EP3224334A2 - Systeme und verfahren im zusammenhang mit der trennung von wachsprodukten aus fischer-tropsch-produkten - Google Patents

Systeme und verfahren im zusammenhang mit der trennung von wachsprodukten aus fischer-tropsch-produkten

Info

Publication number
EP3224334A2
EP3224334A2 EP15807697.6A EP15807697A EP3224334A2 EP 3224334 A2 EP3224334 A2 EP 3224334A2 EP 15807697 A EP15807697 A EP 15807697A EP 3224334 A2 EP3224334 A2 EP 3224334A2
Authority
EP
European Patent Office
Prior art keywords
product
separation liquid
gas stream
wax
temperature
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.)
Withdrawn
Application number
EP15807697.6A
Other languages
English (en)
French (fr)
Inventor
Shehzada Khurram
Zeeshan NAWAZ
Khalid Karim
Thabet AL-QAHTANI
Abdullah Turki AL-JALOUD
Saud AL-KHUDEER
Ali AL-HAMMAD
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.)
SABIC Global Technologies BV
Original Assignee
SABIC Global Technologies BV
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 SABIC Global Technologies BV filed Critical SABIC Global Technologies BV
Publication of EP3224334A2 publication Critical patent/EP3224334A2/de
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/16—Oxygen-containing compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/06—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by gas-liquid contact
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/08—Inorganic compounds only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/14—Hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/34—Apparatus, reactors
    • C10G2/341—Apparatus, reactors with stationary catalyst bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1022—Fischer-Tropsch products

