WO2008016330A2 - Bio formula to substitute diesel fuel - Google Patents
Bio formula to substitute diesel fuel Download PDFInfo
- Publication number
- WO2008016330A2 WO2008016330A2 PCT/SG2007/000224 SG2007000224W WO2008016330A2 WO 2008016330 A2 WO2008016330 A2 WO 2008016330A2 SG 2007000224 W SG2007000224 W SG 2007000224W WO 2008016330 A2 WO2008016330 A2 WO 2008016330A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reactor
- temperature
- tank
- proceeded
- result
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Ceased
Links
Classifications
-
- 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- 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
- 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
- bio formula 100 a production process of biofuel further-on called as "bio formula 100", as an alternative material to substitute Diesel Fuel originated from vegetables in the form of palm coconut oil waste.
- Biofosil subsidy which is being accounted for to the selling Biofosil price, resulted in the high Biofosil price hike, so as to deeply affect almost all public levels, especially the lower level community.
- Biofosil is one of natural sources that can not be renewed, it is deemed necessary and important to put into consideration to have an alternative as its substitution.
- Biofosil substitutions such as bricks, coals taken from plantation waste, biogas and others.
- Biofosii from different raw materials, produced through chemical reaction process, distillation residue, thermal cracking, fractionalization and other processes which have been done to meet the need of alternative fuel.
- many of them is of high cost, in the supply of raw materials, its additive, supporting materials, its catalyst, instrument, location and so on.
- most of them have to go through difficult process stages, especially to keep continued process, even though it can be simplified, the result of quality and quantity are not at the maximum, that is, far from adequately anticipated.
- bio formula 100 an alternative material of biofuel originated from vegetables which is of palm coconut waste.
- the object of the current invention primarily in regard to the production process of bio formula 100, as an alternative materia! of diesel fuel, essentially covers some stages.
- R1 Reactor Reactor FFA Treatment Unit
- R1 Reactor Reactor FFA Treatment Unit
- the result is proceeded into D1 distillation column to be distilled the top/vapour fraction, in the form of methanol, through the condenser at temperature 20 * C, in liquid condition proceeded to TB1.
- the bottom/liquid fraction in the form of liquid (water + glycerol + methanol + salt) through the reboiler at temperature 100° C, in liquid condition and proceeded to TB5.
- R2A and R2B is removed through the bottom part reactor, proceeded into PR2 (Pre Reactor Reserved), further-on it is proceeded into D2 distillation column, the top/vapour fraction D2, in the form of methanol through the condenser at temperature 20 ° C, in liquid condition, proceeded to D1 for continued process in D1 so that D1 input becomes two, that is D2 and E1, and further-on distilled the same way as the initiai D1 stage the bottom/liquid fraction, which is the mixture of Bio Diesel and Glycerine through the reboiier at temperature 100° C, in liquid condition, being recovered/withdrawn through D3 distillation column, reserved in the Reserve Tank Glycerol TB2.
- PR2 Pre Reactor Reserved
- the top/vapour fraction in the form of Glycerine through the condenser at temperature 20 * C, in liquid condition, and is proceeded into TB2 the bottom/liquid fraction in the form of (methyl ester/biodiesel) through reboiler at temperature 150'C 1 in liquid condition, is proceeded to R4 Reactor
- the methyl ester/biodiesel is being neutralized from pH 10 to become pH (5,5 - 6,5) by adding sulphuric acid with 12 Molar concentration, one-hundredth methyl ester volume, from TB3 tank (the sulphuric acid bait tank) and one-fifth methyl ester volume from the TB4 water reserved tank, being processed as the second catalyst, then evaporated in E2, the result of evaporation, top fraction in the form of water + soap + salt are kept in TB5 Dirty Water Reserve Tank, and the bottom fraction which is the Biodiesel 100 (further-
- the B-100 Biofuel product having physico and chemical characteristics as follows:
- Figure 1 is a stream diagram of B-100 formula production process as the diesel fuel substitution which is in line with the current invention.
