WO2009089591A1 - Système et appareil de fabrication de biodiesel - Google Patents

Système et appareil de fabrication de biodiesel Download PDF

Info

Publication number
WO2009089591A1
WO2009089591A1 PCT/AU2009/000051 AU2009000051W WO2009089591A1 WO 2009089591 A1 WO2009089591 A1 WO 2009089591A1 AU 2009000051 W AU2009000051 W AU 2009000051W WO 2009089591 A1 WO2009089591 A1 WO 2009089591A1
Authority
WO
WIPO (PCT)
Prior art keywords
manufacturing plant
container
biodiesel
oil
biodiesel manufacturing
Prior art date
Application number
PCT/AU2009/000051
Other languages
English (en)
Inventor
Sandy Kelly
Laurence Baum
Original Assignee
The Biofuel Partnership Limited
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from AU2008900210A external-priority patent/AU2008900210A0/en
Application filed by The Biofuel Partnership Limited filed Critical The Biofuel Partnership Limited
Priority to CN200980110110.0A priority Critical patent/CN101978027B/zh
Priority to AU2009204648A priority patent/AU2009204648B2/en
Publication of WO2009089591A1 publication Critical patent/WO2009089591A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—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
    • C—CHEMISTRY; METALLURGY
    • 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
    • C—CHEMISTRY; METALLURGY
    • 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
    • C11C3/003—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fatty acids with alcohols
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00592—Controlling the pH
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • 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
    • 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 alternative and sustainable fuel sources and particularly to a system and apparatus for the production of biodiesel.
  • Biodiesel refers to a diesel-equivalent processed fuel consisting of short chain alkyl (methyl or ethyl) esters, made by transesterification of vegetable oils or animal fats, which can be used (alone, or blended with conventional diesel fuel) in unmodified diesel-engine vehicles.
  • the present invention is directed to a biodiesel manufacturing system and apparatus, which may at least partially overcome at least one of the abovementioned disadvantages or provide the consumer with a useful or commercial choice.
  • the present invention in one form, resides broadly in a biodiesel manufacturing plant including a housing containing a power generation means, an oil expeller for mulching raw feedstock to extract raw oil from the feedstock, a mixer/reaction vessel in which the raw oil is mixed with a catalyst material and at least one separation means to separate methyl ester from other products.
  • the manufacturing plant of the present invention can take in most oil- bearing fruit — jatropha, palm, rapeseed, and the like — and process it to produce biodiesel fuel to the required European Standard. This means that the output of the plant can go straight into the tank of a modern diesel engine without modifying its settings.
  • the process undertaken will typically be alcoholysis (often referred to as transesterification) according to the general reaction illustrated in Figure 1.
  • the output is ideal for smaller communities which want to use the fuel themselves. It is particularly suitable for a 100-hectare plantation, with production ranges between 1500 and 2000 litres per day - and the cost is a fraction of the rates normally charged for mineral diesel fuels.
  • the housing is preferably a container, normally a shipping container or the like.
  • the container will typically be divided into a number of compartments in order to house particular components of the manufacturing plant. According to the preferred embodiment, the container will normally be divided into two compartments, the larger being approximately double the size of the smaller, thus delineating the hazardous area and separating it from the hot area.
  • the housing will preferably be rectangular and defined by a base wall, a plurality of sidewalls and a top wall. It is preferred that the housing has a non- corroding weatherproof tropical-grade shell. A particularly preferred material of construction for the housing is a relatively heavy duty plastic.
  • the housing is preferably fully sealable from the environment, but will normally be provided with at least some ventilation openings. It is preferred that ventilation driven by natural air flows is used. In order to provide such ventilation, openings may be provided in the base wall or a lower portion of the sidewalls in order to allow the escape of heavier than air gases.
  • the housing is preferably also provided with lateral openings and events in upper regions in order to allow the escape of lighter than air gases.
  • the container will normally be spaced above the ground surface or mount surface to promote natural flow under the container and circulation within the process area within the container.
  • Auxiliary circulation promotion means may be provided such as fans mounted to the power generation means for example.
  • the fans may be associated with ducting in order to split and communicate the airflow between the compartments to provide a positive pressure to prevent any gas.
  • the container will normally be provided with Ming/securing/transport points or connections. These connections will preferably be accessible only from within the container, and therefore access into the interior of the container will usually be required before the container can be secured in position, or removed.
  • Lift points will normally be provided at at least some of the upper corners of the container, normally at each of the four upper coiners.
  • Anchor points ⁇ will normally be provided at at least some of the lower corners of the container, normally at each of the four lower corners.
