WO2019212421A1 - Method of processing a bio-based material and apparatus for processing the same - Google Patents
Method of processing a bio-based material and apparatus for processing the same Download PDFInfo
- Publication number
- WO2019212421A1 WO2019212421A1 PCT/TH2019/000010 TH2019000010W WO2019212421A1 WO 2019212421 A1 WO2019212421 A1 WO 2019212421A1 TH 2019000010 W TH2019000010 W TH 2019000010W WO 2019212421 A1 WO2019212421 A1 WO 2019212421A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- various embodiments
- reactor
- treated oil
- temperature
- bio
- Prior art date
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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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
-
- 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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
-
- 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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/003—Specific sorbent material, not covered by C10G25/02 or C10G25/03
-
- 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
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- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
- C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
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- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
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- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/54—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
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- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/60—Controlling or regulating the processes
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- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including a sorption process as the refining step in the absence of hydrogen
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- 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
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
- C10L1/026—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for compression ignition
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- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
- C11C1/08—Refining
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- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/12—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation
- C11C3/123—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation using catalysts based principally on nickel or derivates
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- 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
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- C10G2300/1011—Biomass
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- C10G2300/1014—Biomass of vegetal origin
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- 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
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- C10G2300/1018—Biomass of animal origin
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- 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
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- C10G2300/1048—Middle distillates
- C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
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- 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
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- C10G2300/20—Characteristics of the feedstock or the products
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- C10G2300/301—Boiling range
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- 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
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- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/304—Pour point, cloud point, cold flow properties
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- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/44—Solvents
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/06—Gasoil
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the present invention relates to a method of processing a renewable resource, in particular a bio-based material, ami an apparatus for processing the same,
- non-renewable resources such as fossil fuel, crude oil and petroleum
- Usage of non-renewable resources may have significant impact on greenhouse gas emissions. Therefore, using alternative sources that are renewable may reduce greenhouse gas emissions and be more environmentally friendly compared to non-renewable resources.
- Biofuel is being increasingly considered as a viable renewable resource for various applications, such as in engines.
- examples of biofuel include biomass derivatives, biogases, and liquid fuels and can be widely divided into bioalcohols, biodiesel, green diesel, vegetable oil, bioethers, biogas, syngas and solid biomass fuels.
- T here are various challenges with using biofuel.
- biofuel such as vegetable oil in engines requires significant engine modification, including changing of piping and injector construction materials so that engine performance may be maintained as compared to non-renewable resources such as diesel or petrol.
- maintenance costs may be increased due to higher wear and tear, which may lead to an increase in incidences of engine failure.
- a technical problem to be solved by the disclosure or present invention is to provide a treated oil for making green diesel and phase change materials suitable for use in applications such as, but not limited to, engines, car parts and buildings.
- the treated oil of the present invention can be obtained through a method of processing without the need to use any petrochemical source as a starting materia! (or a raw material).
- Another technical problem to be solved by the disclosure or present invention is to provide a method for processing a bid-based material such that high purity of desired products may be obtained.
- a method of processing a renewable bio-based material comprising the step of reacting the bio-based material with hydrogen in the presence of a catalyst on a support in a reactor to form a treated oil; (i) passing the treated oil through a distillation unit and an adsorption unit to form green diesel; and/or (ii) passing the treated oil through at least one distillation column to separate the treated oil into at least one component mid passing the at least one component through an adsorption column; and wherein the reactor Comprises a cooling function for controlling the temperature of the reactor; wherein the cooling function is at least one of an internal cooling function and an external cooling function.
- the treated oil may be obtained in a one-step method and further processed to form green diesel, PCM and/or industrial solvent using a combination of a distillation step mid an adsorption Step. Consequently, high purity of green diesehPCM and/or industrial solvent may be obtained.
- the method is versatile aid easily tunable. Furthermore, the method may lead to a savings in time and costs. b>01 3 ⁇ 4
- the support is alumina (AI2Q3), si tica (SiOi) or alumina-silica (AbOj-SiOa).
- the treated oil comprises at least one kind of n-paraffin and at least one kind of isoparaffin and the method further comprises die step of selecting the catalyst depending on whether a Ibw volume of isoparaffins or a high volume of isoparaffins is desired.
- the support is AI2O3 and the catalyst on AljOj is selected from the group consisting of N iMo/AfeOi and NiW/AbOj.
- the support is AI2O3 and the catalyst on AI2O3 is selected from the group consisting of NiCoMo/AhOs, NiMoP/AbOj and COM0/AI2O3.
- the temperature in the reader is 200°C to 400°C.
- the temperature in the reactor is 250 ® C to 350°C.
- the pressure in the reactor is 25 bar to 40 bar.
- the pressure in the reactor is 30 bar to 40 bar.
- the ratio of hydrogen to the bio-based material is 0.03g hydrogen/g bio-based material to Q.10g hydrogen/g bio-based material.
- the ratio of hydrogen to the bio-based material is 0.05g hydrogen/g bio-based material to 0.07g hydrogen/g bio-based material.
- tiie method further comprises the step of purifying the trdated oil.
- the step of purifying the treated oil comprises the step of passing the treated oil through a high-pressure separator followed by the step of passing through a low-pressure separatin'.
- the reactor is a trickle bed reactor or a packed bed reactor.
- the internal pooling function comprises adding a cooling substance into the reactor.
- the external cooling function is a multi tube or a shallow bed reactor with a best transfer unit
- tire adsorption unit comprises at least one adsorbent selected from the group consisting of activated carbon, ion exchange resin, molecular sieve and chemical adsorbent.
- the at least one component is selected from the group consisting of n-paraffin having less than 16 carbon atoms, n-hexadecane, n-heptadecane, n- octadecane and n-paraffin having more than 18 carbon atoms.
- the adsorption column comprises at least one adsorbent selected from the group consisting of activated carbon, ion exchange resin, molecular sieve and chemical adsorbent.
- a green diesel comprising isoparaffin in an amount of 0 to 10 wt% and n- paraffin in am amount of 90 to 100 wt%.
- the green diesel has a distillation range of 200°C to 350°C.
- the green diesel has a flash point in the range of 1O0 ® C to 130°C.
- the green diesel further comprises total glycerides less titan 0,05wt%.
- phase change material comprising isoparaffin in an amount of 0 to 1 wt% and n- paraffin in an amount of 99 to 100 wt%.
- an industrial solvent comprising ti-parafrm and a distillation range of 250°C to 270 t> C.
- a system for processing a renewable bio ⁇ ba$ed material comprising a reactor for reacting the bio-based material with hydrogen in the presence of a catalyst oh a support to form a treated oil; and wherein the reactor comprises a cooling function for controlling the temperature Of the reactor; (i) a distillation unit for passing the treated oil through to form green diesel and an adsorption unit for passing the green diesel through; and/or (ii) at least one distillation column to separate the treated oil into at least one component and an adsorption column for passing the at least one component through; wherein the cooling function is at least one of an internal cooling function and an external cooling function,
- the system may be relatively straightforward, simple and versatile because the treated pil may be obtained in a one-step and further processed to form green diesel, PCM and/or industrial solvent. Consequently, high purity of green diesel, PCM and/or industrial solvent may be obtained. Furthermore, the system may lead to a savings in time and costs.
- the internal cooling function comprises a cooling substance selected from tin? group consisting of a fresh amount of the bio-based material, a fresh amount of hydrogen, a portion of the treated oil aid a combination thereof.
- the system further comprises a high-pressure separator and a low-pressure separator tor passing the treated oil through.
- the external cooling function comprises a multi tube or a shallow bed reactor with a heat transfer unit.
- the external cooling function further comprises a coolant selected from the group consisting of a fresh amount of the bio-based material, a fresh amount of hydrogen, a portion of the treated oil, a combination thereof and a heat transfer fluid.
- an embodiment of the present invention relates to a method of processing a bio-based material to forth a treated oil for making green diesel and phase change materials.
- Figure 1 illustrates a flow diagram of preparing treated oil from a bio-based material and green diesel using the treated oil
- Figure 2 illustrates a flow diagram of preparing at least one phase change material and an industrial solvent using the treated oil prepared from the method in Figure 1 ;
- Figure .3 il lustrates a flow diagram of ah alternative method for preparing treated oil, green diesel, at least one phase change material and an industrial solvent.
- Figure 4 illustrates a flow diagram of the reactor comprising an internal cooling function
- Figure 5 illustrates a flow diagram of the reactor comprising an external cooling function.
- the term“density” refers to the ratio of mass of a particular fuel and volume occupied by the particular fuel.
- the term“cloud point” measures the first appearance of wax.
- the term“contaminant” refers to a substance that is not a desired product of the method of the present invention, such as but not limited to tight hydrocarbons such as propane, hydrogen, water, carbon monoxide, carbon dioxide, nitrogen, sulphur, phosphorus, heavy metals, alkali metals, solids, detergent and acids.
- cooling function refers to the introduction of a cooling substance, coolant and/or a mechanical device/apparatus to decrease or at least maintain the temperature of the reactor to prevent overheating.
- the introduction of a cooling substance includes but is not limited to the introduction of a fresh amount of the bio-based material, introduction of a fresh amount of hydrogen, introduction of a portion of treated oil or introduction of a combination thereof.
- the introduction of coolants includes but is not limited to the introduction of a fresh amount of the bio-based material, introduction of a fresh amount of hydrogen, introduction of a portion of treated oil, introduction of a combination thereof or introduction of a heat transfer fluid.