- the current invention is mainly in regard to the production process of bio formula 100, functioning as the alternative substitution of diesel fuel, essentially covering the following stages:
- R1 Reactor FFA Treatment Unit Reactor
- FFA Treatment Unit Reactor being the mixing tank reactor
- temperature (60 - 70) 'C? the kind ⁇ ype of continued reactor in operation condition
- temperature (60 - 70) 'C? the kind ⁇ ype of continued reactor in operation condition
- temperature (60 - 70) 'C? the kind ⁇ ype of continued reactor in operation condition
- temperature (60 - 70) 'C? the kind ⁇ ype of continued reactor in operation condition
- temperature (60 - 70) 'C? atmospheric pressure
- the fractions (bottom) of the distillation result being the methyl ester, having a temperature of 70 * C.
- the top/vapor fraction, methanol, through the condenser at temperature 20 * C, in liquid condition is proceeded to TB1.
- the bottom/liquid fraction which is a mixture of (water + glycerol + soap) through the reboiler at temperature 70° C, in liquid form and proceeded to TB5.
- WVO is proceeded (being the bait in the form of oil waste of fruits/palm coconut) which has been evaporated in E1 evaporator and retained in PR1 (Pre Reactor Reserved) for 30 minutes, meant for homogeneity, mixed and put into R2A and R2B reactors (which is the main reactor being the mixing tank for continued process/ the CSTR Main Reactor through M1 together with the mixture result of R3 i.e. NaMethanol. This is done in order to obtain Methyl Ester result.
- D2 distillation column having column packing specification, in operation condition (temperature 65 * C, pressure - (20 - 60) mmHg, condenser/reboiler on the distillation container is in the form of Shell and Tube and the reboiler is the Reboiler Kettle, the top/vapour fraction, in the form of methanol through the condenser at temperature 20 'C, in liquid condition proceeded into D1 for continued process in D1 so that D1 input becomes two i.e.
- top/vapour fraction in the form of Glycerol through condenser at temperature 20 * C, in liquid condition, proceeded to TB2
- bottom/liquid fraction in the form of (methyl ester/biodiesel) through the reboiler at temperature 65 * C, in liquid condition proceeded to R4 reactor.
- Biodiesel B-100 the substitution of diesel fuel reserved in the Biodiesel B-100 Product Tank.
- Biodiesel B-100 product has a physico and chemical characteristics as the following: Physico state is in the form of yellow-brownish liquid The chemical characteristics of 6 maximum acid number The above-mentioned characteristics have fully met the criteria as alternative material for diesel fuel substitution.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Liquid Carbonaceous Fuels (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Fats And Perfumes (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Bio formula 100 production process as an alternative material to substitute diesel fuel is disclosed. The process covers the following stages: refinery of oil waste originated from palm coconut, the end-product proceeds into R1 reactor while adding methanol and sulphuric acid, evaporation in E1, distillation in column D1, the result is retained in TB1 bait tank and proceeded into R3 tank, NaOH/KOH is included, having WVO flow in (oil waste of fruits/palm coconut) which have been evaporated in E1 and reserved in PR1, mixed and put into the R2A and R2B through M1 together with the mixture result of R3 proceeded into PR2, then distillation into D2 column for continued process in D1 so that D1 input becomes two that is D2 and E1, the bottom/liquid fraction through the reboiler, in liquid condition, is recovered/withdrawn through D3 distillation column, retained in TB2, at D3 distillation column, the top/vapour fraction, in the form of methanol through the condenser, proceeding to TB2, methyl ester/biodiesel is proceeded into R4 Reactor, neutralising by adding sulphuric acid from TB3 tank and water from TB4 water reserve tank, processed as the second catalyst, which then being evaporated in E2, the top fraction is retained in TB5, and the bottom fraction in the form of biodiesel 100 is reserved.
Description
Description
BIO FORMULA TO SUBSTITUTE DIESEL FUEL
Invention in the technical sector
This invention is regarding a production process of biofuel further-on called as "bio formula 100", as an alternative material to substitute Diesel Fuel originated from vegetables in the form of palm coconut oil waste.
Background of the invention
Fuel has been always an issue in various countries. Many ways have been taken in searching alternative material to substitute fuel. Relative to the current -invention is the material for fuel oil meant to operate diesel engine which is the diesel fuel
Fuel oil material Biofosil subsidy which is being accounted for to the selling Biofosil price, resulted in the high Biofosil price hike, so as to deeply affect almost all public levels, especially the lower level community. As we believe Biofosil is one of natural sources that can not be renewed, it is deemed necessary and important to put into consideration to have an alternative as its substitution.