  • the container is preferably mounted above ground level. Normally, the container will be mounted on a plurality of legs. A particularly preferred height will be 450 mm above the ground or mount surface. It is preferred that the legs used to mount the container are adjustable to allow for height adjustment of the container and also to provide levelling capabilities.
  • the container and/or the legs of the container will normally be mounted relative to a plinth or slab laid on the ground surface.
  • the slab will preferably be or include concrete and will normally be reinforced.
  • the container may be mounted utilising sound and/or vibration absorbing material.
  • the power generation means will preferably be mounted at one end portion of the container with the oil expeller mounted below the power generation means.
  • the oil expeller mounted below the power generation means.
  • a raw oil catch tray will normally be located below the expeller.
  • the catch tray will also typically be configured to function as a heavy gauge filter to remove larger particulate or plant matter which may escape the oil expeller.
  • the raw oil catch tray will typically be in fluid communication with a raw oil holding tank.
  • the finished biodiesel holding tank will normally be located at a lower portion of the end of the container opposite to the power generation means.
  • the compartment located towards the middle of the container, between the compartment containing the power generation means and the compartment containing the finished by a diesel holding tank, will preferably hold the chemical process equipment used to produce the finished biodiesel.
  • the raw oil from the oil expeller is preferably pumped into a first heater and then to the mixer where the catalyst is mixed and passes through a second heater, to a settling column.
  • the settling columns preferably allow the methanol vapour to be collected in a holding tank. From the bottom of the settling tank, glycerine is drawn off and discharged to a collection tank external to the machine.
  • the biodiesel is then pumped through further separation steps, at least one of which discharges to a methanol collector, normally to a zeolite column and then to the polishing filters, through a pH meter into the finished biodiesel holding tank.
  • the plant of the present invention includes a power generation means, and the power generation means will normally be mounted at an upper portion of the interior of the container towards one end of the container.
  • the power generation means will normally include a diesel generating set or diesel power pack. Typically, the power generation means will produce hydraulic power or electricity which will then be used to power the other process components.
  • the power generation means is preferably fully enclosed within a separate compartment within the container. This may assist with limiting contamination of the process and/or the raw oil or finished biodiesel.
  • the power generation means will normally, by its very nature, produce heat during operation. Waste heat from the power generation means may preferably be used to it is partially heat the raw oil or to provide heat to other process equipment.
  • the power generation means is normally associated with a pump in order to move the raw oil, intermediate products and finished biodiesel into, out of and through the process steps.
  • a screw pump is preferred and normally more than one screw pump will be provided.
  • the system includes an oil expeller.
  • the oil expeller is designed to pulp the raw feedstock and to produce the raw oil. Any configuration of oil expeller can be used.
  • the preferred oil expeller is adjustable to control the clearance allowed for the feedstock. The adjustable nature of the expeller also allows the control of where by movement of the engaging parts.
  • the expeller will normally have a central shaft which rotates and about which is mounted a pulping body which engages with a surrounding sheet to grind or pulp with the feedstock to release the raw oil.
  • the expeller shaft is typically driven by an electrical or hydraulic motor powered from the power generation means.
  • the present invention typically include a raw oil collection tank. Interposed between the outlet of the expeller and the raw oil collection tank is typically a separation or filtration means, normally including a weir and a mesh filter.
  • the raw oil collection tank is typically located below the expeller.
  • the tank has a capacity of approximately 600 L. It is of course anticipated that different size tanks may be provided for different sized plants.
  • the raw oil collection tank is preferably vented to the interior of the process area of the container by means of a circuitous vent member.
  • This vent member will typically be provided with a flash arrestor, normally a gauze flash arrestor.
  • the circuitous vent member will rise to a level above the interior floor of the container, normally to a height of approximately 300 mm above the floor.
  • the raw oil will typically be extracted from the raw oil holding tank by a pump means.
  • the raw oil outlet from the raw oil collection tank will be located above the base of the tank, a preferred position being approximately 50 mm above the base of the tank.
  • the raw oil collection tank will also have a drain valve positioned at a lower portion in order to permit removal of condensation or to allow the tank to be drained.
  • the oil Upon leaving the raw oil collection tank, the oil will typically be passed through a heater, normally a heat exchanger.
  • the heat exchanger will normally be located immediately adjacent the discharge side of the pump. The heat exchanger will preferably supply enough energy to the oil to raise the raw oil temperature to approximately 45°C.
  • the heat will normally be provided from heated water which may be heated by diverting the flow of coolant from the power generation means .