- the mechanical device/apparatus for cooling the reactor includes but is not limited to a multi tube or, a shallow bed reactor with a heat transfer unit.
- the mechanical deviee/apparalus for cooling the reactor may be integrated with the reactor dr may be a separate unit attachable/detachable from the reactor.
- the term -’cooling substance’ includes but is not limited to the term
- the term“green diesel” refers to a biofuel feat contains mainly paraffin which is derived from a renewable resource such as a bio-based material instead of a nonrenewable resource such as a petroleum-based oil. In other words, there is no need for a non- renewable resource to make the green diesel.
- the term“low volume” when used in relation to the amount of isoparaffin refers to an amount of about 0 to about 5 wt%.
- the term“high volume” when used in relation to the amount of isoparaffin refers to an amount of more than 5 wi%.
- the term“paraffin” includes n-paraffins, isoparaffins and a mixture thereof.
- fee term“"paraffin” refers to acyclic saturated hydrocarbons of general chemical formula Cnt1 ⁇ 2+>.
- n-paraffin refers to a normal paraffin or linear paraffin which is a straight-chain acyclic saturated hydrocarbon.
- the term “isoparaffin” refers to a branched paraffin which is a branched acyclic saturated hydrocarbon
- aromatics refers to aromatic hydrocarbons, i.e. hydrocarbons containing at least one aromatic ring.
- phase change material refers to a material for maintaining the temperature of a system by means of heat transfer between the PCM and the system.
- PCM phase change material
- the temperature of the system is higher than the temperature of the PCM, heat will be transferred from the system to the PCM and it will decrease the temperature of the system.
- the temperature of the system is lower than the temperature of the PCM, heat will be transferred from the PCM to the system and it will increase the temperature of the system.
- the temperature of the PCM will stay the same (e.g. at the melting point of the PCM).
- the PCM can maintain the temperature of the system as at the melting point of fee PCM,
- fee term“treated oil” refers to a pure form of fee oil or at impure form of fee oil
- the oil may comprise at least one kind of n-paraffin, at least one kind of isoparaffin or a combination thereof add may be mixed with contaminants, gases and/or water.
- n-parafftn or isoparaffin refers to a paraffin comprising a specific number of carbon atoms such as a number in fee range of 3 to
- the term“reactant stream” refers to a feed comprising hydrogen and at least one bio-based material.
- the feed may also comprise treated oil.
- fee terms“comprising”,“consisting of * , and fee like are to be construed as non-exhaustive, or in other words, as meaning“including, but not limited to”.
- the term“about” typically means +/- 5% of the stated value, more typically +/- 4% of the stated value, more typically +/- 3% of the stated value, more typically 47- 2% of fee stated value, even more typically +/- 1% of the stated value, and even more typically 47- 0.5% of the stated value.
- range format may be disclosed in a range format. It is appreciable feat fee description in range format is merely for convenience and brevity and should not be construed as a limitation on the scope of the disclosed ranges. Accordingly, the description of a range should be considered to have specifically disclosed all the possible subranges as well as individual numerical values within that range. For example, description of a range such as from 1 to 6 should be considered to have specifically disclosed sub-ranges such as from 1 to 3, from I to 4, from 1 to 5, from 2 to 4, from 2 to 6, from 3 to 6 etc., as well as individual numbers within that range, for example, 1, 2, 3, 4, 5, and 6. Ranges are not limited to integers, and can include decimal measurements. This applies regardless of the breadth of the range.
- a method of processing a biobased material comprising reacting the bio-based material with hydrogen in the presence of a catalyst on a support in a reactor to form a treated oil ; wherein the bio-based material is renewable.
- the treated oil is obtained in high yield by a one-step method involving a hydrotreating reaction.
- the hydrotreating reaction makes use of hydrogen which may bind to sulphur and phosphorus to remove impurities.
- the treated oil may be obtained in a yield of about 80% to about 85% of the bio-based material, More advantageously, the treated oi l does not require more than one step to obtain the treated oil, thereby leading to a savings in time and costs.
- some prior art methods lead to an intermediate product which requires further processing to obtain a product that is substantially equivalent to the treated oil of the present invention. Consequently, such prior art methods require at least one additional step to process the intermediate product to obtain the product that is substantially equivalent to the treated oil of the present invention, thereby making such prior art methods more costly and more time-consuming.
- the bio-based material is a feedstock that is substantially renewable and comprises triglycerides and free fatty acids that may be derived from a plant (including a vegetable) or an animal or a combination thereof.
- the bio-based material includes but is not limited to animal oils such as tallow oil, train oil, fish oil or plant oils such as bleach palm oil (BPO), refined bleach palm oil (RBDPO), palm olein, palm stearin, palm fatty acid distillate, canola oil, com oil, sunflower oil, soybean oil, oils from desertie plants such as jatropha oil and balanites oil, rapeseed oil, tall oil, hempseed oil, olive oil, linseed oil, mustard oil, peanut oil, castor oil, coconut oil, or one or more combinations thereof.
- animal oils such as tallow oil, train oil, fish oil or plant oils such as bleach palm oil (BPO), refined bleach palm oil (RBDPO), palm olein, palm stearin, palm fatty acid distillate, can
- the vegetable oil may be crude vegetable oil or refined credible vegetable oil.
- the plant oil and/or animal oil may be new oil, used oil, waste oil or a combination thereof.
- the method of the present invention Converts the triglycerides to a treated oil containing at least one kind of n-paraffin and at least one kind of isoparaffin almost completely, such that the treated oil is substantially free of triglycerides. Due to the reaction mechanism of the method for producing the treated oil, monoglycerides and diglycerides do hot exist in the treated oil. As such, the total glyceride content in the treated Oil is equivalent to the triglyceride content in the treated oil.
- the treated oil is substantially free of triglycerides. In other words, there is less than I wt%, less than 0.8 wt%, less than 0.6 wt%, less than 0.5 wt%, less than 0.4 wt%, less than 0.3 wt%, less than 0.2 wt%, less than 0, 1 wt%, or less than 0.05 wt% of triglycerides in the treated oil.
- the method of the present invention is relatively more environmentally friendly than a method that makes use of a non-renewable resource such as a petroleum-based material or a mixture of a petroleum-based material aid a bio-based material.
- apparatus 131 is adapted to control tire flow rate and pressure of the bio-based material
- stream lti2 is formed, wherein stream 102 comprises the bio-based material having a predetermined flow rate and pressure, and wherein the pressure of stream 102 is higher than the pressure of stream 101.
- Stream 102 then passes through a heat exchanger (apparatus 132), wherein apparatus 132 is adapted to increase the temperature of stream 102, thereby forming stream 103 which comprises die bio-based material having a predetermined temperature, wherein the temperature of stream 103 is higher than die temperature of stream 102.
- apparatus 132 is adapted to increase the temperature of stream 102, thereby forming stream 103 which comprises die bio-based material having a predetermined temperature, wherein the temperature of stream 103 is higher than die temperature of stream 102.
- hydrogen may be passed through a control valve or a compressor (apparatus 133), wherein apparatus 133 is adapted to control the flow rate and pressure of the hydrogen.
- apparatus 133 is adapted to control the flow rate and pressure of the hydrogen.
- stream 105 is formed, wherein stream 105 comprises hydrogen having a predetermined flow rate and pressure, and wherein the pressure of stream 105 is higher than die pressure of stream 104
- Stream 105 then passes through a heat exchanger (apparatus 134), wherein apparatus 134 is adapted to increase the temperature of stream 105, thereby forming stream 106 which comprises hydrogen having a predetermined temperature, wherein the temperature of stream 106 is higher than the temperature of stream 105.
- stream 103 and stream 106 are introduced intb a reactor (apparatus 135).
- Stream 103 and stream 106 may be introduced into apparatus 135 in the form of co-current
- the method of the present invention may further comprise selecting the catalyst.
- the catalyst may be selected from the group consisting of CoMo, NiMo, NiW, NiCoMo and NiMoP.
- the catalyst may be in the form of sulphide active phases, so that the amount of sulfur in the treated oil may be adj usted/adui (crated,
- the catalyst may be adequately resistant to catalyst poisons, such that the efficiency of the catalyst may be maintained throughout the method.
- the catalyst may be recycled and reused, thereby lowering the operating costs because a new catalyst may not be necessary.
- the efficiency of the catalyst may be recovered by, such as but not limited to, adding a sulfidation agent
- the sulfidation agent may be selected from the group consisting of carbon disulfide, dimethyl disulfide, polysulfide oil, mercaptan and hydrogen sulfide.
- the catalyst may be selected based on whether the desired treated oil should contain a low vo lume of isoparaffins ora high volume of isoparaffins.
- the catalyst is selected from the group consisting of NiMo and NiW if the desired treated oil should contain a low volume of isoparaffins.
- the catalyst is NiMo if the desired treated oil should contain a low volume of isoparaffins.
- the catalyst is selected from the group consisting of NiCoMo, NiMoP and CoMo if the desired treated oil should contain a high volume of isoparaffins.
- the catalyst is NiCoMo if the desired treated oil should contain a high volume Of isoparaffins.
- the catalyst comprises at least one of the two transition metals selected from the group consisting of Ni and Mo. In various embodiments, the catalyst further comprises another transition metal or a group V element. (0082] In various embodiments, the catalyst loading may be about 0.5 wt% to about 20 wt%. The amount of catalyst used may be calculated based on the amount of the bio-based material and hydrogen.
