U.S. patent application number 11/831535 was filed with the patent office on 2008-02-28 for bio formula to substitute diesel fuel.
Invention is credited to B.F. Prawoto.
Application Number | 20080047194 11/831535 |
Document ID | / |
Family ID | 38997593 |
Filed Date | 2008-02-28 |
United States Patent
Application |
20080047194 |
Kind Code |
A1 |
Prawoto; B.F. |
February 28, 2008 |
BIO FORMULA TO SUBSTITUTE DIESEL FUEL
Abstract
Methods for preparing a diesel substitute are disclosed. The
methods may include continuous processes from distillation of waste
vegetable oil, preparation of methanol, preparation of Na-methoxide
mixtures, reactions between distilled waste vegetable oil and
Na-methoxide mixtures, and separations of reaction products. A
biodiesel substitute having a brownish-yellow color and a maximum
acid number of 6 is also disclosed.
Inventors: |
Prawoto; B.F.; (JAKARTA
PUSAT, ID) |
Correspondence
Address: |
VOLPE AND KOENIG, P.C.
UNITED PLAZA, SUITE 1600
30 SOUTH 17TH STREET
PHILADELPHIA
PA
19103
US
|
Family ID: |
38997593 |
Appl. No.: |
11/831535 |
Filed: |
July 31, 2007 |
Current U.S.
Class: |
44/605 |
Current CPC
Class: |
Y02E 50/13 20130101;
C10L 1/026 20130101; C10G 2300/1011 20130101; Y02P 30/20 20151101;
Y02E 50/10 20130101 |
Class at
Publication: |
044/605 |
International
Class: |
C10L 1/00 20060101
C10L001/00 |
Foreign Application Data
Date |
Code |
Application Number |
Aug 1, 2006 |
ID |
P00200600449 |
Claims
1. A method of producing an alternative diesel substitute that
includes a methyl ester/biodiesel, the method comprising: (a)
distilling waste vegetable oil to obtain waste vegetable oil
distillate; (b) adding methanol and sulphuric acid to the
distillate to produce first reaction products; (c) subjecting the
first reaction products to evaporation; (d) distilling a first
portion of products obtained in step (c) to produce a bottom
fraction including methyl ester, and a top/vapor fraction including
methanol; (e) mixing methanol produced in step (d) with NaOH/KOH to
produce a Na-methoxide mixture; (f) homogenizing a second portion
of products obtained in step (c) and mixing the homogenized
products with Na-methoxide produced in step (e) to produce second
reaction products; (g) distilling the second reaction products to
produce a top/vapor fraction including methanol and a bottom
fraction including methyl ester/biodiesel and glycerol; (h)
distilling the methyl ester/biodiesel and glycerol obtained in step
(g) to produce a top fraction including glycerol and a bottom
fraction including methyl ester/biodiesel; (i) neutralizing the
methyl ester/biodiesel, and subjecting the neutralized methyl
ester/biodiesel to evaporation to produce a bottom fraction
including the alternative diesel substitute.
2. The method of claim 1, wherein the distillation of step (a) is
accomplished through membrane filtration.
3. The method of claim 1, wherein step (b) includes maintaining the
distillate, methanol, and sulphuric acid at 60-70.degree. C. and
atmospheric pressure for 60-120 minutes.
4. The method of claim 1, wherein the evaporation in step (c)
includes maintaining a temperature of 60-70.degree. C. at 20-60
mmHg for 60-90 minutes.
5. The method of claim 1, wherein the distilling of step (d) is
performed with a first distillation column operated at
60-70.degree. C. at 20-60 mmHg.
6. The method of claim 1, wherein the bottom fraction obtained in
step (d) also includes water, glycerol, and soap; the bottom
fraction is subjected to refluxing and the methyl ester is
separated from the water, glycerol, and soap.
7. The method of claim 1, further comprising condensing the
methanol in the top/vapor fraction produced in step (d) in a
condenser at 20.degree..
8. The method of claim 6, further comprising concentrating the
methanol to a concentration of 99%.
9. The method of claim 1, wherein the distilling step (g) is
performed with a second distillation column operated at
60-70.degree. C. at 20-60 mmHg.
10. The method of claim 1, further comprising concentrating the
methanol in the top/vapor fraction produced in step (g) in a
condenser at 20.degree.; and optionally combining the methanol of
step (g) with the methanol obtained in step (d) to produce combined
methanol, wherein the combined methanol is processed in the same
steps as the methanol of step (d).