There has been many Biofosil substitutions being highlighted such as bricks, coals taken from plantation waste, biogas and others. Biofosii from different raw materials, produced through chemical reaction process, distillation residue, thermal cracking, fractionalization and other processes which have been done to meet the need of alternative fuel. However, many of them is of high cost, in the supply of raw materials, its additive, supporting materials, its catalyst, instrument, location and so on. Besides, most of them have to go through difficult process stages, especially to keep continued process, even though it can be simplified, the result of quality and quantity are not at the maximum, that is, far from adequately anticipated. Deficiencies often exist everywhere in the technical area like this, however, in order to minimize the lack and obstacles mentioned above at the utmost possible, primarily in quality and quantity wise, the effective value of the product. Even though it could produce something, it is inadequately beneficial especially to public use.
In this instance, to the industry the product is categorized less effective, in other words inapplicable to the industry. Needless to say, this would be useless and such product is unable to meet the economic value.
These obstacles mentioned above would just result in high price of BBM, specifically relevant to this invention coverage, which is the diesel fuel. If that is the case, the issue is raised whether or not an alternative could be found to process alternative raw material for biofuel in order to obtain any alternative fuel to substitute diesel fuel. For those who are constantly innovative, willing to express and to interact in their area, there would be always an alternative to process the production of biofuel from alternative raw materials which could reduce the entire cost and sales price.
By implementing production process of bio formula 100 as substitution of diesel fuel in accordance with the current invention, the obstacles mentioned above could be overcome or at least reduced significantly.
invention summary
The objective focus of the current invention is in regard to the production process of biofuel, further-on called "bio formula 100", an alternative material of biofuel originated from vegetables which is of palm coconut waste.
The object of the current invention, primarily in regard to the production process of bio formula 100, as an alternative materia! of diesel fuel, essentially covers some stages.
- distillation of oil waste from palm coconuts from TB6 by filter press distillation (membrane kind of distillation, membrane plate distillation type)
- the result of 1000 kg distillation flow into R1 Reactor (Reactor FFA Treatment Unit) which is a mixing reactor, of double jacket reactor type, while adding 10.7%, 107 methanol 99% and 25 kg 98% concentrated sulphuric acid.
- the product result is put in the E1 evaporator,
- the result is proceeded into D1 distillation column to be distilled the top/vapour fraction, in the form of methanol, through the condenser at temperature 20* C, in liquid condition proceeded to TB1.
the bottom/liquid fraction, in the form of liquid (water + glycerol + methanol + salt) through the reboiler at temperature 100° C, in liquid condition and proceeded to TB5. the distillation result of methanol with 99% concentration volume 800 ml, and is restrained in the TB1 bait tank which is of Stainless Steel tank, and proceeded to R3 tank which is the mixing tank, wherein at the same time NaOH/KOH is also included with concentration, weight 15 — 25 kg as catalyst, then mixed with 150 kg methanol in M1 mixing tank to obtain Na-Methoxide mixture. then have WVO to proceed (which is the bait of oil waste originated from fruits/palm coconut) which have been evaporated in E1 evaporator and stored in PR1 (Pre Reactor Reserved), mixed and put into the R2A and R2B reactor (which is the main reactor, the mixing reactor tank, for continued process / Main Reactor CSTR through M1 together with the mixture result of R3 which is Glycerine. the result of R2A and R2B is removed through the bottom part reactor, proceeded into PR2 (Pre Reactor Reserved), further-on it is proceeded into D2 distillation column, the top/vapour fraction D2, in the form of methanol through the condenser at temperature 20 ° C, in liquid condition, proceeded to D1 for continued process in D1 so that D1 input becomes two, that is D2 and E1, and further-on distilled the same way as the initiai D1 stage the bottom/liquid fraction, which is the mixture of Bio Diesel and Glycerine through the reboiier at temperature 100° C, in liquid condition, being recovered/withdrawn through D3 distillation column, reserved in the Reserve Tank Glycerol TB2. at D3 distillation column the top/vapour fraction, in the form of Glycerine through the condenser at temperature 20 *C, in liquid condition, and is proceeded into TB2 the bottom/liquid fraction in the form of (methyl ester/biodiesel) through reboiler at temperature 150'C1 in liquid condition, is proceeded to R4 Reactor
At the R4 mixture tank functioning as neutralizing reactor, the methyl ester/biodiesel is being neutralized from pH 10 to become pH (5,5 - 6,5) by adding sulphuric acid with 12 Molar concentration, one-hundredth methyl ester volume, from TB3 tank (the sulphuric acid bait tank) and one-fifth methyl ester volume from the TB4 water reserved tank, being processed as the second catalyst, then evaporated in E2, the result of evaporation, top fraction in the form of water + soap + salt are kept in TB5 Dirty Water Reserve Tank, and the bottom fraction which is the Biodiesel 100 (further-on called as B-100 Bϊofuel the substitution of diesel fuel) restrained in B-100 Biofuel Product Tank.