  • the catalyst used in transesterification process of the present invention will also be stored within the container of the preferred embodiment. Normally, the catalyst will be stored in one or more catalyst tanks. These tanks are preferably able to be filled from outside the container and normally, an inlet will be provided for this purpose. The catalyst tanks will also preferably be ventilated by providing a circuitous vent member again typically with an associated spark arrestor.
  • the catalyst and the raw oil will normally be mixed in the mixer after heating the raw oil.
  • the catalyst used normally be an anhydrous mixture of the methanol and sodium or potassium hydroxide in proportions of approximately 12:1 by mass, for example Sodium Methylate. This mixture will normally be injected into a disturbed flow of raw oil in the mixer by means of a dosing pump.
  • the mixer will preferably be appropriate configured to thoroughly mix the catalyst and raw oil.
  • a further heater will typically be provided immediately adjacent to mixer such that the fluid exiting the mixer can be heated to approximately 9O 0 C.
  • the heater will normally utilise waste heat recovered from the power generation means by means of hot air derived from passing a current of air across the exhaust pipe.
  • An additional benefit of using the waste heat is the cooling of the exhaust from the power generation means (to approximately 15O 0 C.)
  • the mixer may have integrated heating means provided to maintain the heat of the mixture whilst in the mixer. This can be achieved by wrapping the mixer in a heated water j acket, for example.
  • the methanol gases vaporise off the mixture in a controlled fashion.
  • This gas will typically be condensed and collected in a vessel connected to an anti- siphon/degassing column. Removing the gas at this process location will preferably permit all subsequent process vessels to be gas tight.
  • the separation steps will normally include degassing, settling and glycerine separation, final methanol separation, filtration, and final polishing.
  • the settling and glycerine separation step will preferably include the removal of the methyl ester, normally by drawing off, and the discharge of the glycerine from the product mixture to an external collection vessel.
  • the methyl ester is preferably drawn off to a flow stabilising column for the final methanol separation process.
  • the final methanol/methyl ester separation will preferably take place in a methanol separator.
  • the methanol separation of will preferably be a mechanical device that allows the methanol to flash vaporise from the product mixture by using differential pressure rather than heat.
  • the methanol is preferably driven by airflow to a condensation column and from there to a collection vessel.
  • the methyl ester is preferably collected within the methanol separator and passed to the flow stabilisation column where it joins the methyl ester which was separated from the settling and glycerine separation step.
  • the methyl ester is then preferably moved via the pump means through the filtration and polishing steps.
  • the methyl ester is preferably passed through a series of filters of ever decreasing cross-section to provide a preferable ultimate filtration size of approximately 1 micron.
  • the methyl ester may also be pumped through a zeolite column and/or an activated carbon column to adsorb remaining contaminants.
  • a pH adjustment system may be provided to ensure that the product biodiesel has a pH of approximately 7.
  • the adjustment system may be configured to add amounts of sulphuric acid in order to comply with the requisite European standard.
  • the biodiesel fuel is then preferably discharged into the biodiesel holding tank.
  • the holding tank is approximately 2000 (m)litres in capacity and is located in a lower portion of the container.
  • the ventilation will be provided for the holding tank by circuitous vent again, provided with spark arrestors and extending to approximately 300 mm above the top of the holding tank.
  • the plant of the present invention is typically provided with a comprehensive hydraulic control system.
  • all the hydraulic or electrical motors provided and driven by the power generation means will be located outside the process area.
  • Control wiring and valve operated servos are preferably low voltage with the wiring being shielded and communicating with a control panel through a gas tight gland.
  • the control panel is preferably also located outside of the process area.
  • the feedstock used according to the present invention can include most oil bearing fruit or plants for example, jatropha, palm, rapeseed, and the like. Other feedstocks can be used with an appropriate adjustment of the process conditions or parameters.
  • Figure 1 is a schematic of a general transesterification reaction used in the system of a preferred embodiment of the present invention.
  • Figure 2 is a view from above (top wall removed) of a particularly preferred configuration of the container of the present invention.
  • Figure 3 is a perspective view from above of the container illustrated in Figure 2.
  • Figure 4 is an isometric view of the container illustrated in Figures 2 and 3.
  • a portable biodiesel manufacturing plant 10 is provided.
  • the system has the following features: Generating Set or Power Plant
  • the proposed generating set is the Kubota SQ-3200, with operating parameters of: • Engine Speed: 1500 rpm
  • the generating set is fully enclosed, with a sound footprint meeting all current legislation and is contained in an upper part 11 of one end of the container of the illustrated embodiment.
  • the characteristics are as follows: • Consumption 5.3 litres per hour • Fuel tank 62 litres
  • coolant from the jacket cooling system will be passed via a thermostat to a heater around the oil system.