- the catalyst may be separated into one or more portions.
- the extent of the reaction between the biobased material and hydrogen may be controlled.
- the amount of heat produced may be controlled. Consequently, the temperature in the reactor may be controlled.
- the catalyst may be loaded on a support, such as an acidic porous solid support.
- the acidic porous solid support may be alumina (AhOiX silica (SH1 ⁇ 4) or a mixture of alumina and silica (AhOj-SiOz).
- the support may be such as but not limited to fluoride alumina,
- the hydrogen may be fresh hydrogen or recycled hydrogen or a mixture thereof.
- stream 103 and stream 106 may react by contacting the surface of the catalyst in the reactor, thereby producing a treated oil (stream 107).
- stream 107 then passes through a heat exchanger (apparatus 136), wherein apparatus 136 is adapted to reduce the temperature of stream 107, thereby forming stream 108 which comprises treated oil having a predetermined temperature, wherein the temperature of stream 108 is lower than the temperature of stream 107.
- apparatus 136 is adapted to reduce the temperature of stream 107, thereby forming stream 108 which comprises treated oil having a predetermined temperature, wherein the temperature of stream 108 is lower than the temperature of stream 107.
- the method of the present invention may occur under hydrotreating conditions in the reactor.
- the method of the present invention may be carried out at a temperature of about 200°C to about 4Q0°C, about 250°C to about 4QO 0 C > about 250°C to about 350°C or about 300°C to about 350°C and a pressure of about 25 bar to about 50 bar, about 25 bar to about 40 bar, about 30 bar to about 40 bar or about 35 bar to about 40 bar.
- the temperature is relatively low compared to prior art methods. Consequently, less undesired products may he formed.
- the temperature in the reactor is about 300”C to about 350°C because the yield of the desired products would be higher.
- decarboxylation, and/or hydrodeoxygenation and/or isomerization of the bio-based material may also occur because of the choice of catalyst.
- hydrocracking may be inhibited, thereby maintaining the range of carbon number of hydrocarbons formed in the range of CM to C «.
- hydrocracking is an undesirable reaction because it may lead to a decreased amount of PCM in the treated oil, thereby resulting in a lower yield of PCM production.
- the yield of PCM may be advantageously higher than prior art methods because the PCM portion in die treated oil may be higher.
- the method of the present invention may be carried put at a space velocity of about 0.5 per hour (hr 1 ) to about 2 hr 1 or about 1.0 hr *.
- an increase in the space velocity may increase the quantity of treated oil and its products thereof because of the greater capacity to support a higher volume of feedstock.
- a decrease in the space velocity will increase the reaction time and increase the quality of the treated oil and its products thereof, albeit in a lower quantity.
- the space velocity is lower than about 0.5 hr 1 , there may be a drop in the quality -and quantity of the treated oil and its products thereof.
- tire space velocity is about 1.0 hr '1 , there is a balance of the quantity and quality of the treated oil and its products thereof.
- the ratio of hydrogen to the hio-kased material may be about 0.03 g hydrogen/g oil to about 0.10 g hydrogen/g oil, about 0.05 g hydrogen/g oil tp about 0.07 g hydrogen/g oil or about 0.05 g hydrogen/g oil to about 0.08 g hydrogen/g oil If the ratio of hydrogen to the oil is more than 0.1 g hydrogen/g oil, a beneficial effect will not be observed because there is sufficient hydrogen when the ratio of hydrogen to the oil is less than 0.1 g hydrogen/g oil. In other words, 0.03-0.10 g hydrogen/g oil is sufficient. This may advantageously lead to the lowering of operation costs because only a relatively small amount of hydrogen is necessary.
- an increase in the pressure Of hydrogen can increase the solubility of hydrogen in the bio-based material, thereby facilitating the hydrogenation reaction.
- the hydrogenation reaction may occur efficiently.
- the hydrogenation may occur at a relatively low pressure, there may be an economic advantage because compressors to pressurize the hydrogen are not necessary.
- the reactor and other equipment costs may be reduced because operation is at a relatively low pressure.
- the method further comprises purifying the treated oil.
- purifying the treated oil comprises passing the treated oil through a high-pressure separator followed by a low-pressure separator.
- the high-pressure separator may act as a separator and operate at a pressure similar to the pressure of the reactor.
- the high-pressure separator may separate the gaseous component, which may be predominantly hydrogen, from the treated oil.
- the gaseous component may further comprise carbon dioxide, carbon monoxide and propane.
- the carbon dioxide may be removed by a method such as but not limited to pressure swing absorption, absorption with an amine or reaction with a hot carbonate solution.
- carbon monoxide and propane may be removed by tire high-pressure separator.
- the high-pressure separator and/or the low-pressure separator may remove the light fraction, whereby tire light fraction may contain propane and/or sulfur- containing compounds.
- the separating process that makes use of the high- pressure separator and/or the low-pressure separator requires a smaller amount of energy and is a simpler process compared to a process for removing the heavy fraction (such as triglycerides or heavy paraffin content having more than 20 carbon atoms).
- stream 108 passes through a high-pressure separator (apparatus 137) to obtain a purified treated oil (stream 109) and a gaseous component (stream 110).
- apparatus 137 operates at a pressure similar to the pressure in apparatus 135.
- stream 110 may be treated.
- stream 109 passes through a low- pressure separator (apparatus 138), After passing through apparatus 137, the pressure of the purified treated oil (stream 109) may decrease and enter apparatus 138, wherein water (stream 111), which is a by-product may be separated from stream 108 to form a more purified treated oil (stream 112).
- apparatus 138 After passing through apparatus 137, the pressure of the purified treated oil (stream 109) may decrease and enter apparatus 138, wherein water (stream 111), which is a by-product may be separated from stream 108 to form a more purified treated oil (stream 112).
- the reactor is a trickle bed reactor (siieh as but not limited to a narrow tube-type), a packed bed reactor, a shallow bed reactor or a basket-type reactor.
- Each bed is adapted to contain the catalyst, which may be in the form of solid particles.
- the reactor further comprises a cooling function for controlling the temperature of the reactor.
- a cooling function for controlling the temperature of the reactor. This is because reactions such as hydrogenation and deoxygenation are highly exothermic reactions.
- the cooling function advantageously maintains the temperature of the reactor at a suitable temperature range.
- the cooling function minimizes or avoids overheating of the reactor, thereby allowing the reactor’s temperature profile to be optimized, such that the temperature of the reactor is at (or around) an optimal temperature.
- the term“optimal temperature” is defined as a temperature (or temperature range) which the catalyst in the reactor is most active at catalyzing the desired reaction instead of catalyzing one or more unwanted side reactions (such as hydrocracking).
- the feed when the feed comprises bio-based material (such as when the feed consists essentially of biobased material), the feed may be introduced into the reactor at multiple points along the length of the reactor. Consequently, the feed comprising bio-based material may be introduced at a temperature that is near to the optimal temperature. Compared to prior art, the feed comprising bio-based material may be advantageously introduced at a temperature that is nearer to the optimal temperature. This can arise because by introducing the feed comprising bio-based material at multiple points along the length of the reactor, Optimized temperature profile of the reactor may be achieved, which may result in better distribution of temperature within (or throughout) the reactor.
- the catalyst used in the method of the present invention may be better utilized, and a greater efficiency of the catalyst may he «thieved and production rate can be increased. More advantageously, the occurrence of side reactions may be prevented. Side reactions may occur as a result of failure to control the temperature of the reactor, such that the temperature of the reactor may lead to a decrease in the yield of the treated oil. If the reactions such as hydrogenation and deoxygenation occur too quickly, they may be uncontrollable and the temperature of the reaction may in turn be uncontrollable.
- the cooling function comprises an internal cooling function and/or an external cooling function.
- the internal cooling function may operate by means of quenching (or internal cooling).
- Interred cooling is a method of introducing a cooling substance (such as Q l , Q2 in Figure 4) having a tower temperature (such as inlet temperature T ⁇ , in Figure 4) than the temperature of the reactor, thereby maintaining the temperature of the reactor at a suitable temperature.
- a cooling substance such as Q l , Q2 in Figure 4
- the substance for internal cooling include but is not limited to a fresh amount of the bio-based material, a fresh amount Of hydrogen, a portion of treated oil or a combination thereof. Hie portion of treated oil used as the cooling substance may be freshly prepared or prepared in a previous batch.
- the cooling substance may be introduced into the reactor in a single portion or more than one portion and may be dependent on the number of beds in the reactor, in various embodiments, the cooling substance may be introduced into the reactor using a nozzle.
- the nozzle may be pointed at any angle tanging from perpendicular to the flow of the reactant stream aid parallel to the flow of the reactant stream (i,e. co-current).
- tile nozzle Is not pointed against the flow of the reactant stream (i.e. countercurrent).
- prior art methods may introduce the cooling substance through a nozzle, such that the cooling substance is against the flow of the reactant stream (i.e. countercurrent).
- the cooling substance may be accumulated above and/or around the catalyst (such as at a lower end of a catalyst bed, such as a lower end of a first bed, a lower end of a second bed and/or a tower end of a subsequent bed), such that the cooling substance may cause over reaction and/or overheating.
- overheating may occur if the cooling substance is a bio-based material.
- This difference may have an effect on the performance and capability of the internal cooling function. For instance, a fresh amount of the bio-based material can be used as the cooling substance of the present invention, whereas it is not favorable to use a fresh amount of the biobased material for such prior art methods.