The B-100 Biofuel product having physico and chemical characteristics as follows:
Physico is in theJorm of yellow-brownish liquid The chemical characteristics are of 6 maximum acid number The above-mentioned characteristics have fully met the criteria as the aftemative material for diesel fuel substitution.
Short description of the picture
Figure 1 is a stream diagram of B-100 formula production process as the diesel fuel substitution which is in line with the current invention.
Complete description of the invention
Production process in detail of B-100 bio formula which is in line with the current invention, can be better comprehended by referring to Figure 1 attached and the following description:
The current invention, is mainly in regard to the production process of bio formula 100, functioning as the alternative substitution of diesel fuel, essentially covering the following stages:
- distillation of oil waste from palm coconut by membrane/filter press, distillation of 1 time/stage.
- distillation result proceeds to R1 Reactor (FFA Treatment Unit Reactor) being the mixing tank reactor, the kindΛype of continued reactor in operation condition, temperature (60 - 70) 'C?, atmospheric pressure,
for (60 - 120) minutes while adding (10 - 15)% methanol 99% concentration and 12 Molar (1 - 1,5)% sulphuric acid
- the result is proceeded into E1 evaporator, with a temperature operation condition (60 - 70)° C, pressure - (30 - 50) mmHg, for (60 - 90) minutes.
- the result is proceeded into D1 distillation column to be distilled with a temperature operation condition (60 - 70)° C, pressure - (30 - 50) mmHg,
The fractions (bottom) of the distillation result being the methyl ester, having a temperature of 70* C. the top/vapor fraction, methanol, through the condenser at temperature 20* C, in liquid condition is proceeded to TB1. the bottom/liquid fraction, which is a mixture of (water + glycerol + soap) through the reboiler at temperature 70° C, in liquid form and proceeded to TB5.
- the result of methanol distillation with 99% concentration, volume 50 liters, is retained in the TB1 bait tank which is a Stainless Steel tank, and proceeded to R3 tank which is a mixing tank, wherein within the same time also included solid NaOH/KOH (1 - 1,5)% WVO weight as catalyst, and then mixed in the M1 mixing tank till a reaction mixture is reached (reaction: methanol + NaOH/KOH -> NaMethanol),
- then WVO is proceeded (being the bait in the form of oil waste of fruits/palm coconut) which has been evaporated in E1 evaporator and retained in PR1 (Pre Reactor Reserved) for 30 minutes, meant for homogeneity, mixed and put into R2A and R2B reactors (which is the main reactor being the mixing tank for continued process/ the CSTR Main Reactor through M1 together with the mixture result of R3 i.e. NaMethanol. This is done in order to obtain Methyl Ester result.
- the result of R2A and R2B are being removed through the bottom part of the reactor, and proceeded into PR2 (Pre Reactor Reserved). This is done to obtain optimum result.