  • a heat recovery system is mounted to provide further heating of the raw oil.
  • two B-form pulleys will each drive a Mono screw type pump through an electrically operated clutch.
  • Each pump will be regulated to handle flow rates of approximately 250 litres per hour.
  • Power is provided by a diesel powered hydraulic power pack.
  • the engine water cooled high speed diesel engine running at approximately 2600 rpm.
  • Power is generated by a bank of three hydraulic pumps providing power to:
  • the electrical alternator is sized to meet the requirement of the three heating elements (15kW) and driven by a hydraulic motor running at 1500 rpm.
  • the alternator is specified to a low temperature rise (4O 0 C).
  • a hydraulic oil cooling matrix mounted outside the engine radiator.
  • the electrical system comprises a simple distribution board with a three phase isolator, an isolating switch and the thermostat contactor.
  • the air flow to the radiator is partially deflected to provide a flow that permits the necessary pressure differential that will draw air through the Chantrelle.
  • the raw material feedstock will typically undergo breakdown in physical size and/or chemical availability of the target material.
  • a "squidger” may be used initially.
  • the squidger is an adaptation of the wood chipping machine used extensively to render down trees to more easily disposed wood drippings.
  • the squidger is hydraulically powered and turns a circular plate fitted with cutting blades, and is enclosed in a sheet metal housing.
  • the material exiting the squidger may then proceed through a macerator.
  • the purpose of the macerator is to crack the feedstock in order to permit the expeller to expend less energy in cracking the feedstock and thereby use its energy more efficiently in expelling the oil.
  • the macerator preferably comprises a pair of intermeshed gears mounted between face plates.
  • One gear, the driven gear is located in bush type bearings mounted as friction fit in the end plates.
  • the gear is driven by a hydraulic motor by way of a reduction gear arrangement that permits the macerator gears to run at half the motor speed.
  • the macerator gears are typically hardened steel and are sufficiently long to cover the whole width of the expeller intake.
  • the idler gear will normally be mounted in similar bush bearings as the driven gear, however, the bushes are mounted in an adjustable sliding block in each face plate in order to permit the distance between the gear axes to be adjusted.
  • the side face plates are preferably secured to two plates parallel to the axes of rotation. Above the sides, there is normally a tapered chute arrangement to accept the loaded feedstock. Under the macerator, there is a sheet metal chute to guide the broken feedstock to the expeller. Expeller
  • the purpose of the Expeller is to extract the oil from within the feedstock.
  • the Expeller' s has a tapered screw arrangement. It is driven by a hydraulic motor through a flexible direct coupling and an adjustable positive pressure device.
  • the shaft speed is controlled by a speed controller on the hydraulic motor which is constrained to operate in the range 0 - 120 rpm.
  • the shaft comprises two sections, a parallel section that provides a positive feed, and a tapered section that permits a controlled compression of the feedstock.
  • the shaft is a composite structure of glass filled nylon laid upon a steel shaft.
  • the shaft rotates within a tapered bore, machined in a series of plates bound together by an array of tie rods in high tensile steel.
  • the shaft discharges the compressed feedstock into a choke arrangement that is adjustable to permit a variation in throughput that has a resultant controlling influence on the pressure within the expeller.
  • the plates have clearance channels to relieve the oil.
  • the oil is discharged into the hot oil tank.
  • Hot Oil Collection Tank
  • the clear oil After passing through a weir and a mesh filter, the clear oil is collected in a plastic tank mounted below the expeller 12.
  • the tank has a capacity of approximately 600 litres.
  • the tank is vented to the interior of the process area by means of a goose necked vent with a gauze flash arrestor.
  • the goose neck will stand 300 mm above the floor.
  • Oil will be extracted from the tank by a Mono pump, drawing by way of fuel grade flexible hoses from approximately 50 mm above the base of the tank.
  • the tank will have a drain valve positioned at the bottom to permit condensation to be run off.
  • the oil will be passed through a marine type heat exchanger within the generating set immediately upon discharging from the pump.
  • This heat exchanger will supply approximately 5kW of energy to the oil raising the oil temperature to approximately 45°C.
  • Heat from the jacket water will be provided by diverting the flow of coolant between the radiator and the engine water jacket by means of a tee- piece and a thermostat, consistent with marine practice.
  • the catalyst tank 17 is an intrinsic part of the separating bulkhead and holds 300 litres of premixed catalyst.
  • the tank is filled from the exterior of the plant of the present invention by hand pump from 200 litre drums, and ventilated by a swan necked vent with spark arrestor.
  • the oil is supplied to the mixer from the Primary Oil Heater.
  • the catalyst a mixture of Methanol and Sodium or Potassium Hydroxide in the proportions of 12:1 by mass, is injected into a disturbed flow of raw oil by means of a dosing pump supplied by Prominent Fluid Controls Ltd.
  • a dosing pump supplied by Prominent Fluid Controls Ltd.
  • the mixer there is an array of wheels, which is another proprietary plant feature that ensures ideal mixing.
  • the mixer combines the raw vegetable oil with the sodium methylate/methanol reagent.
  • the flows of the catalyst and raw vegetable oil are controlled to provide the necessary ratio of mixing.