11. The method of claim 1, wherein the bottom fraction including
methyl ester/biodiesel and glycerol in step (g) is reboiled prior
to step (h).
12. The method of claim 1, wherein the distilling of step (h) is
performed with a third distillation column operated at
60-70.degree. C. at 20-60 mmHg.
13. The method of claim 1, wherein the glycerol in the top fraction
of step (h) is transferred to a glycerol reserve tank.
14. The method of claim 1, further comprising reboiling the bottom
fraction including methyl ester/biodiesel of step (h) prior to step
(i).
15. The method of claim 1, wherein the neutralizing step in (i)
further comprises adjusting the pH to 5.5-6.5.
16. The method of claim 15, wherein the step of adjusting the pH is
accomplished by adding sulphuric acid.
17. The method of claim 16, wherein the sulphuric acid is 12 M and
is added at a volume corresponding to 1-1.5% of the methyl
ester/biodiesel volume.
18. The method of claim 1, wherein the neutralizing step in (i)
further comprises adding water.
19. The method claim 1, wherein the evaporating step in (i)
includes an evaporator operating at 60-70.degree. C. at 20-60 mmHg
for 60 minutes.
20. An alternative diesel substitute produced by the method of
claim 1.
Description
FIELD OF INVENTION
[0001] The invention relates to a bio formula which is an
alternative diesel fuel and originated from vegetables in the form
of palm coconut oil waste. The invention also relates to a process
for production of the bio formula.
BACKGROUND
[0002] Fuel has been always an issue in various countries and many
ways have been explored in search of alternative materials that
could substitute for current fuels. The current invention relates
to a substitute material suitable to operate a diesel engine, e.g.
a substitute diesel fuel.
[0003] Fuel oil material subsidies account for fossil fuel prices,
and result in fossil fuel price hikes. As a result, all public
levels, especially the lower level community are deeply affected by
fossil fuel availability. Since fossil fuel is a natural resource
that cannot be renewed, it is necessary and important to develop
alternatives or substitutes.
[0004] Many fossil fuel substitutes, such as bricks, coals taken
from plantation waste, biogas and others, have been highlighted.
Also, either obtaining fossil fuel from different raw materials, or
producing fossil fuel through chemical reaction processes,
distillation residues, thermal cracking, fractionalization and
other processes has been explored to meet the need for
alternatives. Many of these approaches are, however, costly due to
the supply of raw materials, additives, supporting materials,
catalysts, instrumentation, location, and so on. In most cases, the
alternatives or substitutes must go through difficult processing
stages. It especially difficult to maintain continued processes.
Even though the processes can be simplified, the result is product
quality and quantity below the maximum, that is, far from
anticipated adequate levels. Attempts to overcome these
deficiencies have resulted in inadequate product, especially for
public use.
[0005] In addition, the products made by these prior attempts to
overcome the deficiencies are not suitable for industrial use.
Needless to say, the products are useless and do not have economic
value.
[0006] The current invention, a substitute diesel fuel, is directed
to avoiding these obstacles and the resulting high prices for
fossil fuel. An alternative must be found to process a different
raw material for diesel fuel and, thus, obtain an alternative or
substitute diesel fuel. There is a need for innovators, willing to
express and to interact in their area and find alternatives to
produce diesel fuel from alternative raw materials. The
alternatives could reduce the entire cost of production and also
the sales price of the product.
[0007] The current invention includes bio formula 100 and a process
for its production. Bio formula 100 is a substitute for diesel
fuel. Through the use of bio formula 100 and the methods for its
production, the obstacles mentioned above may be reduced or
overcome.
SUMMARY
[0008] The invention herein relates to a method of producing an
alternative diesel substitute that includes a methyl
ester/biodiesel. The method includes distilling waste vegetable oil
to obtain waste vegetable oil distillate. Methanol and sulphuric
acid are added to the distillate to produce first reaction
products, which are subjected to evaporation. A first portion of
these products are distilled to produce a bottom fraction including
methyl ester, and a top/vapor fraction including methanol. A
portion of the methanol is mixed with NaOH/KOH to produce a
Na-methoxide mixture. A second portion of the first reaction
products are homogenized and the homogenized products are mixed
with a portion the Na-methoxide mixture to produce second reaction
products. The second reaction products are distilled to produce a
top/vapor fraction including methanol and a bottom fraction
including methyl ester/biodiesel and glycerol. The methyl
ester/biodiesel and glycerol fraction is further distilled to
produce a top fraction including glycerol and a bottom fraction
including the methyl ester/biodiesel. The methyl ester/biodiesel is
neutralized and subjected to evaporation to produce a bottom
fraction including the alternative diesel substitute.