- then proceeded into D2 distillation column having column packing specification, in operation condition (temperature 65* C,
pressure - (20 - 60) mmHg, condenser/reboiler on the distillation container is in the form of Shell and Tube and the reboiler is the Reboiler Kettle, the top/vapour fraction, in the form of methanol through the condenser at temperature 20 'C, in liquid condition proceeded into D1 for continued process in D1 so that D1 input becomes two i.e. D2 and E1, and further-on being distilled similar to the initial D1 stage, the bottom/liquid fraction, a mixture of methyl ester and glycerol through the reboiler at temperature 65 " C, in liquid condition, being recovered/withdrawn through D3 distillation column, reserved in TB2 Glycerol Reserved Tank, at the D3 distillation column having Packing Column specification in operation condition (temperature 65* C, pressure -
(20 - 60) mmHg,
- top/vapour fraction, in the form of Glycerol through condenser at temperature 20 *C, in liquid condition, proceeded to TB2, the bottom/liquid fraction, in the form of (methyl ester/biodiesel) through the reboiler at temperature 65* C, in liquid condition proceeded to R4 reactor. at the R4 mixing tank reactor functioning as neutralizing reactor, in operation condition, temperature of (30 - 40)" C, the atmospheric pressure, for 60 minutes, methyl ester/biodiesel being neutralized from pH 10 to become pH (5,5 — 6,5) by adding sulphuric acid at 12 Molar concentration, volume (1 — 1,5)% Volume methyl ester, from TB3 tank (from sulphuric acid bait tank) and water amounting to (10 - 15)% from the TB4 water reserve tank, processed as the second catalyst, then being evaporated in E2, in operation condition (temperature 65* C, pressure -
(20 - 60) mmHg, for 60 minutes. evaporaton result, top fraction is water + soap + salt reserved in the TB5 Dirty Water Reserve Tank, and the bottom fraction which is the biodiesel 100 (further-on called as Biodiesel B-100 the substitution of diesel fuel) reserved in the Biodiesel B-100 Product Tank.
Such Biodiesel B-100 product has a physico and chemical characteristics as the following: Physico state is in the form of yellow-brownish liquid The chemical characteristics of 6 maximum acid number The above-mentioned characteristics have fully met the criteria as alternative material for diesel fuel substitution.
The technical sector, the stage by stage process as mentioned in the description above will not limit this invention coverage, but will also be included in the invention coverage with the process stage mentioned in the above description.
Claims
1. The current invention, mainly on the production of bio formula 100 as an alternative diesel fuel substitution material, essentially covering the following stages:
- distillation of oil waste from palm coconut through membrane/filter press, distilllation 1 time/stage.
- the d:stillation result goes in the R1 Reactor (FFA Treatment Unit Reactor) which is the mixing reactor, kind/type CSTR reactor in operation condition, temperature (60 - 70) " C, atmospheric pressure, for (60 - 90) minutes while adding 99% methanol and 12 Molar (concentration) (1 - 1,5)% volume WVO sulphuric acid.
- the result is put in the E1 evaporator, in operation condition (temperature 65 *C, pressure - (20 - 60) mmHg, for (60 - 90) minutes.
- the result is proceeded in the D1 distillation column to be distilled in operation condition (temperature 65 " C, pressure — (20 - 60) mmHg, for 60 minutes, the fractions (top, bottom) distillation result which are (methanol, methyl ester), having a temperature of 2Q*C/65*C, with a concentration of 99% top/vapour fraction, in the form of methanol, through the condenser at temperature 20* C, in liquid condition is proceeded to TB1,
the bottom/liquid fraction, in the form of mixture (water + glycerol + methanol + soap) through the reboiler at temperature 65 *C, in liquid condition is proceeded to TB5, reflux from condenser and reboiler
- the result of methanol distillation with 99% concentration, reserved in TB1 bait tank which is a Stainless Steel tank and proceeded to R3 tank which is the mixing tank wherein at the same time is also included solid NaOH/KOH, in the amount of (1 — 1,5)% VWO weight as catalyst and 99% methanol in the amount of (10 - 15)% WVO weight, and then mixed in the M1 mixing tank till a mixed reaction if obtained (reaction: methanol + NaOH/KOH -> Na Methanol),
- then WVO is proceeded (which is the bait in the form of oil waste of fruits/palm coconut) which has been evaporated at the E1 evaporator and stored in PR1 (Pre Reactor Reserved) for 60 minutes, meant for homogenic purpose, mixed and put into R2A and R2B reactor (which is the main reactor in the form of mixing tank for continued process / CSTR Main Reactor) through M1 together with the mixed result from R3, that is NaMethanol. This is done in order to obtain optimum met iyl ester result
- the result of R2A and R2B is removed through the bottom part of the reactor, proceeded into PR2 (Pre Reactor Reserved). This is done in order to obtain optimum result,
- then proceeded into the D2 distillation column having a specification of Column Packing, in operation condition (temperature of 65* C, pressure —
(20 - 60) mmHg, for 60 minutes.