  • the oil enters the mixer at not less than 65°C.
  • the catalyst enters the mixer by way of a non-return valve.
  • the mixing is achieved through a combination of shear plane and turbulent mixing.
  • the fluid Upon emerging from the mixer, the fluid is heated to approximately
  • waste heat recovered from the generator exhaust 90°C by means of waste heat recovered from the generator exhaust.
  • the waste heat is collected by heating water in a tube stack by allowing the exhaust gas to pas through the tubes. This has the added advantage of cooling the exhaust to approximately
  • Heating is achieved by wrapping the mixer in a water jacket. Degassing
  • the settling and separation is undertaken using the HydraShear 13, a patented technology built and developed in Australia by Machining and Hydraulics.
  • This patented system permits the methyl ester to be drawn off and the glycerine to be discharged to an external collection vessel.
  • the methyl ester is drawn off to a flow stabilising column through the final methanol separation process, from which it continues through the remaining polishing and filtration.
  • Final methanol separation The Methanol Separator 14 is a mechanical device that permits the methanol to flash off by using differential pressure rather than heat.
  • the methanol is driven by a draught of air to the condensing column and thence to the collecting vessel.
  • the methyl ester is collected within the separator chamber and passed to the flow stabilising columns 16.
  • the methyl ester is pumped by the second Mono screw pump through two columns 15 containing zeolite and activated carbon that permits all remaining contaminants to be adsorbed.
  • the Zeolite In a pre Mixer stage the Zeolite is mixed with Perlite in a proportion that will optimise the absorption of water. In the post-Chantrelle phase, the Zeolite is used without any additive.
  • the FAME generally leaves the Chantrelle at a pH of 8.5. This is reduced by passing it through the ion exchange medium and subsequently by dosing the FAME with an appropriate quantity of Phosphoric Acid to provide a biodiesel with a pH of 7.0 + /- 0.2, which is well within the desired parameters.
  • polishing filters are 5 ⁇ m paper element filters.
  • the biodiesel passes through a pH meter to ensure that the fuel complies with EN 14214, and has a pH of 7. In the unlikely event that it fails so to comply, the fuel will have minute amounts of Sulphuric Acid added to comply.
  • the neutral fuel is then discharged to a holding tank of approximately 2,000 litres capacity located in the floor of the machine and perforated with large diameter holes.
  • Ventilation is by swan-necked vents with spark arrestors extending some 300 mm above the tank top. Bonding
  • the structure is generally of a suitable plastic as are all component containers and vessels. Hoses are of fuel grade flexible material with plastic or metal fittings.
  • AU component elements are grounded by bonding straps to ensure zero resistance, and the whole structure grounded through the container securing anchors. Electrical system
  • Control wiring and valve operating servos are low voltage with the cabling shielded and led to the control panel through a gas tight gland. All lights and warning indicators are LED's or LCD's where appropriate.
  • the control panel is located outside the process area. Ventilation
  • the tanks that comprise the floor of the machine are perforated with large diameter holes to permit heavy gases to sink out of the machine. Vents are located on both sides of the machine at the top in way of the process area.
  • the container itself will be mounted on legs some 450 mm above a concrete plinth ensuring a natural flow of air under the machine encouraging the circulation of air within the process area.
  • Air from the engine driven cooling fan will be ducted and split to provide the necessary airflow to positively vent the methanol vapours and to provide a positive flow of ventilating air. As this fan is not driven by any electrical device, the risk of spark is eliminated.
  • a "cauldron” may be provided to function as both the hot oil tank and glycerin separator.
  • the glycerin separation tank is inserted inside the hot oil tank and secured with a collar of angle cross section to provide a gas tight joint.
  • the glycerin separation tank comprises four chambers with a linear reduction in volume across a series of weirs.
  • the top of the tank is closed by a sealed lid.
  • the bottom of the tank has a manifold that permits the glycerin to be run off as desired.
  • the Container The container is constructed from plastic with securing points accessible only from the interior. Lifting points are located at the four top corners and anchoring points are located at the four lower corners.
  • the container will be mounted 450mm above the ground with adjusters in the anchor legs to permit the unit to be levelled.
  • a chute On either side of the expeller, a chute will be situated, on the input side to permit loading and on the opposite side to facilitate discharge.
  • the engine will be mounted in its sound absorbing container on a mounting platform with rubber infill seals surrounding the unit to provide suitable aesthetics.
  • the access door will be gas tight with a clear view panel. Access to the container will be by two steps.
  • the machine is capable of handling most feedstocks currently used. Installation
  • the plant of the present invention requires only the simplest of preparation - level concrete plinth approximately 3 m x 6 m x 150 mm. Road access would assist, but is not essential. Servicing
  • the fuel holding tank should be drained of moisture daily •
  • the expeller shaft should be changed every 1750 hours.
  • the Process 1. Load feedstock 2. Feedstock macerated a. Through Squidger if Coconut or Macadamia in shell b. Through Macerator