[0009] The invention herein also relates to the alternative diesel
substitute produced by a method of producing an alternative diesel
substitute. The method includes distilling waste vegetable oil to
obtain waste vegetable oil distillate. Methanol and sulphuric acid
are added to the distillate to produce first reaction products,
which are subjected to evaporation. A first portion of these
products are distilled to produce a bottom fraction including
methyl ester, and a top/vapor fraction including methanol. A
portion of the methanol is mixed with NaOH/KOH to produce a
Na-methoxide mixture. A second portion of the first reaction
products are homogenized and the homogenized products are mixed
with a portion the Na-methoxide mixture to produce second reaction
products. The second reaction products are distilled to produce a
top/vapor fraction including methanol and a bottom fraction
including methyl ester/biodiesel and glycerol. The methyl
ester/biodiesel and glycerol fraction is further distilled to
produce a top fraction including glycerol and a bottom fraction
including the methyl ester/biodiesel. The methyl ester/biodiesel is
neutralized and subjected to evaporation to produce a bottom
fraction including the alternative diesel substitute.
BRIEF DESCRIPTION OF THE DRAWING
[0010] FIG. 1 is a stream diagram of B-100 formula production
process for a diesel fuel substitute which is in line with
embodiments of the current invention.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
[0011] As used herein, "bio formula 100," "BioFuel B-100," or
"B-100" refers to a substitute diesel fuel originated from
vegetables in the form of palm coconut oil waste (WVO).
[0012] A production process for B-100 is shown in FIG. 1 and
described as follows.
[0013] Embodiments of the current invention are directed to bio
formula 100 and its production process. Bio formula 100 can
function as an alternative or substitute for diesel fuel, and is of
solar origin. The production process may include the following
stages:
[0014] In a preferred embodiment, membrane distillation, and more
preferably membrane plate distillation is used in a preliminary
stage of the process. As shown in FIG. 1, stages from tank TB6 to
reactor R1 include distillation of palm coconut oil waste by a
membrane/filter press at 1 time/stage to obtain. As indicated, the
distillate is transferred to reactor R1, an FFA Treatment Unit
Reactor, which is a mixing tank reactor suitable for continuous
operation; for example a CSTR reactor. Reactor R1, in preferred
embodiments is double jacketed. In a preferred embodiment, reactor
R1 receives 1000 kg palm coconut oil waste distillate. In an
embodiment, the distillate is maintained at a temperature of
60-70.degree. C. at atmospheric pressure for 60-120 minutes. In a
preferred embodiment, this time is about 90 minutes. At this stage,
a volume of 99% methanol corresponding to 10-15% of the WVO volume
is added. A volume of 12 Molar sulphuric acid corresponding to
1-1.5% of the WVO volume is also added. In a preferred embodiment,
the final concentration of methanol in this step is 10.7%. Also,
sulphuric acid may be added in alternative amounts, including 25
kg.
[0015] The reaction products proceed to an evaporator E1. In an
embodiment, the evaporator E1 operates at a temperature of
60-70.degree. C. and a pressure of 20-60 mmHg (preferably 30-50
mmHg). In a preferred embodiment the temperature is about
65.degree. C. Evaporation may be carried out for 60-90 minutes.
[0016] The evaporated products proceed to a distillation column D1
and are distilled at 60-70.degree. C. (preferably 65.degree. C.)
and 20-60 mmHg (preferably 30-50 mmHg). The result of distillation,
in the bottom fraction, includes a methyl ester having a
temperature of 65-70.degree. C. (preferably 65.degree. C.). Liquid
methyl ester proceeds to tank TB5. A mixture of water, glycerol,
and soap is also in the bottom/liquid fraction and is refluxed from
a condenser and reboiler at 65-70.degree. C. (preferably 65.degree.
C.). The water, glycerol, and soap are transferred to the Dirty
Water Reserve Tank TB5 in liquid form.
[0017] The top/vapor fraction in distillation column D1 includes
methanol that is condensed as it travels through a 20.degree. C.
condenser. Methanol concentrated to 99% is retained in the TB1 bait
tank, which is a Stainless Steel tank. The volume of methanol could
be 800 mls or more, and in the embodiment where 1000 kg distillate
enters reactor R1, approximately 50 liters 99% methanol may be
obtained. The methanol proceeds to mixing tank R3. The amount of
methanol transferred is about 10-15% of the WVO, and solid NaOH/KOH
at about 1-1.5% of the WVO weight is added as catalyst at the same
time. In another embodiment, the NaOH/KOH measure may be 15-25 kg.