- the fractions (top, bottom), the distillation result in the form of (methanol/methyl ester), with a temperature of 65 'C, the top/vapour fraction, in the form of methanol through the condenser at temperature of 20* C, in liquid condition is proceeded to D1 for continued process in D1 so that D1 input becomes two that is D2 and E1, and then distilled similar to D1 initial stage the top/liquid fraction, in the form of (glycerol + soap + Methyl ester) through the reboiler at temperature 65* C, in liquid condition, being recovered/ withdrawn through the D3 distillation column, reserved in the Glycerol TB2 Reserve Tank,
- at D3 distillation column, having a Column Packing specification in operation condition (temperature 65* C, pressure - (20 - 60) mmHg, for
(60-90) minutes. the top/vapour fraction, in the form of glycerine through the condenser at temperature 20 'C, in liquid condition is proceeded to TB2, the bottom/liquid fraction, in the form of (methyl ester/biodiesel) through the reboiler at temperature 65* C, in liquid condition is proceeded to R4
Reactor,-
- at R4 mixing tank reactor functioning as a neutralized reactor, in operation condition, temperature 40 "C, atmospheric pressure, for 60 minutes, the methyl ester/biodiesel is being neutralized from pH 10 to become pH (5,5 - 6) by adding sulphuric acid with 12 Molar concentration, volume (1 - 1 ,5)%, from TB3 tank (sulphuric acid bait tank) and water (10 - 15)% volume from the TB4 water reserved tank, processed as the second catalyst, and then evaporated in E2, in operation condition (temperature 65 ° C, pressure - (20 - 60) mmHg, for (60 - 90) minutes,
- the evaporation result, top fraction consisting of water + soap + salt is retained in the TB5 Dirty Water Reserve Tank and the bottom fraction which is the biodiesel 100 (further-on called as Biodiesel B-100 being the substitution of diesel fuel) is reserved in the Biodiesel B-100 Product Tank.
Such Biodiesel B-100 product has physico and chemical characteristics as the following:
Physico state is in the form of yellow-brownish liquid The chemical characteristics of 6 maximum acid number
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| INP00200600449 | 2006-08-01 | ||
| ID20060449 | 2006-08-01 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2008016330A2 true WO2008016330A2 (en) | 2008-02-07 |
| WO2008016330A3 WO2008016330A3 (en) | 2009-06-11 |
Family
ID=38997593
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/SG2007/000224 Ceased WO2008016330A2 (en) | 2006-08-01 | 2007-07-30 | Bio formula to substitute diesel fuel |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US20080047194A1 (en) |
| WO (1) | WO2008016330A2 (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2742793C (en) * | 2008-11-26 | 2016-05-10 | Elevance Renewable Sciences, Inc. | Methods of producing jet fuel from natural oil feedstocks through oxygen-cleaved reactions |
| BRPI0921222A2 (en) * | 2008-11-26 | 2018-10-23 | Elevance Renewable Sciences | Jet fuel production processes from natural oil feedstock through metathesis reactions. |
| 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 |
| CN104479882A (en) | 2009-10-12 | 2015-04-01 | 艾勒旺斯可再生科学公司 | Methods of refining and producing fuel from 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 |
| US9175231B2 (en) | 2009-10-12 | 2015-11-03 | Elevance Renewable Sciences, Inc. | Methods of refining natural oils and methods of producing fuel compositions |
| 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 |
| 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 |
| US9222056B2 (en) | 2009-10-12 | 2015-12-29 | Elevance Renewable Sciences, Inc. | Methods of refining natural oils, and methods of producing fuel compositions |
| US9051519B2 (en) | 2009-10-12 | 2015-06-09 | Elevance Renewable Sciences, Inc. | Diene-selective hydrogenation of metathesis derived olefins and unsaturated esters |
| US9169447B2 (en) | 2009-10-12 | 2015-10-27 | Elevance Renewable Sciences, Inc. | Methods of refining natural oils, and methods of producing fuel compositions |
| 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 |
| US9133416B2 (en) | 2011-12-22 | 2015-09-15 | 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 |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3444893A1 (en) * | 1984-12-08 | 1986-06-12 | Henkel KGaA, 4000 Düsseldorf | METHOD FOR PRODUCING FATTY ACID METHYL ESTERS |