- the use of a fresh amount of biobased material as the cooling substance may result in the formation of a hot spot that can negatively affect the quality of toe treated oil and its products thereof and/or negatively affect operation of the method.
- the volume of each portion of the cooling substance may be adjustable from 0 to 100 wt% of the total volume of cooling substance.
- the total volume of cooling substance may be dependent on the range of temperature to be cohttoi led. For instance, if the temperature increase is relatively high (in other words, the range of temperature to be controlled is relatively big), it may be necessary to use a greater volume of cooling substance.
- the temperature in the reactor may be decreased.
- the cooling substance may be introduced via an inlet connected to the reactor.
- a first cooling substance may be introduced via an inlet and the first cooling substance may be distributed over a cross section of a bed of the reactor. The reactant stream from the bed may then contact the first cooling substance at an interface of the bed and an adjacent bed, such that the temperature of the reactant stream is decreased. After the reactant stream contacts the adjacent bed, the temperature of the reactant stream may increase because of the reaction between the bio-based material and hydrogen.
- cooling substance may be introduced via another inlet connected to the reactor, the cooling substance may likewise lower the temperature of the reactant stream when the readmit stream contacts the cooling substance. Consequently, the temperature of the readmit stream may be controlled and maintained at a suitable temperature range.
- the temperature in the reactor 135 may change (or increase) from a first temperature (Ti) to a second temperature (Tz).
- first temperature may be about 320°C and the second temperature may be about 389 ® C.
- the increase in temperature is because the reaction between die bio-based material and hydrogen is an exothermic reaction, thereby producing a significant amount of heat.
- a cooling substance (Ql) may be introduced at the interface (denoted by a dotted line) between the first bed (Bl) andasecond bed (B2), such that die cooling substance (Ql) causes the temperature in die reactor 135 to change (or decrease) from the second temperature (Ta) fo a third temperature (T>).
- the third temperature (Tj) may be the same temperature as the first temperature (T i) or a different temperature, as long as the third temperature (Tj) is lower than the second temperature
- the cooling substance (Ql) having an inlet temperature (Tq) mixes with the reactant stream, which (lows from the first bed (Bl) to the second bed (82).
- the cooling substance (Ql) performs an internal cooling function.
- the temperature in the reactor 135 may change (or increase) from the third temperature (T3) to a fourth temperature (14).
- the fourth temperature (T4) may be the same temperature as the second temperature (T2) or a different temperature, as long as the fourth temperature (T*) is hitter than the third temperature (Tj).
- a fresh portion of the cooling substance (Q2) may be introduced at the interface (denoted by a dotted line) between the second bed (B3) mid a third bed (B3), such that the cooling substance (Q2) causes the temperature in the reactor 135 to change (or decrease) from the fourth temperature (T 4 ) to a fifth temperature (Tj).
- the fifth temperature (T$) may be the same temperature as the first/third temperature (T t /T3 ⁇ 4) or a different temperature, as long as the fifth temperature (Ts) is lower than the fourth temperature (T 4 ).
- the cooling substance ⁇ Q2) having an inlet temperature (T4) mixes with the reactant stream, which flows from the second bed (82) to the third bed (B3).
- the cooling substance (Q2) performs an internal cooling function.
- the temperature in the reactor 135 may change (or increase) from the fifth temperature (T$) to a sixth temperature (Ts).
- the sixth temperature (Ts) may be the same temperature as the second/fourth temperature (T2/T4) or a different temperature, as long as the sixth temperature (Ts) is higher than the fifth temperature (T 5 ).
- the external cooling function may be Such as but not limited to a multi tube or a shallow bed reactor with a heat transfer unit.
- the shallow bed reactor works in combination with the heat transfer unit
- lhe external cooling function is a heat transfer unit (H i , H2) that may be added as an integral part of the reactor at an interface (denoted by a dotted line) of a bed and an adjacent bed.
- the interface may be between a first bed (Bl) and a second bed (B2) or between the second bed (B2) and a third bed (B3).
- the heat transfer Unit (HI , H2) is a shell and tube heat exchanger.
- the reactant stream from a bed may contact the heat transfer unit at an interface of the bed and an adjacent bed, such that die temperature of the reactant stream is decreased.
- the temperature of the reactant stream may increase because Of the reaction between the bio-based material and hydrogen.
- another heat transfer unit may be installed at an interface of the adjacent bed and another adjacent bed. The heat transfer unit may likewise lower the temperature of the reactant stream when the reactant stream contacts tile heat transfer unit Consequently, the temperature of the reactant stream may be controlled and maintained at a suitable temperature range.
- a coolant such as Cl, C2 in Figure 5 having a lower temperature (such as inlet temperature T q in Figure 5) than the temperature of the reactor may be introduced into the heat transfer unit, such as via the shell side of the heat transfer unit.
- the reactant stream which may pass through the tube side of the heat transfer unit will transfer heat energy to the coolant, thereby maintaining the temperature of the reactor at a suitable temperature.
- the exchanging of heat energy between die coolant and the reactant stream occurs without mixing ofthe reactant stream with the coolant.
- the coolant performs an external cooling function. Consequently, the temperature of the reactant stream will decrease and the temperature of the coolant will increase. As the temperature ofthe reactant stream decreases, the temperature of the reactor is maintained at a suitable temperature.
- Examples of the coolant include but are not limited to a fresh amount of the bio based material, a fresh amount of hydrogen, a portion of treated oil, or a combination thereof, or a heal transfer fluid.
- the portion of treated of! used as the coolant may be freshly prepared or prepared in a previous hatch.
- the coolant may be introduced into the apparatus for cooling the reactor in a single portion or more than one portion and may be dependent on the number of beds in the reactor.
- the volume of each portion of the coolant may be adjustable from 0 to 100 wt% of the total volume of coolant.
- the total volume of coolant may be dependent on the range of temperature to be controlled. For instance, if the temperature increase is relatively high (in other words, tins range of temperature to be controlled is relatively big), it may be necessary to use a greater volume of coolant
- the temperature in the reactor 135 may change (or increase) from a first temperature (Ti) to a second temperature (T3 ⁇ 4).
- the first temperature may be about 320°C and the second temperature may be about 380°C.
- the increase in temperature is because the reaction between the bio-based material and hydrogen is an exothermic reaction, thereby producing a significant amount of heat.
- the reactant stream may flow through a side (such as the tube side) of the heat transfer unit (H 1) which is located at the interface (denoted by a dotted line) between the first bed (Bl) and a second bed (B2), and coolant (Cl ) may be introduced into a side (such as the shell side) of the heat transfer unit ( H 1 ), such that the coolant (C 1 ) causes the temperature in the reactor 135 to change (or decrease) from the second temperature to a third temperature (T3).
- tile third temperature (Ti) may be the same temperature as the first temperature (Tt) or a different temperature, as long as the third temperature (T3) is lower than the second temperalure (T2).
- the coolant (Cl) having an initial temperature (Inlet temperature T ⁇ ,) would have a final temperature (outlet temperature T q l ), wherein the initial temperature is lower than the final temperature.
- the temperature in the reactor 135 may change (or increase) from tire third temperature (T3) to a fourth temperature
- the fourth temperature (Ta) may be the same temperature as the second temperature (T2) or a different temperature, as long as the fourth temperature (T4) is higher than the third temperalure (Ti).
- the reactant stream may flow through a side (such as the tube side) of a heat transfer unit (H2) which is located at the interface (denoted by a dotted fine) between the second bed (B2) and a third bed (B3), and coolant (C2) may be introduced into a side (such as the shell side) of the heat transfer unit (H2), such that the coolant (C2) causes foe temperature in the reactor 135 to change (or decrease) from the fourth temperature (I4) to a fifth temperature (Ts).
- a side such as the tube side
- coolant (C2) may be introduced into a side (such as the shell side) of the heat transfer unit (H2), such that the coolant (C2) causes foe temperature in the reactor 135 to change (or decrease) from the fourth temperature (I4) to a fifth temperature (Ts).
- the fifth temperature (Ts) may be the same temperature as the first/third temperature (T1/T 3 ) or a different temperature, as long as the fifth temperature (Ts) is lower than the fourth temperature (T4). Consequently, the coolant (C2) having an initial temperature (inlet temperature T q ) would have a final temperature (outlet temperature T q 1 ), wherein the initial temperature is lower than the final temperature.
- the sixth temperature (Ts) may be the same temperalure as the second/fourth temperature OVT4) or a different temperature, as long as the sixth temperature (Ts) is higher than the fifth temperature
- the treated oil can be further processed to form green diesel and/or a phase change material (PCM).
- the treated oil can be further processed to form an industrial solvent, in various embodiments, further processing of the treated oil to form green diesel, PCM and/or industrial solvent makes use of a combination of a distillation step and an adsorption step. It is appreciable that the ratio of treated oil that undergoes further processing to form green diesel to the PCM and the industrial solvent is from 1 :0 to 0: l .
- PCM portion* when used in the context of treated oil, refers to die proportion (or ratio) of treated oil that undergoes further processing to form PCM and the industrial solvent.
- the treated oil produced by the method of the present invention may contain a low volume of isoparaffins or a high volume of isoparaffins.
- Isoparaffins obtained from the method of the present invention may be substantially free of sulfur, olefins and aromatics, non-toxic and do not lead to the formation of harmful products during combustion.
- the term“substantially free” when used in the context of a byproduct e.g.