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Microbiology (AREA)
  • Liquid Carbonaceous Fuels (AREA)
  • Fats And Perfumes (AREA)

Abstract

L'invention porte sur une installation de fabrication de biodiesel comprenant une enveloppe contenant un moyen de génération de courant, une presse à huile pour broyer finement une matière d'alimentation brute afin d'extraire l'huile brute de la matière d'alimentation, un mélangeur/récipient de réaction dans lequel l'huile brute est mélangée avec une matière de catalyseur et au moins un moyen de séparation pour séparer l'ester méthylique des autres produits.
PCT/AU2009/000051 2008-01-16 2009-01-16 Système et appareil de fabrication de biodiesel WO2009089591A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN200980110110.0A CN101978027B (zh) 2008-01-16 2009-01-16 一种生物柴油生产系统及装置
AU2009204648A AU2009204648B2 (en) 2008-01-16 2009-01-16 A biodiesel manufacturing system and apparatus

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2008900210 2008-01-16
AU2008900210A AU2008900210A0 (en) 2008-01-16 A Biodiesel Manufacturing System and Apparatus

Publications (1)

Publication Number Publication Date
WO2009089591A1 true WO2009089591A1 (fr) 2009-07-23

Family

ID=40885000

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU2009/000051 WO2009089591A1 (fr) 2008-01-16 2009-01-16 Système et appareil de fabrication de biodiesel

Country Status (4)

Country Link
CN (1) CN101978027B (fr)
AU (1) AU2009204648B2 (fr)
MY (1) MY163543A (fr)
WO (1) WO2009089591A1 (fr)

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013007394A2 (fr) 2011-07-14 2013-01-17 Enerdice Gmbh Système de production de biodiesel mobile
WO2013091002A1 (fr) * 2011-12-20 2013-06-27 The Biocube Corporation Ltd Système et appareil de fabrication de biodiesel
US8735640B2 (en) 2009-10-12 2014-05-27 Elevance Renewable Sciences, Inc. Methods of refining and producing fuel and specialty chemicals from natural oil feedstocks
US8889932B2 (en) 2008-11-26 2014-11-18 Elevance Renewable Sciences, Inc. Methods of producing jet fuel from natural oil feedstocks through oxygen-cleaved reactions
US8933285B2 (en) 2008-11-26 2015-01-13 Elevance Renewable Sciences, Inc. Methods of producing jet fuel from natural oil feedstocks through metathesis reactions
US8957268B2 (en) 2009-10-12 2015-02-17 Elevance Renewable Sciences, Inc. Methods of refining natural oil feedstocks
US9000246B2 (en) 2009-10-12 2015-04-07 Elevance Renewable Sciences, Inc. Methods of refining and producing dibasic esters and acids from natural oil feedstocks
US9051519B2 (en) 2009-10-12 2015-06-09 Elevance Renewable Sciences, Inc. Diene-selective hydrogenation of metathesis derived olefins and unsaturated esters
US9133416B2 (en) 2011-12-22 2015-09-15 Elevance Renewable Sciences, Inc. Methods for suppressing isomerization of olefin metathesis products
US9139493B2 (en) 2011-12-22 2015-09-22 Elevance Renewable Sciences, Inc. Methods for suppressing isomerization of olefin metathesis products
US9169174B2 (en) 2011-12-22 2015-10-27 Elevance Renewable Sciences, Inc. Methods for suppressing isomerization of olefin metathesis products
US9169447B2 (en) 2009-10-12 2015-10-27 Elevance Renewable Sciences, Inc. Methods of refining natural oils, and methods of producing fuel compositions
US9175231B2 (en) 2009-10-12 2015-11-03 Elevance Renewable Sciences, Inc. Methods of refining natural oils and methods of producing fuel compositions
US9222056B2 (en) 2009-10-12 2015-12-29 Elevance Renewable Sciences, Inc. Methods of refining natural oils, and methods of producing fuel compositions
US9365487B2 (en) 2009-10-12 2016-06-14 Elevance Renewable Sciences, Inc. Methods of refining and producing dibasic esters and acids from natural oil feedstocks
US9382502B2 (en) 2009-10-12 2016-07-05 Elevance Renewable Sciences, Inc. Methods of refining and producing isomerized fatty acid esters and fatty acids from natural oil feedstocks
US9388098B2 (en) 2012-10-09 2016-07-12 Elevance Renewable Sciences, Inc. Methods of making high-weight esters, acids, and derivatives thereof
CN110878232A (zh) * 2019-12-01 2020-03-13 江西艾迪尔新能源有限公司 一种旋转固定床快速反应制备生物柴油装置

