WO2008143593A2 - Bbn 100 to substitute diesel fuel - Google Patents
Bbn 100 to substitute diesel fuel Download PDFInfo
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- WO2008143593A2 WO2008143593A2 PCT/SG2008/000181 SG2008000181W WO2008143593A2 WO 2008143593 A2 WO2008143593 A2 WO 2008143593A2 SG 2008000181 W SG2008000181 W SG 2008000181W WO 2008143593 A2 WO2008143593 A2 WO 2008143593A2
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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
- 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
-
- 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
Definitions
- This invention is regarding a production process of BBN (biofuel) further- on called as "BBN 100", as an alternative material to substitute diesel fuel originated from vegetables in the form of palm coconut oil waste or Jatropha Curcas oil waste.
- BBM fuel oil material
- BBM biofosil
- BBM biofosil
- BBN biofuel
- BBN 100 an alternative material of Diesel Fuel originated from vegetables which is of palm coconut waste or Jatropha curcas oil waste.
- the object of the current invention primarily in regard to the production process of BBN 100 (biofuel), as an alternative material of diesel fuel, essentially covers some stages.
- R1A, R1B, R1C 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 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.
- VWO which is the bait of oil waste originated from fruits/palm coconut or jatropha
- E1 evaporator 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.
- PR1 Pre Reactor Reserved
- 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 E ⁇ 1, and further-on distilled the same way as the initial D1 stage the bottom/liquid fraction, which is the mixture of Bio Diesel and Glycerine through the reboiler at temperature 100 * C, in liquid condition, being recovered/withdrawn through D3 distillation column, reserved in the Reserve Tank Glycerol TB2.
- 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, in liquid condition, is proceeded to
- 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 BBN-100 Biofuel product having physico and chemical characteristics as follows:
- the chemical characteristics are of 6 maximum acid number
- Figure 1 is a stream diagram of BBN-100 (biofuel) 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 BBN 100 (biofuel), 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.
- R1A, R1B, R1C Reactor FFA Treatment Unit Reactor
- R1A Treatment Unit Reactor being the mixing tank reactor, the kind/type 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 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 or jatropha) 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.
- 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 1 in liquid condition proceeded to R4 reactor.
- top fraction is water + soap + salt reserved in the TB5
- Biofuel BBN-100 the substitution of diesel fuel reserved in the Biofuel BBN-100 Product Tank.
- Such Biofuel BBN-100 product has a physico and chemical characteristics as the following:
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Liquid Carbonaceous Fuels (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
BBN 100 (biofuel) production process as an alternative material to substitute diesel fuel, essentially covers the following distillation stages: - refinery of oil waste originated from palm coconut or jatropha through distillation - the end-product proceeds into R1A, R1B, R1C reactor while adding methanol and sulphuric acid - the result is put in E1 evaporator, - the result is being proceeded into D1 distillation column to be distilled - methanol distillation result is retained in TB1 bait tank and proceeded into R3 tank, at the same time NaOH/KOH is included, - then to have VWO flow in (oil waste of fruits/palm coconut) which have been evaporated in E1 and reserved in PR1 (Pre Reactor Reserved), mixed and put into the R2A and R2B (Main Reactor CSTR) through M1 together with the mixture result of R3 - the result of R2A and R2B is then proceeded into PR2 (Pre Reactor Reserved), - then is proceeded into D2 distillation column for continued process in D1 so that D1 input becomes two that is D2 and E1, and hereafter distilled as in D1 initial stage - the bottom/liquid fraction, in the form of (glycerol + soap + methyl ester) through the reboiler, in liquid condition, is recovered/withdrawn through D3 distillation column, retained in TB2 Glycerol reserved tank, - at D3 distillation column, the top/vapour fraction, in the form of methanol through the condenser, in liquid condition is proceeded to TB2, methyl ester/biodiesel is proceeded into R4 Reactor, - at R4 neutralizing reactor being neutralized by adding sulphuric acid from TB3 tank (the sulphuric acid bait tank) and water from TB4 water reserve tank, processed as the second catalyst, which then being evaporated in E2, - the evaporation result, the top fraction consisting of water + soap + salt is retained in TB5 Dirty Water Reserved Tank, and the bottom fraction in the form of biodiesel 100 (futher-on called as Biofuel BBN-100 being the substitution of diesel fuel) is reserved in the Biofuel BBN-100 Product Tank.
Description
Description
BBN 100 TO SUBSTITUTE DIESEL FUEL
Invention in the technical sector
This invention is regarding a production process of BBN (biofuel) further- on called as "BBN 100", as an alternative material to substitute diesel fuel originated from vegetables in the form of palm coconut oil waste or Jatropha Curcas 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 BBM (biofosil) subsidy which is being accounted for to the selling BBM (biofosil) price, resulted in the high BBM (biofosil) price hike, so as to deeply affect almost all public levels, especially the lower level community. As we believe BBM (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 BBM (biofosil) substitutions being highlighted such as bricks, coals taken from plantation waste, biogas and others. BBM (biofosil) 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 biofossil 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 diesel fuel from alternative raw materials which could reduce the entire cost and sales price.