- sulfur, olefins, aromatics or a mixture thereof) in the treated oil refers to an amount of less than 100 parts per million by weight (ppmw), less than 50 ppmw, less than 20 ppmw, less than 10 ppmw, less than 5 ppmw or less than I ppmw in the treated oil.
- PCM may be substantially free of sulfur, aromatics and alcohols.
- the term “substantially free” when used in the context of a byproduct (e.g. sulfur, aromatics, alcohols or a mixture thereof) in PCM refers to an amount of less than 100 ppmw, less than 50 ppmw, less than 20 ppmw, less than 10 ppmw, less than 5 ppmw or less than 1 ppmw in foe PGM.
- a byproduct e.g. sulfur, aromatics, alcohols or a mixture thereof
- PCM obtained using foe treated oil may be substantially free of sulfur, aromatics and alcohols.
- a high volume of isoparaffins may be desired.
- foe heated oil may comprise a high volume of isoparaffins.
- foe catalyst used in the process of foe present invention may cause isomerization of foe bio-based material to occur, thereby producing a high volume of isoparaffins.
- prior art methods may require isomerization of the treated oil because foe treated oil may comprise essentially all n-paraffins, thereby having poor cold flow properties. As such, if it is desirable to improve the cold flow properties of the treated oil, foe treated oil obtained using prior art processes may require an additional step of isomerization.
- a low volume of isoparaffins may be desired. Generally, it is difficult if riot impossible to separate isoparaffin from normal paraffin (n-paraffin, n-Cl 5 to n-C18). If there is a high volume of isoparaffin in the treated oil, the resulting PCM would contain isoparaffin as an impurity and the purity of n-paraffin of the PCM would not reach 99 wt%. In various embodiments, the purity of n-paraffin of the PCM is about 99 wt%. In various embodiments, the PCM comprises at least 99 wt% of n-paraffin, wherein the n-paraffin may be at least one kind of n-paraffin. Consequently, die PCM is obtained in high purity and consists essentially of n-paraffin.
- the method further comprises passing the treated oil through a distillation unit and an adsorption unit to form green diesel.
- the distillation unit is coupled to the adsorption unit.
- the distillation unit is connected to the adsorption unit
- the quality of the green diesel is comparable or better than green diesel produced by prior art methods.
- the flash point of the green diesel of the present invention is relatively higher than foe flash point of green diesel produced by prior art methods. This may be because the treated oil is passed through the distillation unit
- the distillation unit comprises at least one distillation column.
- the green diesel may be obtained in a yield of about 80% to about 85% of the biobased material.
- the isoparaffin content in green diesel is in the range of about 0 wt% to about 10 wt% and the n-paraffin content in green diesel is in the range of about 90 wt% to about 1Q0 wt%.
- die treated oil for making green diesel passes through a distillation Unit (apparatus 139) followed by an adsorption unit (apparatus 140).
- stream 113 passes through apparatus 139, which may comprise a distillation tower operating at atmospheric pressure or under vacuum for separating out low boiling point hydrocarbon compounds (stream 1 16), so that the green diesel obtained may have a higher cetane number and lower volume of sulphur.
- the cetane number is at least 100.
- die green diesel obtained has a cetane number of about 100 to about 105.
- the green diesel of the present invention may have a relatively higher flash point compared tp prior art green diesel.
- the flash point of the green diesel of the present invention may be in the range of about 100°C to about 130°C, about 1 10°C to about 130°C, about 120°C to about 130°C, or about 12G°C to about 125°C.
- the product obtained from apparatus 139 is stream 115 » which is subsequently passed through apparatus 140, wherein apparatus 140 is adapted for eliminating sulphur and decreasing acidity of stream 115, thereby forming green diesel (stream 117).
- the adsorption unit comprises at least one adsorbent selected from the group consisting Of activated carbon, ion exchange resin, molecular sieve and chemical adsorbent.
- the ion exchange resin may be a basic ion exchange resin or an acidic ion exchange resin.
- the adsorbent is a basic ionic exchange resin.
- the chemical adsorbent may he basic or acidic, preferably basic.
- the adsorption unit may eliminate contaminants Which may affect the efficiency of the catalyst
- the resultant green diesel may have desirable properties such as a lower amount or a negligible amount of contaminants such as but not limited to sulphur, an oxygen-containing compound, a triglyceride and/or acid.
- the resultant green diesel may be substantially free of oxygeii-containing compounds, substantially free of a heavy fraction (such as triglycerides dr heavy paraffin content having more than 20 carbon atoms) or substantially free of both.
- the term“substantially free” when used in the context of a byproduct e.g.
- At least one oxygen-containing compound, at least one heavy fraction or a mixture thereof) in green diesel refers to an amount of less than 1 wt%, less than 0.8 wt%, less than 0.6 wt%, less than 0.5 wt%, less than 0.4 wt%, less than 0.3 wt%, less than 0.2 wt%, less than 0.1 wl%, less than 0.05 wt%, or less titan 0.01 wt% in the green diesel. Consequently, the green diesel may have a relatively narrow distillation range and trace amount of impurities, tit various embodiments, the total glyceride content in the green diesel is equivalent to the triglyceride content in the green diesel.
- the total glyceride content in the treated oil is equivalent to tire total glyceride content in the green diesel. It would be understood by a person skilled in the aft that standard tests such as EN 14105 may be used to measure the total glyceride content. In various embodiments, there is less than 1 wt%, less than 0.8 wt%, less than 0.6 wt%, 1MS than 0.5 wt%, less than 0.4 wt%, less titan 0.3 wt%, less than 0.2 wt%, less than 0.1 wt%, or less than 0.05 wt% of total glycerides in the green diesel. In various embodiments, there is about O.OI wt% to about 0,05 wt% of total glycerides in the green diesel, in various embodiments, there is about 0.038 wt% of total glycerides in the green diesel.
- the method of the present invention does not require any additional step(s) to separate unreacted triglycerides, whereby each additional step may be a complicated process that requires a significant amount of energy or relatively high energy so that the removal of the unreacted triglycerides can he carried out
- each additional step may be a complicated process that requires a significant amount of energy or relatively high energy so that the removal of the unreacted triglycerides can he carried out
- the green diesel of the present invention is substantially tree of oxygen-containing compounds » oxidation of the green diesel of the present invention may be reduced or prevented. As such, good thermal oxidation stability may be achieved.
- the adsorption unit may be a column (or an adsorption column) or a set of columns (or adsorption columns). In various embodiments, more than one adsorption unit may be used.
- the adsorption of contaminants such as but not limited to heavy metals, sulphur compounds and acids from the treated oil may proceed at atmospheric pressure, at a temperature of about 30°C to about 70°C and a space velocity of about 0.5 h "1 to 2.0 hr*.
- the temperature of the adsorption unit does not need to be adjusted, thereby leading to ease of operation.
- the temperature of the adsorption unit may be selected based on the temperature of the bio-based material or the treated oil.
- the method further comprises passing the treated oil through at least one distillation column to separate the treated oil into at least one component.
- more than one distillation columns may be coupled to each other.
- the method further comprises the step of distillation, in particular but not limited to, vacuum distillation, in various embodiments, the distillation column may comprise at least one packed column or at least ppe tray column. In an embodiment, there may be four distillation columns.
- the distillation column may be part of a distillation unit, in other words, the distillation unit may comprise at least one distillation column and other components.
- the distillation may be carried out in batch mode or continuous mode. In various embodiments, the distillation may occur at a pressure of about 5 milliter (mter) to about 100 mbar. In various embodiments, the temperature at the top of the distillation column may be about 120°C to about 190°C, while the temperature in the reboiler may be about 170°C to about 230°C ⁇
- PCM may be obtained and possess desirable characteristics such as being odor-less. In other words, the scent of the PCM may be eliminated.
- the PCM of the present invention may have comparable or better purity, a different range of melting temperature and1 ⁇ 2 a different heat storage capacify Or heat of fusion.
- die PCM may be obtained in a yield of about 60% to about 80% of PCM portion in the treated oil (or treated oil feed), in various embodiments, the isoparaffin content in PCM is in the range of about 0 wt% to about 1 wt% and the n-paraffin content in PCM is in the range of about 99 wt% to about 100 wt%.
- the at least one component is selected from the group consisting of n-paraffin having less than 16 carbon atoms, n-hexadecane (n-Cl 6), n-heptadecane (n-Cl7), n-oeiadecane (n-C18) and n-paraffin having more than 18 carbon atoms.
- the at least one component may be an industrial solvent.
- the purity of the at least one component is high.
- the industrial solvent may have high purity because it comprises at least 99 wt% n-paraffins. Consequently, the industrial solvent may predominantly contain n-paraffins and therefore have good oxidation thermal stability.
- the industrial solvent consists essentially of n-paraffin, wherein the n- paraffln may be at least one kind of n-paraffin.
- the industrial solvent obtained from the method bf the present invention may comprise less than l ppm of sulphur an d less than I wt% or negligible (not detectable via analytical methods) aromatic compounds (or aromatic content).
- the industrial solvent may contain less than or equal to 50 parts per million by weight (ppmw) of water.
- commercially available green diesels may have a significantly higher amount of water, such as 2,000 ppmw of water.
- the industrial solvent of the present invention may have other features such as but not limited to: relatively high flash point, relatively narrow distillation range, tow viscosity, mild colour, mild odour, low density, non-polar, and low reactivity.
- the industrial solvent may be a non-flammable liquid because it has a relatively high flash point.
- the flash point of the industrial solvent may be about 120°C to about 130°C.