Definitions

  • Syngas mixtures of hydrogen (3 ⁇ 4)
  • carbon monoxide CO
  • syngas mixtures of hydrogen (3 ⁇ 4)
  • carbon monoxide CO
  • a number of well-known industrial processes use syngas for producing various oxygenated organic chemicals.
  • the Fischer- Tropsch catalytic process for catalytically producing hydrocarbons from syngas was initially discovered and developed in the 1920's, and was used in South Africa for many years to produce gasoline range hydrocarbons as automotive fuels.
  • the products produced in a Fischer-Tropsch catalytic process comprise a portion of wax. It is desired to separate the wax from the hydrocarbons in the products so that the hydrocarbons can be further processed in downstream processes.
  • a system comprising: a) a separator tank comprising a first inlet, a second inlet, a first outlet, and a second outlet; b) a heat exchanger; and c) a holding tank comprising a third inlet and a third outlet, wherein the separator tank is in fluid communication with the holding tank via a first connector and via a second connector, wherein the first connector is connected to the first outlet of the separator tank and to the third inlet of the holding tank, wherein the second connector is connected to the first inlet of the separator tank and to the third outlet of the holding tank, and wherein the first connector and the second connector are in communication with the heat exchanger.
  • Also disclosed herein is a method comprising the steps of: a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
  • Also disclosed herein is a method comprising the steps of: a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form; b) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; c) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and d) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
  • a method comprising a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product; c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid
  • FIG. 1 shows a system disclosed herein.
  • Ranges can be expressed herein as from “" one particular value, and/or to "" another particular value. When such a range is expressed, another aspect includes from the one particular value and/or to the other particular value. Similarly, when values are expressed as approximations, by use of the antecedent "," it will be understood that the particular value forms another aspect. It will be further understood that the endpoints of each of the ranges are significant both in relation to the other endpoint, and independently of the other endpoint.
  • X and Y are present at a weight ratio of 2:5, and are present in such a ratio regardless of whether additional components are contained in the compound.
  • a weight percent of a component is based on the total weight of the formulation or composition in which the component is included.
  • STY space time yield
  • Waxes produced from Fischer-Tropsch processes are typically paraffin waxes, that is, a mixture of hydrocarbon molecules, wherein each molecule contains from 20 to 100 carbon atoms.
  • the systems and methods disclosed herein provide means for separating wax from other hydrocarbons, such as, for example, light hydrocarbons.
  • Isothermal and/or adiabatic fixed bed reactors can be used to carry out the Fischer- Tropsch process.
  • the isothermal and/or adiabatic fixed bed reactors are used to convert syngas to hydrocarbon products, including, olefins, waxes (e.g. paraffins) and alcohols.
  • the amount of waxes in the hydrocarbon products is less than 5%. In one aspect, the amount of waxes in the hydrocarbon products is less than 4%, 3%, 2%, or 1%.
  • a system comprising: a) a separator tank comprising a first inlet, a second inlet, a first outlet, and a second outlet, b) a heat exchanger, and c) a holding tank comprising a third inlet and a third outlet, wherein the separator tank is in fluid communication with the holding tank via a first connector and via a second connector, wherein the first connector is connected to the first outlet of the separator tank and to the third inlet of the holding tank, wherein the second connector is connected to the first inlet of the separator tank and to the third outlet of the holding tank, and wherein the first connector and the second connector are in communication with the heat exchanger.
  • the system further comprises a Fisher-Tropsch reactor comprising a fourth inlet and a fourth outlet, wherein the separator tank is in fluid communication with the Fisher-Tropsch via a third connector, wherein the third connector is connected to the to the fourth outlet of the Fisher-Tropsch reactor and the second inlet of the separator tank.
  • the second connector is in communication with a pump.
  • the pump facilitates the transfer of purified separation fluid from the holding tank to the separator tank.
  • the heat exchanger serves two purposes.
  • the first purpose is to lower the temperature of the separation liquid comprising a first wax product that is being transported from the separator tank to the holding tank, such lowering the temperature to a second temperature.
  • the temperature of the separation liquid comprising a first wax product can be, for example, lowered from about 140 °C to about 145 °C.
  • the second purpose is to increase the temperature of the second separation liquid being transported from the holding tank to a fourth temperature.
  • the fourth temperature can be from about 160 °C to about 190 °C.
  • the third connector is configured to transport a first product gas stream comprising a first wax product and a first lower hydrocarbon product from the Fischer-Tropsch reactor to the separator tank.
  • the separator tank is configured to withstand at least a pressure of above about 12 bar.
  • the separator tank can be configured to withstand at least a pressure from about 12 bar to about 20 bar.
  • the separator tank is configured to support a Fischer-Tropsch system on an industrial scale.
  • the separator tank is configured to hold a volume of a first separation fluid on an industrial scale.
  • the holding tank can be configured to hold at least about 1,000 liter of separation fluid.
  • the holding tank can be configured to have a volume from at least about 1,000 liters to about 20,000 liters.
  • the first connector is configured to transport a first wax portion and a first separation liquid from the separator tank to the holding tank.
  • the holding tank is configured to support a Fischer-Tropsch system on an industrial scale.
  • the holding tank is configured to hold a volume of a first separation fluid and a first wax product on an industrial scale.
