures thereof of boric acid or other suitable boron containing compounds.
  • the particles can contain the elements of Groups IA, IIA, HIA, IVA, VA, IHB, IVB, VB, VIB, VIIB, and VIII of the Periodic Table of Elements, in any form including salts, covalent inorganic compounds, or in elemental form, with the exception of Pt, Pd and Ce containing compositions.
  • the particles can also be organic compounds of the foregoing elements.
  • an oil based phosphate containing product is formed by preparing the liquid phosphate salt containing solution either from the “salts” process or in situ using the “exothermic” process from the appropriate acids and bases.
  • the liquid phosphate salt containing solution is mixed with a base stock hydrocarbon in which the salt solution is not soluble to form an emulsified water-in-oil mixture.
  • High shear mixing is applied to the emulsified water-in-oil mixture such that when the emulsion is dehydrated the resulting particle dispersion contains particles in the sub-micron and smaller range.
  • the preparation of the liquid phosphate salt containing solution is continuous and formation of the micro-emulsion is continuous, using an in-line static mixer.
  • These dry particles can be used as fuel additives, catalysts, and other treatment aids to improve combustion and reduce emissions.
  • the fuels can be any hydrocarbon type fuel and can be either gas, liquid or solid or any combinations thereof. Additionally, the particles can be added directly to the combustion chamber or zones in any manner applicable including mixing with the fuel (fuel borne), mixing with the air, adding directly as a separate stream, or any combinations thereof.
  • the nano-sized phosphate salt particles can be dispersed in a matrix in which the particles are not soluble.
  • a dispersion matrix is mineral oil.
  • intermediate sized particles of the phosphate salts can be mechanically milled or ground directly to the desired sub-micron or nano-particle size in the same matrix in which they were formed.
  • An alternate embodiment is directed to forming the particles at high concentrations in one matrix, grinding the particles in this matrix and then diluting with another preferred matrix, especially if the initial matrix might provide an advantage in the milling or grinding step over the final preferred matrix.
  • the initial solid particle is directly slurried into a matrix in which the particles are insoluble, such as a mineral oil, as opposed to the in-situ formation described above.
  • the particles are then milled or ground to the desired size in one- step or in multi-grinding steps as is mechanically required.
  • the particles could be slurried in a suitable or preferred grinding matrix and then diluted with another fluid that might be more suitable for the final application.
  • the particle dispersions can be made in batch processes, continuous processes, combination of batch-continuous processes, or in continuous stirred tank reactor system (CSTR), or in any manner that produces a particle dispersion of the active compound or agent in a matrix such that the average particle size is below 1 micron, preferably below 0.5 microns and more preferably below 0.01 micron.
  • the fuels can be any hydrocarbon type fuel and can be either gas, liquid or solid or any combinations thereof.
  • the particle dispersions can be added to the combustion chamber or zones in any manner applicable including mixing with the fuel (fuel borne), mixing with the air, adding directly as a separate stream, or any combinations thereof.
  • the combustion device can be an internal combustion engine, a turbine, an open flame, or any combustion device in which hydrocarbon fuel is used to convert chemical energy to work or power or heat.
  • Hydrocarbon fuel is any fuel that contains the elements of hydrogen and carbon.
  • the hydrocarbon fuel can also contain other elements including but not limited to oxygen and nitrogen.

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  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Edible Oils And Fats (AREA)
  • Lubricants (AREA)

Abstract

La présente invention propose un procédé en continu de production d'un produit contenant du phosphate à base d'huile. Le procédé en continu consiste à mélanger de l'eau avec au moins une base et un acide orthophosphorique pour produire une solution contenant un sel de phosphate liquide. Cette solution est ensuite séchée, granulée et mélangée avec un hydrocarbure de base pour former le produit contenant un phosphate à base d'huile.
PCT/US2007/022598 2006-10-26 2007-10-25 Procédé pour préparer des produits contenant un sel de phosphate WO2008057232A2 (fr)

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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005001004A2 (fr) * 2003-06-23 2005-01-06 Envirofuels L.P. Additif destine a du combustible hydrocarbone et procede associe
WO2006037094A1 (fr) * 2004-09-28 2006-04-06 Envirofuels L.L.C. Additif pour bruleurs a mise a feu directe et flammes nues alimentes par un hydrocarbure liquide ou liquefie, et procedes associes

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005001004A2 (fr) * 2003-06-23 2005-01-06 Envirofuels L.P. Additif destine a du combustible hydrocarbone et procede associe
WO2006037094A1 (fr) * 2004-09-28 2006-04-06 Envirofuels L.L.C. Additif pour bruleurs a mise a feu directe et flammes nues alimentes par un hydrocarbure liquide ou liquefie, et procedes associes

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