- the distillation range of the industrial solvent is in the range of about 240°C to about 280"C or about 250°C to about 270°C.
- the IBP of the industrial solvent is at least 240°C or at least 250°C
- the FBP of the industrial solvent is at most 280°C or at most 270°C,
- PCM (stream 1 14, wherein die composition of stream 112 is identical to stream 114) passes through a distillation column (apparatus 142), thereby separadrig stream 120 which contains n- paraffin having less than 16 carbons and stream 1 19.
- Stream 119 then passes through another distillation column (apparatus 144), thereby separating stream 123 which contains n-hexadecane as a main component of at least about 99.0 percent by mass and stream 122.
- Stream 122 then passes through another distillation column (apparatus 146), thereby separating stream 126, which contains n-heptadecane as a main component of at least about 99.0 percent by mess and stream 125.
- Stream 125 then passes through another distillation column (apparatus 148), thereby separating stream 129 which contains n-octadecane as a main component of at least about 99.0 percent by mass and stream 128, which contains n-paraffin having more titan 18 carbon atoms as a main component.
- stream 128 may exit from the bottom of distillation column (apparatus 148) and used as a fuel oil (bunker oil). Accordingly, more than one distillation columns may be coupled to each other.
- the fuel oil may be used for various applications such as but not limited to fuel for mobile engines.
- the method further comprises passing the at least one component through an adsorption unit.
- the distillation column is coupled to the adsorption unit.
- the distillation column is connected to the adsorption unit.
- the adsorption unit may improve the quality of the at least one component by eliminating any remaining contaminants, thereby making it suitable for a desired use, such as but not limited to an industrial solvent or a PCM. Removal of the contaminants, such as but not limited to undesired volatile organic compounds, substances that may impart a bad odour or colour to the industrial solvent and/or the PCM, may minimize or eliminate undesirable characteristics of the industrial solvent or the PCM, Such as but not limited to a had odour or an undesired colour.
- the adsorption unit comprises at least one adsorption column, each adsorption column may comprise at least one adsorbent selected from the group consisting of activated carbon, ion exchange resin, molecular sieve and chemical adsorbent.
- the ion exchange resin may be a basic ion exchange resin or an acidic ion exchange resin
- the molecular sieve may have a pore size ranging from about 3 angstrom (A) to about 15 A.
- the ehernica! adsorbent may be bade or acidic, preferably basic.
- the adsorption may proceed at atmospheric pressure, at a temperature of about 30°C to about 70°C and a space velocity of about 0.5 h' 1 to 2.0 h *1 .
- the temperature of the adsorption unit does not need to be adjusted, thereby leading to ease of operation.
- the temperature of the adsorption unit may be selected based on the temperature of the input stream, such as but not limited to stream 120, stream 123, stream 126 and stream 129; [00140] In various embodiments mid as illustrated in Figure 2, stream 120 passes through an adsorption unit (apparatus 143) to form stream 121 , which is suitable to be an industrial solvent.
- stream 123 passes through an adsorption unit (apparatus 145) td form stream 124, which is suitable to be a PCM (PCM #1).
- PCM PCM #1
- stream 126 passes through an adsorption unit (apparatus 147) to form stream 127, which is suitable to be a PCM (PCM #2).
- stream 129 passes through an adsorption unit (apparatus 149) to form stream 130, which is suitable to be a PCM (PCM #3).
- green diesel obtainab le by the method described above, wherein the green diesel comprises isoparaffin in an amount of 0 to 10 wt3 ⁇ 4 and n-paraffin in an amount of 90 to 100 wt%.
- the distillation range of the green diesel is relatively narrow. In various embodiments, the distillation range of the green diesel is in the range of about 200% to about 350%, about 250% to about 330°C, about 255% to about 330% about 255°C to about 325°C, about 260% to about 325% about 260% to about 330% about 250% to about 323% or about 260°C to about 323%. In various embodiments, the initial boiling point (IBP) of the green diesel is in the range of about 200% to about 350% preferably about 250% to about 310% about 250% to about 270% about 255°G to about 265% In various embodiments, the IBP is at least 250% at least 255% or at least 260%.
- the IBP of the green diesel of the present invention may be relatively higher. Ih various embodiments, the IBP of the greet) diesel of the present invention may be about 260.5% whereas the IBP of a first commercially available green diesel is 180%, while the IBP of a second commercially available green diesel is 173%. Consequently, this shows that the green diesel of the present invention has a higher composition (or proportion) of normal paraffin having high carbon atoms (such as n-Cl 5 to n-Cl8) than commercially available green diesels.
- the final boiling point (FBP) of the green diesel is lower than commercially available green diesels.
- the FBP is at most 350% at most 340%, at most 335%, at most 330% or at most 325%.
- the FBP of the green diesel of the present invention is about 323.0%, whereas the FBP of the first commercially available green diesel is 360% while the boiling point of a third commercially available green diesel is from 350%. Consequently, when the green diesel of the present invention is used (or combusted), the amount of pollution generated is relatively lower than commercially available green diesels. For example, less small particles are generated from combustion of the green diesel of the present Invention.
- phase change material obtainable by the method described above, wherein the phase change material comprises isoparaffin in an amount of 0 to l wt% and n-paraffin in an amount of 99 to 100 wl%.
- a system for processing a bio-based material comprising a reactor 135 for reacting the bio-based material (stream 101 ) with hydrogen (stream 104) in the presence of a catalyst on a support to form a treated oil (stream 109); wherein the bio-based material (stream 101) is renewable; and wherein the reactor 135 comprises a cooling function for controlling the temperature of the reactor; wherein the cooling function is at least one of an internal cooling function mid an external cooling function.
- the internal cooling function may comprise a cooling substance, wherein the cooling substance may be a fresh amount of the bio-based material, a fresh amount of hydrogen, and/or a portion of the treated oil.
- the system further comprises a high-pressure separator (apparatus 137) and a low-pressure separator (apparatus 138) for passing the treated oil (stream 109) through, in various embodiments, the reactor 135 is coupled to the high-pressure separator (apparatus 137).
- the reactor 135 is connected to a heat exchanger (apparatus 136) and the heat exchanger (apparatus 136) is connected to a high-pressure separator (apparatus 137).
- the high-pressure separator (apparatus 137) is coupled to the low-pressure separator (apparatus 138).
- the high-pressure separator (apparatus 137) is connected to the low-pressure separator (apparatus 138).
- the external cooling function comprises a multi tube or a shallow bed reactor or a heat transfer unit.
- the external cooling function further comprises a coolant, wherein foe coolant may be a fresh amount of the bio-based material, a fresh amount of hydrogen, and/or a portion of the treated oil, or a heat transfer fluid.
- foe coolant may be a fresh amount of the bio-based material, a fresh amount of hydrogen, and/or a portion of the treated oil, or a heat transfer fluid.
- the system further comprises a distillation unit (apparatus 139) for passing the treated oil (stream 113) through to form green diesel (stream 117).
- the distillation unit (apparatus 139) is coupled to the low-pressure separator (apparatus 138).
- the low-pressure separator apparatus 138
- foe distillation unit (apparatus 139) is connected to the low-pressure separator (apparatus 138).
- the system further comprises an adsorption unit (apparatus 140) for passing the green diesel (stream 117) through-
- the adsorption unit (apparatus 140) is coupled to the distillation unit (apparatus 139).
- the adsorption unit (apparatus 140) is connected to the distillation unit (apparatus 139).
- the system further comprises at least one distillation column (such as apparatus 142, apparatus 144, apparatus 146, apparatus 148) to separate the treated oil into at least one component
- at least one distillation column such as apparatus 142
- one of the at least one distillation column is coupled to the low-pressure separator (apparatus 138).
- the distillation column (apparatus 142) is connected to the low- pressure separator (apparatus 138).
- the system further comprises an adsorption column (such as apparatus 143. apparatus 145, apparatus 147, apparatus 149) for passing the at least one component through.
- the adsorption column may be part of an adsorption unit
- the adsorption column (such as apparatus 143) is coupled to the distillation column (such as apparatus 142).
- the adsorption column (apparatus 143) is connected to the distillation column (apparatus 142)
- the adsorption column (apparatus 145) is connected to the distillation column (apparatus 144)
- the adsorption column (apparatus 147) is connected to the distillation column (apparatus 146)
- the adsorption column (apparatus 148) is connected to the distillation column (apparatus 148).
- the method of processing a renewable bio-based material comprises the step of reacting the bio-based material with hydrogen in the presence of a catalyst on a support in a reactor to form a treated oil; (i) passing the treated oil through a distillation unit and an adsorption unit to form green diesel; and/or (ii) passing the treated oil through at least one distillation column to separate the treated oil into at least one component and passing the at least one component through an adsorption column; and wherein the reactor comprises a cooling function for controlling the temperature of the reactor; wherein the cooling function is at least one of an internal cooling function and an external cooling function.
- a bio-baaed material may be passed through a pump (apparatus 131), wherein apparatus 131 is adapted to control die flow rate and pressure df the bio-based material.
- apparatus 131 is adapted to control die flow rate and pressure df the bio-based material.
- stream 102 is formed, wherein streadi 102 comprises the bio-based material having a predetermined flow rate and pressure, and wherein the pressure of stream 102 is higher than the pressure of stream ID l .