  • the holding tank can be configured to hold at least about 1,000 liters of separation fluid and wax.
  • the holding tank can be configured to have a volume from at least about 1,000 liters to about 20,000 liter.
  • the second connector is configured to transport a second separation liquid from the holding tank to the separator tank.
  • the separator tank comprises a fifth outlet.
  • the fifth outlet can be connected to a fifth connector that is configured to remove a first lower hydrocarbon product from the separator tank.
  • the holding tank comprises a sixth outlet.
  • the sixth outlet can be connected to a sixth connector that is configured to remove a first wax product from the holding tank.
  • the disclosed system can be operated or configured on an industrial scale.
  • the system, apparatus, and methods disclosed herein can be configured to produce a first product gas stream comprising a first wax product and a first lower hydrocarbon product on an industrial scale.
  • the apparatus and methods can separate a first wax product from a first product gas stream comprising a first wax product and a first lower hydrocarbon product in batches on an industrial scale.
  • the batch size can comprise any desired industrial-scale batch size.
  • the disclosed system can be operated or performed on any desired time scale or production schedule that is commercially practicable.
  • the disclosed system, apparatus, and methods can produce a quantity of at least 1 ton of a first product gas stream comprising a first wax product and a first lower hydrocarbon product in a period of 2 hr or less, including exemplary quantities of at least about 10 tons within the period.
  • the period of time can be 1 hr.
  • the disclosed system, apparatus, and methods can have a STY of at least 0.5/kg/hr of catalyst for the reactors disclosed herein.
  • the disclosed system, apparatus, and methods can have a STY of at least 0.7/kg/hr of catalyst for the reactors disclosed herein.
  • the disclosed system, apparatus, and methods can have a STY from 0.5 to 1/kg/hr of catalyst for the reactors disclosed herein.
  • the components of the disclosed system and apparatus can be shaped and sized to permit production of a first product gas stream comprising a first wax product and a first lower hydrocarbon product on an industrial scale.
  • FIG. 1 shows a system (100).
  • the system (100) has a Fisher-Tropsch reactor (104).
  • the Fisher-Tropsch reactor (104) has a fourth inlet connected to a fourth connector (102) and a fourth outlet connected to a third connector (106).
  • the third connector (106) is connected to the separator tank (108) via a second inlet on the separator tank (108).
  • the separator tank (108) has a first outlet connected to a first connector (110).
  • the first connector (110) is in communication with heat exchanger (112).
  • the first connector (110) is connected to the holding tank (114) via a third inlet on the holding tank (114).
  • the holding tank (114) has a third outlet that is connected to a second connector (116).
  • the second connector (116) is in communication with heat exchanger (112).
  • the second connector (116) can also be in communication with a pump (118).
  • the second connector (116) is connected to the separator tank (108) via a first inlet on the separator tank (108).
  • the separator tank (108) has a fifth outlet connected to a fifth connector (122), which is configured to remove products from the separator tank (108).
  • the holding tank (114) can have a sixth outlet connected to a sixth connector (120), which is configured to remove wax.
  • the systems disclosed herein can be used in methods to separate wax, such as, for example, paraffins, from a hydrocarbon stream comprising light hydrocarbons.
  • a method comprising the steps of: a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
  • the method can further comprise the steps of c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
  • Also disclosed herein is a method comprising the steps of: a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form; b) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; c) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and d) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
  • the method further comprises the steps of e) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and f) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with the second separation liquid having the fourth temperature, thereby liquefying or solidifying at least a portion of the first wax product into the second separation, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
  • the method further comprises the step of transporting the first separation liquid comprising the first wax product from the holding tank to the heat exchanger.
  • the step of a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form is performed in a holding tank.
  • a method comprising a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product; c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid
  • the second separation liquid can recycled back into step b) and is the first separation liquid.
  • the recycling of the second separation liquid is continuous.
  • the first separation liquid and the second separation liquid being recycled in the separation tank can have a temperature from about 160 °C to about 190 [0046]
  • the first temperature is from about 230 °C to about 250 °C.
  • the first temperature can be from about 235 °C to about 245 °C.
  • the second temperature is from about 160 °C to about 190 °C.
  • the second temperature can be from about 165 °C to about 185 °C, such as, from about 170 °C to about 180 °C.
  • the third temperature is from about 140 °C to about 145 °C.
  • the third temperature is from about 142 °C to about 144 °C.
  • the fourth temperature is from about 160 °C to about 190 °C.
  • the fourth temperature can be from about 165 °C to about 185 °C, such as, from about 170 °C to about 180 °C.
  • the first product gas stream comprises less than 5% of the first wax product.
  • the first product gas stream can comprise less than 3% of the first wax product.
  • first product gas stream can comprise less than 2% of the first wax product.
  • the first product gas stream comprises from about 1% to about 5% of the first wax product.
  • the second product gas stream comprises less than 0.5% of the first wax product.
  • the second product gas stream can comprise less than 0.3% of the first wax product.
  • the second product gas stream can comprise less than 0.1% of the first wax product.