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107249722A (zh) * 2014-12-03 2017-10-13 贝克瑞概念国际有限责任公司 混合室

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050006290A1 (en) * 2003-06-05 2005-01-13 Patten J. P. Mobile biodiesel refinery
US6979426B2 (en) * 2002-03-15 2005-12-27 Biodiesel Industries Biodiesel production unit
US20060080891A1 (en) * 2004-10-20 2006-04-20 Council Of Scientific And Industrial Research Process for the preparation of fatty acid methyl ester from triglyceride oil by transesterification
WO2007033425A1 (fr) * 2005-09-23 2007-03-29 Cassa Pty Ltd Systeme de recyclage et de production de bio-carburant mobile destine a des dechets animaux

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100383220C (zh) * 2006-01-23 2008-04-23 生作仁 生物柴油及其制备工艺
CN100432187C (zh) * 2006-09-21 2008-11-12 郑州新力德粮油科技有限公司 生物柴油的生产方法
CN100398629C (zh) * 2006-09-29 2008-07-02 合肥工业大学 植物油皂脚制备生物柴油的工艺方法
CN1974724B (zh) * 2006-12-04 2010-09-29 李燕丽 高效制备生物柴油的方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6979426B2 (en) * 2002-03-15 2005-12-27 Biodiesel Industries Biodiesel production unit
US20050006290A1 (en) * 2003-06-05 2005-01-13 Patten J. P. Mobile biodiesel refinery
US20060080891A1 (en) * 2004-10-20 2006-04-20 Council Of Scientific And Industrial Research Process for the preparation of fatty acid methyl ester from triglyceride oil by transesterification
WO2007033425A1 (fr) * 2005-09-23 2007-03-29 Cassa Pty Ltd Systeme de recyclage et de production de bio-carburant mobile destine a des dechets animaux

Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8889932B2 (en) 2008-11-26 2014-11-18 Elevance Renewable Sciences, Inc. Methods of producing jet fuel from natural oil feedstocks through oxygen-cleaved reactions
US8933285B2 (en) 2008-11-26 2015-01-13 Elevance Renewable Sciences, Inc. Methods of producing jet fuel from natural oil feedstocks through metathesis reactions
US9169447B2 (en) 2009-10-12 2015-10-27 Elevance Renewable Sciences, Inc. Methods of refining natural oils, and methods of producing fuel compositions
US9732282B2 (en) 2009-10-12 2017-08-15 Elevance Renewable Sciences, Inc. Methods of refining natural oil feedstocks
US9175231B2 (en) 2009-10-12 2015-11-03 Elevance Renewable Sciences, Inc. Methods of refining natural oils and methods of producing fuel compositions
US9469827B2 (en) 2009-10-12 2016-10-18 Elevance Renewable Sciences, Inc. Methods of refining natural oil feedstocks
US8957268B2 (en) 2009-10-12 2015-02-17 Elevance Renewable Sciences, Inc. Methods of refining natural oil feedstocks
US9000246B2 (en) 2009-10-12 2015-04-07 Elevance Renewable Sciences, Inc. Methods of refining and producing dibasic esters and acids from natural oil feedstocks
US9051519B2 (en) 2009-10-12 2015-06-09 Elevance Renewable Sciences, Inc. Diene-selective hydrogenation of metathesis derived olefins and unsaturated esters
US9464258B2 (en) 2009-10-12 2016-10-11 Elevance Renewable Sciences, Inc. Diene-selective hydrogenation of metathesis derived olefins and unsaturated esters
US9382502B2 (en) 2009-10-12 2016-07-05 Elevance Renewable Sciences, Inc. Methods of refining and producing isomerized fatty acid esters and fatty acids from natural oil feedstocks
US9222056B2 (en) 2009-10-12 2015-12-29 Elevance Renewable Sciences, Inc. Methods of refining natural oils, and methods of producing fuel compositions
US10689582B2 (en) 2009-10-12 2020-06-23 Elevance Renewable Sciences, Inc. Methods of refining natural oil feedstocks
US8735640B2 (en) 2009-10-12 2014-05-27 Elevance Renewable Sciences, Inc. Methods of refining and producing fuel and specialty chemicals from natural oil feedstocks
US9365487B2 (en) 2009-10-12 2016-06-14 Elevance Renewable Sciences, Inc. Methods of refining and producing dibasic esters and acids from natural oil feedstocks
US9284512B2 (en) 2009-10-12 2016-03-15 Elevance Renewable Sicences, Inc. Methods of refining and producing dibasic esters and acids from natural oil feedstocks
WO2013007394A3 (fr) * 2011-07-14 2013-05-10 Enerdice Gmbh Système de production de biodiesel mobile
WO2013007394A2 (fr) 2011-07-14 2013-01-17 Enerdice Gmbh Système de production de biodiesel mobile
US9364770B2 (en) 2011-12-20 2016-06-14 The Biocube Corporation Ltd. Biodiesel manufacturing system and apparatus
WO2013091002A1 (fr) * 2011-12-20 2013-06-27 The Biocube Corporation Ltd Système et appareil de fabrication de biodiesel
US9169174B2 (en) 2011-12-22 2015-10-27 Elevance Renewable Sciences, Inc. Methods for suppressing isomerization of olefin metathesis products
US9139493B2 (en) 2011-12-22 2015-09-22 Elevance Renewable Sciences, Inc. Methods for suppressing isomerization of olefin metathesis products
US9133416B2 (en) 2011-12-22 2015-09-15 Elevance Renewable Sciences, Inc. Methods for suppressing isomerization of olefin metathesis products
US9481627B2 (en) 2011-12-22 2016-11-01 Elevance Renewable Sciences, Inc. Methods for suppressing isomerization of olefin metathesis products
US9388098B2 (en) 2012-10-09 2016-07-12 Elevance Renewable Sciences, Inc. Methods of making high-weight esters, acids, and derivatives thereof
CN110878232A (zh) * 2019-12-01 2020-03-13 江西艾迪尔新能源有限公司 一种旋转固定床快速反应制备生物柴油装置

Also Published As

Publication number Publication date
MY163543A (en) 2017-09-29
AU2009204648A1 (en) 2009-07-23
CN101978027A (zh) 2011-02-16
CN101978027B (zh) 2014-07-16
AU2009204648B2 (en) 2013-04-18

Similar Documents

Publication Publication Date Title
AU2009204648B2 (en) A biodiesel manufacturing system and apparatus
RU2766001C2 (ru) Интегрированная система конверсии отходов и соответствующий способ
US7906082B2 (en) Method and apparatus for refining biodiesel
US6979426B2 (en) Biodiesel production unit
CA2922494C (fr) Procede de fabrication de biodiesel et reacteur
US7947858B2 (en) Method and apparatus for thermal processing of biomass
CN112742852B (zh) 一种餐余垃圾生态处理装置及其处理方法
EP3080232B1 (fr) Procédé et système de production de biocarburant liquide provenant d'huiles et/ou de graisses à base biologique
US9364770B2 (en) Biodiesel manufacturing system and apparatus
US20120060411A1 (en) Mobile biodiesel production facility
CN216005592U (zh) 一种油泥集成干化处理系统
Piętak et al. Possibility of automation of a mobile biodiesel production plant
CN211069068U (zh) 一种脂肪酸残渣蒸馏塔
WO2013007394A2 (fr) Système de production de biodiesel mobile
CN202440340U (zh) 一种高尔夫球场湖水净化处理车
OA16912A (en) A biodiesel manufacturing system and apparatus.
MX2007010827A (es) Proceso y aparato para producir biodiesel empleando una etapa ácida y dos etapas alcalinas.
CN102583623A (zh) 一种高尔夫球场湖水净化处理车

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 200980110110.0

Country of ref document: CN

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09702303

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: PI 2010003337

Country of ref document: MY

WWE Wipo information: entry into national phase

Ref document number: 2009204648

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: 1736/MUMNP/2010

Country of ref document: IN

ENP Entry into the national phase

Ref document number: 2009204648

Country of ref document: AU

Date of ref document: 20090116

Kind code of ref document: A

122 Ep: pct application non-entry in european phase

Ref document number: 09702303

Country of ref document: EP

Kind code of ref document: A1