- Stream 102 then passes through a heat exchanger (apparatus 132), wherein apparatus 132 is adapted to increase the temperature of stream 102, thereby forming stream 103 which comprises the bio-based material having a predetermined temperature, wherein the temperature of stream 103 is higher than the provided a system for processing a bio-based material comprising a reactor 135 for reacting the hio-hased material (stream 101) with hydrogen (stream 104) in the presence of a catalyst on a support to form a treated oil (stream 109); wherein die biobased material (stream 101) is renewable; and wherein the reactor 135 comprises a cooling function for controlling the temperature of the reactor, wherein the cooling function is at least one of an internal cooling function and an external cooling function.
- apparatus 132 is adapted to increase the temperature of stream 102, thereby forming stream 103 which comprises the bio-based material having a predetermined temperature, wherein the temperature of stream 103 is higher than the provided a system for processing a bio-based material comprising a reactor 135 for react
- stream 106 may react by contacting the surface of the catalyst in the reactor, thereby producing a treated oil (stream 107).
- stream 107 then passes through a heat exchanger (apparatus 136) followed by a high-pressure separator (apparatus 137) and a low- pressUre separator (apparatus 138).
- the method illustrated in Figure 1 is identical to the method illustrated in Figure 3, except that the separation point of the treated oil is moved such that the separation point is after the distillation unit (apparatus 139) instead of after the low pressure separator (apparatus 138).
- a purified treated oil (stream 109) and a gaseous component (stream 110) arc formed, in various embodiments, after the purified treated oil (stream 109) passes through apparatus 139, low boiling point hydrocarbon compounds (stream 116) are separated out.
- PCM passes through a distillation column (apparatus 142), thereby separating stream 120 which contains n-paraftin having less than 16 carbons and stream 119.
- Stream 119 then passes through another distillation column (apparatus 144), thereby separating stream 123 which contains n- hexadecane as a main component of at least about 99.0 percent by mass and stream 122.
- Stream 122 then passes through another distillation column (apparatus 146), thereby separating stream 126, which contains n-heptadecane as a main component of at least about 99.0 percent by mass and stream 125.
- stream 125 then passes through another distillation column (apparatus 148), thereby separating stream 129 which contains n-oc tadecane as a main component of at least about 99.0 percent by mass and stream 128, which contains n-paraftin having more than 18 carbon atoms as a main component, in various embodiments, stream 128 may exit from the bo ttom of distillation column (apparatus 148) and used as a fuel oil (banker oil).
- stream 1:20 passes through an adsorption unit (apparatus 143) to form stream 121, which is suitable to be an industrial solvent
- stream 123 passes through an adsorption unit (apparatus 145) to form stream 124, which is suitable to be a PCM (PCM #1 ).
- stream 126 passes through an adsorption unit (apparatus 147) to form stream 127, which is suitable to be a PCM (PCM #2).
- stream 129 passes through an adsorption unit (apparatus 149) to form stream 130, which is suitable to be a PCM (PCM #3).
- PCM #1, PCM #2, PCM #3 obtained from the alternative method illustrated in Figure 3 is identical to the corresponding PCM (PCM #1, PCM #2, PCM #3) obtained from the method illustrated in Figure 2.
- the purified treated oil may pass through an adsorption unit (apparatus 140).
- apparatus 140 is adapted for eliminating sulphur and decreasing acidity of stream 115, thereby forming green diesel (stream 117). It would be understood by a person skilled in the ait that the green diesel obtained from the method illustrated in Figure 3 is identical to tire green diesel obtained from the method illustrated in Figure 1 ,
- a system for processing a bio-based material comprising a reactor 135 for reacting the bio-based material (stream 101) with hydrogen (stream 104) in the presence of a catalyst on a support to form a treated oil (stream 109); wherein the bio-hased material (stream 101) is renewable; and wherein tire reactor 135 comprises a cooling function for controlling the temperature of the reactor; wherein the cooling function is at least one of an internal cooling function and an external cooling function.
- the system further comprises a high-pressure separator (apparatus 137) and a low-pressure separator (apparatus 138) for passing the treated oil (stream 109) through.
- the reactor 135 is coupled to the high-pressure separator (apparatus 137).
- the reactor 135 is connected to a heat exchanger (apparatus 136) and the heat exchanger (apparatus 136) is connected to a high-pressure separator (apparatus 137).
- die high-pressure separator (apparatus 137) is coupled to tile low- pressure separator (apparatus 138).
- the high-pressure separator (apparatus 137) is connected to the low-pressure separator (apparatus 138).
- the system further comprises a distillation unit (apparatus 137).
- the distillation unit (apparatus 139) for passing the heated oil (stream 113) through.
- the distillation unit (apparatus 139) is coupled to die low-pressure separator (apparatus 138).
- the distillation unit (apparatus 139) is connected to the low-pressure separator (apparatus 138).
- the system further comprises an adsorption unit (apparatus 140) for passing the green diesel (stream 117) through.
- the system further comprises at least one distillation column (such as apparatus 142, apparatus 144, apparatus 146, apparatus 148) to separate the treated oil into at least one component.
- the adsorption unit (apparatus 140) is coupled to the distillation unit (apparatus 139).
- the adsorption unit (apparatus 140) is connected to the distillation unit (apparatus 139).
- one of the at least one distillation column (such as apparatus 142) is coupled to the distillation unit (apparatus 139).
- the distillation column (apparatus 142) is connected to the distillation unit (apparatus 139).
- the system further comprises an adsorption column (such as apparatus 143, apparatus 145, apparatus 147, apparatus 149) for passing the at least one component through.
- the adsorption column may be part of an adsorption unit.
- the adsorption column (such as apparatus 143) is coupled to the distillation column (such as apparatus 142).
- the adsorption column (apparatus 143) is connected to the distillation column (apparatus 142), the adsorption column (apparatus 145) is connected to the distillation column (apparatus 144), the adsorption column (apparatus 147) is connected to the distillation column (apparatus 146), and the adsorption column (apparatus 148) is connected to the distillation column (apparatus 148).
- Example 1 [00174$ Different catalysts on an acidic porous solid support were used and the effeets/results obtained are shown in Table L
- a method in accordance with embodiments of the present invention was carded out using palm Olein as feedstock, hydrogen and the catalyst used was NiMo on AI2O3, to prepare treated oil.
- the temperature of the reactor was varied from 300°C to 360°C at a pressure of 30 70 bars, space velocity was 1.0 hf 1 and ratio of hydrogen gas to palm olein was 0.06 g hydrogen/g oil
- Example 4 Another method in accordance with embodiments of the present invention was carried out to illustrate the effect of using different catalysts, such as NiMo/AhOj and NiCoMo/AkQ ⁇ , in the method of preparing a treated oil
- the temperature of the reactor was 330°C at a pressure of 35 bars, space velocity was 1.0 hr 1 and ratio of hydrogen to palm olein was 0.06 g hydrogen/g oil.
- the properties of the obtained treated oil are shown in Table 4.
- the NiCoMa/AbQ j catalyst will cause an isomerization reaction, which will convert linear-chain paraffin products to branched-chain paraffin products, as reflected by the cloud point of the products.
- linear-chain paraffin products have the same number of carbon atoms as branched-chain paraffin products
- branched-chain paraffin products will have a lower melting point than linear-chain paraffin products. Therefore, a higher amount of branched-chain paraffins will lead to a decrease to the cloud point of the resultant green diesel.
- $01811 " Hie results in Table 4 also show that the amount of branched-chain paraffins in the products prepared using the NiMo/AbQj catalyst is lower than the products obtained from the
- NiCoMo/AhO l catalyst which means that the treated oil obtained using the NiMo/AhOs catalyst is more suitable for PCM production.
- a method in accordance with some embodiments of the present invention was carried out using palm olein as feedstock, hydrogen and the catalyst used was NtMb on AI2G3, to prepare treated oil suitable for preparing a PCM.
- the temperature of the reactor was 330°C at a pressure of 35 bars, space velocity was l .0 hr 1 and ratio of hydrogen to palm olein was 0.06 g hydrogen/g oil.
- the treated oil was passed through a method of separation to remove undesired by* products and gases. Subsequently, the treated oil was introduced into a vacuum distillation tower in accordance with embodiments of the present invention.
- a method in accordance with embodiments of the present invention was carried out using various bio-based material as feedstock, hydrogen and the catalyst used was N iMo on AI2O3, to prepare treated oil suitable for preparing green diesel.
- the temperature of the reactor was 350°C at a pressure of 35 bare, space velocity was 1.0 hr "1 and ratio of hydrogen to bfe-based material was 0.06 g bydrogen/g bio-based material.
- a method in accordance with embodiments ofthe present invention was tamed out tb farther process treated Oil from Example 4 to form PGM and an industrial solvent NiMo/AbO ? was used as the catalyst and the method is identical to that illustrated in Figures 1 and 2. Consequently, an industrial solvent (GTR1) and three different FCMs (PCM #01, #02, #03) (stream .121, 124, 127 and 130 respectively) were made.
- GTR1 industrial solvent
- PCM #01, #02, #03 three different FCMs
- PCM #01 * #02, #03 obtained from the method of die present invention.
- the characteristics of PGM #01 , #02, #03 are shown in Table 7.
- PCM #01 , #02, #03 were obtained with high purity of at least 99% by weight, as analysed by Gas Chromatography - Flame Ionization Detector (GC-FtD).
- GC-FtD Gas Chromatography - Flame Ionization Detector
- die commercially available PGM has a purity of about 89% to about 94%. Consequently, die commercially available PGM had a purity of about 5% to about 10% less than the PCMs obtained in the present invention.