  • the second product gas stream comprises from about 0.01% to 0.5% of the first wax product.
  • At least 50% of the first wax product is separated from the first product gas stream.
  • at least 70% of the first wax product is separated from the first product gas stream.
  • at least 80% of the first wax product can be separated from the first product gas stream.
  • at least 85% of the first wax product can be separated from the first product gas stream.
  • at least 90% of the first wax product can be separated from the first product gas stream.
  • at least 95% of the first wax product can be separated from the first product gas stream.
  • at least 97% of the first wax product can be separated from the first product gas stream.
  • at least 99% of the first wax product can be separated from the first product gas stream.
  • the first product gas stream comprises from about 50% to about 99% of the first lower hydrocarbon product.
  • the first product gas stream can comprise from about 50% to about 90% of the first lower hydrocarbon product.
  • the first product gas stream can comprise from about 60% to about 80% of the first lower hydrocarbon product.
  • the first hydrocarbon product comprises C2-C5 hydrocarbons.
  • the first separation liquid comprises silicone oil, an ionic liquid, or a glycol, or a combination thereof.
  • the first separation liquid can comprise silicone oil.
  • the first separation liquid can comprise an ionic liquid, such as ioniq liquids of silver and copper salts, such as for example, silver tetrafluoroborate.
  • the first separation liquid can comprise a glycol.
  • the glycol can be a mono, di, or tri glycol compounds.
  • suitable glycols include ethylene glycol, propylene glycol, and 1,3, butanediol.
  • the first separation liquid can be selected to be a liquid that is inert to the first product gas stream and has a boiling point above that of the temperature, such as about 160 °C to about 190 °C, during operating pressure conditions of the separator tank.
  • the operating pressure of the separator tank can be from about 3 bar to about 12 bar.
  • the second separation liquid comprises less than 0.5% of the first wax product.
  • the second separation liquid can comprise less than 0.3% of the first wax product.
  • the second separation liquid can comprise less than 0.1% of the first wax product.
  • the second separation liquid can comprise less than 0.05% of the first wax product.
  • the second separation liquid comprises from about 0.01% to 0.5% of the first wax product.
  • the second separation liquid is substantially identical to the first separation liquid.
  • the second separation can be the first separation liquid.
  • the separating at least a portion of the first wax product from the first product gas stream is performed in a separator tank at a pressure from about 3 bar to about 12 bar.
  • the separating at least a portion of the first wax product from the first product gas stream is performed in a separator tank at a pressure from about 5 bar to about 10 bar.
  • the first product gas stream comprises less than 10% of C6+
  • the first product gas stream comprises less than 8% of C6+ hydrocarbons. In another aspect, the first product gas stream comprises less than 5% of C6+ hydrocarbons. In yet another aspect, the first product gas stream comprises from about 1% to about 10% of C6+ hydrocarbons.
  • the first wax product is in solid form when separated from the first gas product stream. In another aspect, the first wax product is in liquid form when separated from the first gas product stream.
  • the step of removing the first wax product from the first separation liquid comprises scrapping or skimming the first wax product from the first separation liquid.
  • the method further comprises transporting the second separation liquid having the fourth temperature to a separator tank.
  • a method comprising the steps of: a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
  • Aspect 2 The method of aspect 1, wherein the method further comprises the steps of: c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
  • Aspect 3 The method of aspect 2, wherein the second separation liquid is recycled back into step b) and is the first separation liquid.
  • Aspect 4 The method of any one of aspects 1-3, wherein the first temperature is from about 230 °C to about 250 °C.
  • Aspect 5 The method of any one of aspects 1-4, wherein the second temperature is from about 160 °C to about 190 °C.
  • Aspect 6 The method of any one of aspects 2-5, wherein the third temperature is from about 140 °C to about 145 °C.
  • Aspect 7 The method of any one of aspects 1-6, wherein the first product gas stream comprising less than 5% of the first wax product.
  • Aspect 8 The method of any one of aspects 1-7, wherein the second product gas stream comprising less than 0.5% of the first wax product.
  • Aspect 9 The method of any one of aspects 1-7, wherein the first product gas stream comprising from about 50% to about 99.5% of the first lower hydrocarbon product.
  • Aspect 10 The method of any one of aspects 1-9, wherein at least 50% of the first wax product is separated from the first product gas stream.
  • Aspect 11 The method of any one of aspects 1-9, wherein at least 80% of the first wax product is separated from the first product gas stream.
  • Aspect 12 The method of any one of aspects 1-9, wherein at least 90% of the first wax product is separated from the first product gas stream.
  • Aspect 13 The method of any one of aspects 1-12, wherein the first hydrocarbon product comprises C2-C5 hydrocarbons.
  • Aspect 14 The method of any one of aspects 1-12, wherein the first separation liquid comprises silicone oil, an ionic liquid, or a glycol, or a combination thereof.
  • Aspect 15 The method of any one of aspects 1-14, wherein the second separation liquid comprises less than 0.5% of the first wax product.
  • Aspect 16 The method of any one of aspects 1-15, wherein the second separation liquid is substantially identical to the first separation liquid.
  • Aspect 17 The method of any one of aspects 1-16, wherein the separating at least a portion of the first wax product from the first product gas stream is performed in a separator tank at a pressure from about 3 bar to about 12 bar.
  • Aspect 18 The method of any one of aspects 1-18, wherein the first product gas stream comprises less than 10% of C10+ hydrocarbons.
  • a method comprising the steps of: a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form; b) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; c) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and d) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