| FR2696185B1 (en) * | 1992-09-25 | 1994-12-02 | Inst Francais Du Petrole | Improved process for the production of esters from fatty substances of natural origin. |
| US5525136A (en) * | 1994-09-06 | 1996-06-11 | Rosen; Richard M. | Gasketed multi-media air cleaner |
| US6965044B1 (en) * | 2001-07-06 | 2005-11-15 | Iowa State University Research Foundation | Method of converting free fatty acids to fatty acid methyl esters with small excess of methanol |
| US20040074760A1 (en) * | 2002-10-17 | 2004-04-22 | Carnegie Mellon University | Production of biofuels |
| MY150129A (en) * | 2004-04-09 | 2013-11-29 | Archer Daniels Midland Co | Method of preparing fatty acid alkyl esters from waste or recycled fatty acid stock |
| JP2005350632A (en) * | 2004-06-14 | 2005-12-22 | Electric Power Dev Co Ltd | Method for producing biodiesel fuel |
| SG139562A1 (en) * | 2006-07-11 | 2008-02-29 | W J E Invest Ltd | Biofuel(s) |
-
2007
- 2007-07-30 WO PCT/SG2007/000224 patent/WO2008016330A2/en not_active Ceased
- 2007-07-31 US US11/831,535 patent/US20080047194A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| US20080047194A1 (en) | 2008-02-28 |
| WO2008016330A3 (en) | 2009-06-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2008016330A2 (en) | Bio formula to substitute diesel fuel | |
| Zahid et al. | Production of fuel additive solketal via catalytic conversion of biodiesel-derived glycerol | |
| US8192696B2 (en) | System and process of biodiesel production | |
| Bhutto et al. | Progress in the production of biomass-to-liquid biofuels to decarbonize the transport sector–prospects and challenges | |
| Virmond et al. | Valorization of agroindustrial solid residues and residues from biofuel production chains by thermochemical conversion: a review, citing Brazil as a case study | |
| Peng et al. | Extremely low sulfuric acid catalyst system for synthesis of methyl levulinate from glucose | |
| Alhassan et al. | Catalytic upgrading of waste tire pyrolysis oil via supercritical esterification with deep eutectic solvents (green solvents and catalysts) | |
| BE886588A (en) | ALCOHOL PRODUCTION PROCESS | |
| US20100294643A1 (en) | Process for the selective de-oxygenation of biomass | |
| Martín et al. | Simultaneous optimization and heat integration for the coproduction of diesel substitutes: Biodiesel (FAME and FAEE) and glycerol ethers from algae oil | |
| CN101875845A (en) | Process and special device for joint production of bio-oil and biochar by using crop straw | |
| Win et al. | Sustainable waste-to-energy technologies: Transesterification | |
| Yang et al. | Production of crude bio-oil via direct liquefaction of spent K-Cups | |
| Bertau et al. | Methanol utilisation technologies | |
| WO2008143593A2 (en) | Bbn 100 to substitute diesel fuel | |
| Bloch et al. | Fatty acid esters in Europe: market trends and technological perspectives | |
| CA2729659C (en) | Conversion of glycerol to naphtha-range oxygenates | |
| Blanco-Cejas et al. | Towards greener furfural: evaluating the technical, economic and environmental feasibility of heterogeneous catalysis in biomass conversion | |
| Ohia et al. | Hydrolysis of cellulose wastes: Feasibility of fuel ethanol as alternative to gasoline from petroleum as a usable energy source in Nigeria | |
| US National Alcohol Fuels Commission | Fuel alcohol: an energy alternative for the 1980s: appendix | |
| CN107446631A (en) | A kind of environment protection type biological liquid fuel and preparation method thereof | |
| Pal et al. | Waste Biomass Conversion in Useful Various Chemicals | |
| US20090031618A1 (en) | Vacuum Distillation Process | |
| Shin et al. | Crude oil production and classification of organic compounds on super-critical liquefaction with rice hull | |
| CN102796573A (en) | Low-freezing biodiesel combined fuel and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| 121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 07794238 Country of ref document: EP Kind code of ref document: A2 |
|
| NENP | Non-entry into the national phase |
Ref country code: DE |
|
| NENP | Non-entry into the national phase |
Ref country code: RU |
|
| 122 | Ep: pct application non-entry in european phase |
Ref document number: 07794238 Country of ref document: EP Kind code of ref document: A2 |