- PCM #01, #02, #03 and GTRI are shown in Table 9, As illustrated in Table 9, GTR1 is a n-paraffin having 15 carbons (n-C15), PCM #01 is a n-paraffin having 16 carbons (tv Cl 6), PCM #02 is a n-paraffin having 17 carbons (n-C17) and PCM #03 is a n-paraffin having 18 carbons (n-CI8). Table 9: Chemical structures of PCM #01, #02, #03 and GTRI made using the method of the present invention
- IP01B23 11 ⁇ 2 distillation range of a green diesel obtained from the method of the present invention is shown in Table 10.
- the treated oil obtained from Example 4 was used. wherein NiCoMo/AbOj was used as the catalyst and the treated oil was passed through a distillation unit (apparatus 139) followed by an adsorption column (apparatus 140).
- the distillation range of the green diesel is in the range of about 200°C to about 350°C > in particular about 260.5°C to about 323.0 P C.
- the IBP of the green diesel of the present invention 1 relatively higher. Specifically, the IBP of the green diesel of die present invention is 260.5°C.
- the EBP of a first commercially available green diesel is 180°C
- the IBP of a second commercially available green diesel 1 ⁇ 2 173°C. Consequently, this shows that the green diesel of the present invention has a higher composition (or proportion) of normal paraffin having high carbon atoms (such as n-Cl5 to n-Cl8) than the commercially available green diesels.
- the final boiling point (FBP) of the green diesel of the present invention is lower titan commercially available green diesels.
- the FBP of the green diesel of the present invention is 323.0°C
- the FBP of the first commercially available green diesel is 36tPC
- the boiling point of a third commercially available green diesel is from 350 6 C. Consequently, when the green diesel of the present invention is used (or combusted), the amount of pollution generated is relatively lower titan commercially available green diesels. For example, lei® small particles are generated from combustion of the green diesel of the present invention.
- the green diesel of the present invention is substantially free of oxygen- containing compounds (i.e. no oxygen-containing compounds).
- commercially available green diesels may contain oxygen-containing compounds. Due to the absence of oxygen- containing compounds, oxidation of the green diesel of Re present invention may be reduced or prevented. As such, good thermal oxidation stability is achieved. Consequently, the green diesel of the present invention has a long-lasting quality and long-term storage. For instance, the great diesel of the present invention has an oxidation stability of 35 hours according to EN 15751.
- additives such as antioxidants are not required to increase the shelf life of the green diesel of the present invention.
- the information regarding the series of aliphatic mineral spirits A1 to A7 is based on the technical datasheets prepared by ShellTM and the test methods are as follows: American Society for Testing and Materials (ASTM) D56 was used to measure the flash point of A1 to A3, ASTM D93 was used to measure the flash point of A4 to A7* ASTM 1 ) 4052 was used to measure the density of A1 to A7, gas chromatography (GC) was used to measure die aromatic content and the sulfur content of A1 to A3, Shell Method Series (SMS) 2728 was used to measure the aromatic content of A4 to A7, international Organization for Standards (ISO) 20846 was used to measure the sulfur content of A4 to A7, ASTM Dk6 was used to measure the distillation range of A I to A7.
- ASTM Dk6 was used to measure the distillation range of A I to A7.
- Aliphatic mineral spirits are products of petroleum refinery and are produced by (i) fractionation and hydrogenation of petroleum feedstock such as virgin naphtha and full range naphtha, or (ti) fischer-tropsch process of natural gas feedstock. They are low- viscosity solvents and have low aromatic content
- an industrial solvent of the present invention such as
- GTR1 has several advantages over the series of aliphatic mineral spirits, namely, Al to A7.
- the Hash point of GTRI is significantly higher than that of Al to A7. Due to the production process and nature of the feedstock, aliphatic mineral spirits contain tighter hydrocarbon compounds, thereby causing the flash point to be lower than that of GTR 1 , A higher flash point allows GTRI to be rendered a non-flammable liquid. In general, any liquid that has a flashpoint below 93°C is considered a flammable liquid.
- the distillation range of the industrial solvent of foe present invention such as GTR I is significantly narrower than that of the aliphatic mineral spirits. This is because GTRI predominantly contains n-CI5 and smaller amount of lighter ends (or light traction).
- the aromatic content of the industrial sol vent of the present invention such as Gt ' Rl is lower than that of the aliphatic mineral spirits ( «1 ppm vs ⁇ 200ppm). This is caused by foe fact that petroleum feedstock usually contains a considerable amount of aromatics and the hydrogenation unit (a step in the process whereby aromatics are converted into atiphatics) always leaves trace amount of aromatics in the aliphatic mineral spirits.
- the method of the present invention allows for usage of aromatic-free feedstock because a bio-based material is used as the feedstock instead. Therefore, the presence of aromatic contents in the desired products has been avoided intrinsically.
- Thermal oxidation stability of foe industrial solvent of the present invention such as GTR1 is also superior when compared to the series of aliphatic mineral spirits.
- Good thermal oxidation stability of GTR1 is achieved because GTRt predominantly contains n-paraffins as a primary component. N-paraffins are more resilient to oxidation reactions compared to aliphatic compounds. This characteristic is of utmost importance if the industrial solvent is going to be used for an extended period of time.
- the industrial solvent has better thermal oxidation stability, it is more resilient to the environment and can keep or maintain its properties within an acceptable limit for a longer period of time. Consequently, the industrial solvent of the present invention has a long-lasting quality and long-term storage.
- An example of a biomass-derived industrial solvent is a triglyceride-derived solvent.
- Triglyceride-derived solvents can be categorized as fatty acid methyl esters (FAME) and glycerol -derived solvents.
- FAME can be produced by either (i) transesterification of triglycerides or (H) esterification of fatty acids. Comparing an industrial solvent of die present invention, such as GTRl of Example 7, with FAME, although F AME has been widely used as a biofuel, its Usage as an industrial solvent has been limited due to its poor properties.
- Cargill’s Agri-PureTM AP-406 (AH) is an example of a FAME solvent derived from vegetable oil.
- FAME has a low amount of aromatics, a low amount of sulfur, and a high flash point
- an industrial solvent of the present invention such as GTR1 in Example 7.
- FAME has an ester functional group whereas an industrial solvent Of the present invention, such as GTRl, contains predominantly n-paraffins. Consequently* properties such as thermal oxidation stability, viscosity and colour are different between an industrial solvent of die present invention and FAME.
- an industrial solvent of the present invention has good thermal oxidation stability because it predominantly contains n ⁇ paraffin.
- FAME can be produced by transesterification of triglycerides.
- Glycerol is an important byproduct when transesterification of triglycerides is used for FAME production. Due to its nature of being a highly functionalized compound, glycerol can be converted into many kinds of solvents. In particular, the presence of hired (3) hydroxyl groups in glycerol allows each of the three hydroxyl groups to be functionalized independently of each other.
- industrial solvents that can be derived from glycerol include but are not limited to triacetin (A9), glycerol formal (A 10), 1-3 propanediol, 1, 3 -dmrethoxypropan-2-oi, 1, 2, 3- trimethoxypropane, so!ketal and glycerol carbonate (AI 1 ).
- Lignin is a biomass that mainly comprises of phenolic polymers and can be processed into an industrial solvent by either hydrpgenolysis or pyrolysis. These processes can convert lignin into phenolic compounds. As such, when comparing an industrial solvent of the present invention, such as GTR1 from Example 7, with typical lignin-derived solvents, Iignin- derived solvents predominantly comprises aromatic compounds. Therefore, application and properties of lignin-derived solvents are drastically different from GTRl .
- LOME lignin pyrolysis oil methyl ester
- ft is the only product derived from lignin that is not an aromatic compound.
- An example of a heterocyclic acetal dial cap be produced from lignin is 1, 3-dioxilane.
Abstract
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MYPI2020003336A MY195388A (en) | 2018-04-30 | 2019-04-30 | Method Of Processing A Bio-Based Material And Apparatus For Processing The Same |
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JP2020537007A JP2021518859A (en) | 2018-04-30 | 2019-04-30 | Bio-based material processing method and equipment for processing it |
RU2020125852A RU2020125852A (en) | 2018-04-30 | 2019-04-30 | METHOD AND DEVICE FOR PROCESSING MATERIAL OBTAINED FROM BIOS |
CN201980009525.2A CN111630136A (en) | 2018-04-30 | 2019-04-30 | Method for treating bio-based materials and apparatus for treating said bio-based materials |
EP19730980.0A EP3746523A1 (en) | 2018-04-30 | 2019-04-30 | Method of processing a bio-based material and apparatus for processing the same |
KR1020207022309A KR20200100838A (en) | 2018-04-30 | 2019-04-30 | Bio-based material processing method and apparatus for processing the same |
US16/960,066 US11674096B2 (en) | 2018-04-30 | 2019-04-30 | Method of processing a bio-based material and apparatus for processing the same |
BR112020017866-7A BR112020017866A2 (en) | 2018-04-30 | 2019-04-30 | METHOD OF PROCESSING A BIOLOGICAL BASED MATERIAL AND APPARATUS TO PROCESS THE SAME |
KR1020227028731A KR20220123553A (en) | 2018-04-30 | 2019-04-30 | Method of processing a bio-based material and apparatus for processing the same |
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PH12020551011A PH12020551011A1 (en) | 2018-04-30 | 2020-06-27 | Method of processing a bio-based material and apparatus for processing the same |
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