  • Aspect 20 The method of aspect 19, wherein the first separation liquid comprises at least 10% of the first wax product.
  • Aspect 21 The method of aspects 19 or 20, wherein the second temperature is from about 160 °C to about 190 °C.
  • Aspect 22 The method of any one of aspects 19-21, wherein the third temperature is from about 140 °C to about 145 °C.
  • Aspect 23 The method of any one of aspects 19-22, wherein step a) is performed in a holding tank.
  • Aspect 24 The method of aspect 23, wherein the method further comprises the step of transporting the first separation liquid comprising the first wax product from the holding tank to the heat exchanger.
  • Aspect 25 The method of any one of aspects 19-24, wherein the first wax product is in solid form.
  • Aspect 26 The method of any one of aspects 19-25, wherein removing the first wax product from the first separation liquid comprises scrapping or skimming the first wax product from the first separation liquid.
  • Aspect 27 The method of any one of aspects 19-26, wherein the second separation liquid comprises less than 0.5% of the first wax product.
  • Aspect 28 The method of any one of aspects 19-27, wherein the method further comprises the step of transporting the second separation liquid to a heat exchanger and increasing the temperature of the second separation liquid to a fourth temperature.
  • Aspect 29 The method of aspect 28, wherein the fourth temperature is from about 160 °C to about 190 °C.
  • Aspect 30 The method of aspects 28 or 29, wherein the method further comprises transporting the second separation liquid having the fourth temperature to a separator tank.
  • Aspect 31 The method of aspect 30, wherein the method further comprises the steps of: e) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and f) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with the second separation liquid having the fourth temperature, thereby liquefying or solidifying at least a portion of the first wax product into the second separation, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
  • Aspect 32 The method of aspect 31, wherein the first product gas stream comprising less than 5% of the first wax product.
  • Aspect 33 The method of aspects 31 or 32, wherein the second product gas stream comprising less than 0.5% of the first wax product.
  • Aspect 34 The method of any one of aspects 31-33, wherein the first product gas stream comprising from about 50% to about 99.5% of the first lower hydrocarbon product.
  • Aspect 35 The method of any one of aspects 31-34, wherein at least 50% of the first wax product is separated from the first product gas stream.
  • Aspect 36 The method of any one of aspects 31-35, wherein at least 80% of the first wax product is separated from the first product gas stream.
  • Aspect 37 The method of any one of aspects 31-36, wherein at least 90% of the first wax product is separated from the first product gas stream.
  • Aspect 38 The method of any one of aspects 31-37, wherein the first hydrocarbon product comprises C2-C5 hydrocarbons.
  • Aspect 39 The method of any one of aspects 19-38, wherein the first separation liquid comprises silicon oil, an ionic liquid, or a glycol, or a combination thereof.
  • a system comprising: a) a separator tank comprising a first inlet, a second inlet, a first outlet, and a second outlet; b) a heat exchanger; c) a holding tank comprising a third inlet and a third outlet, wherein the separator tank is in fluid communication with the holding tank via a first connector and via a second connector, wherein the first connector is connected to the first outlet of the separator tank and to the third inlet of the holding tank, wherein the second connector is connected to the first inlet of the separator tank and to the third outlet of the holding tank, and wherein the first connector and the second connector are in communication with the heat exchanger.
  • Aspect 41 The system of aspect 40, wherein the system further comprises a Fisher- Tropsch reactor comprising a fourth inlet and a fourth outlet, wherein the separator tank is in fluid communication with the Fisher-Tropsch via a third connector, wherein the third connector is connected to the to the fourth outlet of the Fisher-Tropsch reactor and the second inlet of the separator tank.
  • Aspect 42 The system of aspect 40 or 41, wherein separator tank is configured to withstand pressure above 15 bar.
  • Aspect 43 The system of any one of aspect 40-42, wherein the holding tank is configured to hold at least 1,000 liters of separation fluid.
  • Aspect 44 The system of any one of aspect 40-43, wherein the separator tank is configured to hold at least 1,000 liters of separation fluid.
  • Aspect 45 The system of any one of aspect 40-44, wherein the second connector is in communication with a pump.
  • Aspect 46 The system of any one of aspect 40-45, wherein the separator tank comprises a fifth outlet.
  • Aspect 47 The system of any one of aspect 40-46, wherein the holding tank comprises a sixth outlet.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Developing Agents For Electrophotography (AREA)
EP15807697.6A 2014-11-26 2015-11-17 Systeme und verfahren im zusammenhang mit der trennung von wachsprodukten aus fischer-tropsch-produkten Withdrawn EP3224334A2 (de)

Applications Claiming Priority (2)

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US201462084644P 2014-11-26 2014-11-26
PCT/IB2015/058895 WO2016083946A2 (en) 2014-11-26 2015-11-17 Systems and methods related to the separation of wax products from products

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EP (1) EP3224334A2 (de)
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US20260008970A1 (en) * 2022-10-26 2026-01-08 Sabic Global Technologies B.V. Systems and methods for processing pyrolysis oil

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US20070131583A1 (en) * 2005-12-13 2007-06-14 Syntroleum Corporation Fischer-Tropsch product condensing process for cold climates
US20080021118A1 (en) * 2006-07-21 2008-01-24 Syntroleum Corporation Hydrocarbon recovery in the fischer-tropsch process
GB2479737A (en) * 2010-04-19 2011-10-26 Gtl F1 Ag Apparatus and Method for Conducting a Fischer-Tropsch Synthesis Reaction
US9238193B2 (en) * 2013-07-23 2016-01-19 Chevron Phillips Chemical Company Lp Separations with ionic liquid solvents

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US20170369797A1 (en) 2017-12-28

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