The contents are then mixed in the M1 mixing tank till a reaction
mixture is reached. The reactions include
methanol+NaOH/KOH.fwdarw.NaMethanol. A Na-Methoxide mixture is
obtained.
[0018] Then, evaporated WVO (the bait in the form of oil waste of
fruits/palm coconut) proceeds from the evaporator E1 to a Pre
Reactor Reserved PR1. To obtain homogeneity, the evaporated WVO is
retained in PR1 for 30-60 minutes (preferably 60).
[0019] A Methyl Ester is preferably obtained by combination of the
NaMethanol from reactor R3 with the WVO emerging from the Pre
Reactor PR1. These components are mixed in mixer M1 and then
transferred into reactors R2A and R2B. These reactors are the main
reactor (mixing rector tank), CSTR Main Reactor, and are the mixing
tanks for a continuous process.
[0020] The products obtained in R2A and R2B are removed through the
bottom part of the reactors, and preferably proceed into Pre
Reactor Reserved PR2 for optimal results. At this stage, the
products proceed into distillation column D2. The distillation
column D2 has Column Packing specifications and is operated at
65.degree. C. and 20-60 mmHg. The condenser/reboiler configuration
of the distillation column includes a distillation container in the
form of Shell and Tube, and the reboiler is a Reboiler Kettle.
[0021] The top/vapor fraction from distillation column D2 includes
methanol, which is condensed by passage through a 20.degree. C.
condenser. In liquid condition, the methanol fraction may be
transferred into distillation column D1 for continued processing.
In these embodiments, D1 receives two inputs of methanol, one from
evaporator E1 and one from distillation column D2. And the
continued processing of methanol from distillation column D2
proceeds similarly to the processing described above regarding
methanol leaving evaporator E1.
[0022] The bottom/liquid fraction from distillation column D2
includes a mixture of methyl ester (biodiesel) and glycerol. This
combination is processed in liquid condition through a reboiler at
65-100.degree. C. (preferably 65.degree. C.). This fraction is
recovered/withdrawn through D3 distillation column.
[0023] The D3 distillation column has Column Packing specifications
and may be operated at 65.degree. C. and 20-60 mmHg. In an
embodiment, this distillation is carried out for 60-90 minutes. The
top/vapor fraction of this column includes Glycerol, which is
condensed in a 20.degree. C. condenser. In liquid condition, this
fraction then proceeds to and is reserved in Glycerol Reserved Tank
TB2.
[0024] The bottom/liquid fraction of distillation column D3
includes the methyl ester/biodiesel. This product is processed
through a reboiler at 65.degree. C., and then proceeds to reactor
R4 in liquid condition.
[0025] Mixing tank R4 functions as neutralizing reactor. In an
embodiment, the mixing tank R4 operates at 30-40.degree. C.
(preferably 40.degree. C.) and atmospheric pressure, and the methyl
ester/biodiesel is processed for 60 minutes in this tank. The
methyl ester/biodiesel is neutralized from pH 10 to pH 5.5-6.5 by
adding 12 Molar sulphuric acid from a sulphuric acid bait tank. In
an embodiment, the volume of sulphuric acid added is one hundreth
that of the methyl ester volume, and in another embodiment the acid
volume ranges from 1-1.5% of the methyl ester. A volume of water
amounting to 10-15% of the methyl ester is also added, and the
water may be drawn from the TB4 water reserve tank. These are
processed as the second catalyst, and then evaporated in an
evaporator E2. The evaporator E2 operates at 65.degree. C. and
20-60 mmHg for 60 minutes.
[0026] The top fraction from evaporator E2 includes water, soap,
and salt, which is reserved in the TB5 Dirty Water Reserve Tank.
The bottom fraction is the biodiesel 100, which is reserved in the
BioFuel B-100 Product Tank TB 7.
[0027] A BioFuel B-100 product made by the above process is
physically a yellow-brownish liquid, and chemically has a preferred
maximum acid number of 6. These characteristics meet the criteria
as an alternate material for solar substitution.
[0028] It is understood, therefore, that this invention is not
limited to the particular embodiments disclosed, but is intended to
cover all modifications which are within the spirit and scope of
the invention as defined by the appended claims; the above
description; and/or shown in the attached drawings.
* * * * *