By implementing production process of BBN 100 (biofuel) as substitution of diesel fuel in accordance with the current invention, the obstacles mentioned above could be overcome or at least reduced significantly.
Invention sunnmary
The objective focus of the current invention is in regard to the production process of BBN (biofuel), further-on called "BBN 100", an alternative material of Diesel Fuel originated from vegetables which is of palm coconut waste or Jatropha curcas oil waste.
The object of the current invention, primarily in regard to the production process of BBN 100 (biofuel), as an alternative material of diesel fuel, essentially covers some stages.
- distillation of oil waste from palm coconuts or jatropha oil waste from TB6 by fitter press distillation (membrane kind of distillation, membrane plate distillation type)
- the result of 1000 kg distillation flow into R1A, R1B, R1C 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 VWO to proceed (which is the bait of oil waste originated from fruits/palm coconut or jatropha) 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 bottoni 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 EΞ1, and further-on distilled the same way as the initial D1 stage the bottom/liquid fraction, which is the mixture of Bio Diesel and Glycerine through the reboiler 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° C, 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 BBN-100 Biofuel the substitution of diesel fuel) restrained in BBN-100 BiofuelProduct Tank.
The BBN-100 Biofuel product having physico and chemical characteristics as follows:
Physico is in the form of yellow-brownish liquid
The chemical characteristics are of 6 maximum acid number
The above-mentioned characteristics have fully met the criteria as the alternative material for diesel fuel substitution.
Short description of the picture
Figure 1 is a stream diagram of BBN-100 (biofuel) 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 BBN-100 (biofuel) 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 BBN 100 (biofuel), 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 R1A, R1B, R1C Reactor (FFA Treatment Unit Reactor) being the mixing tank reactor, the kind/type 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 ύ mixing tank, wherein within the same time also included solid NaOH/KOH (1 - 1,5)% vWO 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 or jatropha) 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* C1 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* C1 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 Biofuel BBN-100 the substitution of diesel fuel) reserved in the Biofuel BBN-100 Product Tank.
Such Biofuel BBN-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 BBN 100 (biofuel) 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 distillation result flow in the R1A, R1B, R1C Reactor (F^A Treatment Unit Reactor) which is the mixing reactor, kind/type CSTR reactor in operation condition, temperature (60 - 70)* C1 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 20*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)% WVO 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 or jatropha) 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 methyl 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 651C, 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 200C, 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* C1 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 Biofuel BBN- 100 being the substitution of diesel fuel) is reserved in the Biofuel BBN-100 Product Tank.
Such Biofuel BBN-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 |
|---|---|---|---|
| IDP00200700247 | 2007-05-24 | ||
| ID20070247 | 2007-05-24 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2008143593A2 true WO2008143593A2 (en) | 2008-11-27 |
| WO2008143593A3 WO2008143593A3 (en) | 2011-09-09 |
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ID=40032302
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/SG2008/000181 WO2008143593A2 (en) | 2007-05-24 | 2008-05-14 | Bbn 100 to substitute diesel fuel |
Country Status (1)
| Country | Link |
|---|---|
| WO (1) | WO2008143593A2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011143728A1 (en) * | 2010-05-21 | 2011-11-24 | Petróleo Brasileiro S.A. - Petrobras | Method for producing aviation biokerosine and aviation kerosine composition |
| CN105270771A (en) * | 2015-11-20 | 2016-01-27 | 重庆恒宇华顿新能源开发有限公司 | Distributed control linkage oil storage tank with gas concentration detection function |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001012581A1 (en) * | 1999-08-18 | 2001-02-22 | David Gavin Brooke Boocock | Single-phase process for production of fatty acid methyl esters from mixtures of triglycerides and fatty acids |
| WO2006105306A2 (en) * | 2005-03-29 | 2006-10-05 | Arizona Chemical Company | Compostions containing fatty acids and/or derivatives thereof and a low temperature stabilizer |
-
2008
- 2008-05-14 WO PCT/SG2008/000181 patent/WO2008143593A2/en active Application Filing
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001012581A1 (en) * | 1999-08-18 | 2001-02-22 | David Gavin Brooke Boocock | Single-phase process for production of fatty acid methyl esters from mixtures of triglycerides and fatty acids |
| WO2006105306A2 (en) * | 2005-03-29 | 2006-10-05 | Arizona Chemical Company | Compostions containing fatty acids and/or derivatives thereof and a low temperature stabilizer |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011143728A1 (en) * | 2010-05-21 | 2011-11-24 | Petróleo Brasileiro S.A. - Petrobras | Method for producing aviation biokerosine and aviation kerosine composition |
| CN105270771A (en) * | 2015-11-20 | 2016-01-27 | 重庆恒宇华顿新能源开发有限公司 | Distributed control linkage oil storage tank with gas concentration detection function |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2008143593A3 (en) | 2011-09-09 |
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