KR101183703B1 - Catalysts for hydrofined biodiesel and method for preparing the same - Google Patents

Abstract

The present invention relates to a catalyst for producing a biodiesel and a method for producing a biodiesel using the same, and more particularly, to a catalyst for producing a biodiesel, in which a catalyst used in a hydrogenation reaction or a carboxylation reaction is supported as an active ingredient in a strong water-resistant carrier. will be.
The catalyst for producing biodiesel according to the present invention can increase the durability of the catalyst by preventing the deactivation of the catalyst by water, which is a by-product generated during the HBD process, by using a carrier having a strong water resistance.

Description

Catalyst for biodiesel production and biodiesel production method using the same {Catalysts for hydrofined biodiesel and method for preparing the same}

The present invention relates to a catalyst for producing a biodiesel and a biodiesel manufacturing method using the same, and more particularly, to a catalyst having a high water resistance as a catalyst used for producing a biodiesel.

As high oil prices continue, the development of alternative energy resources and the need for reduction of greenhouse gases has emerged globally, leading to the development of bioenergy resources. Furthermore, as the supply of biodiesel in Korea and abroad increases due to tax and legislation worldwide, the bioenergy market is growing at an annual rate of 8-12%.

Representative technology for producing diesel oil from biomass is a technique for manufacturing Fatty Acid Methyl Ester (FAME). In addition to the advantages of alternative energy obtained from biomass, FAME has the advantage of higher cetane number compared to diesel oil obtained from conventional mineral oils in terms of physical properties, but has a disadvantage of low oxidation stability and high manufacturing cost.

Presented as the next generation technology is Hydrofined Bio-Diesel (HBD), which is prepared by directly hydrogenating triglyceride through hydrogenation reaction. The production cost of HBD is higher than that of diesel obtained from mineral oil, but the production cost is low compared to the conventional FAME, and the oxidation stability is relatively high because of the hydrogenation process.

And cetane number has the advantage of producing high-quality diesel oil close to 100. In addition, in terms of energy efficiency and greenhouse gas reduction, HBD fuel has the most advantages over mineral oil and FAME.

However, the biggest problem with the HBD process is that it is difficult to maintain the long term activity of the catalyst. Current HBD process uses a conventional catalyst for the hydrogenation process, the conventional hydrogenation catalyst has the disadvantage that the catalyst activity gradually decreases because the carrier is washed off by the water generated as a by-product in the HBD catalyst reaction. In order to solve this problem, a method of minimizing catalyst deactivation by changing the operating conditions of the process such as adding a small amount of feed to mineral oil without using 100% triglyceride has been applied.

There are two main processes of manufacturing HBD. One is a process consisting of only a hydrotreating process, and the other is a process in which an isomerization process is attached to a rear end of the hydrogenation process.

Hydro-treating in HBD is used to hydrogenate fat or fatty acid through hydrogenation reaction, and similar terms are used by mixing hydrogenation, deoxygenation (deoxidation), hydrodeoxygenation, decarboxylation and decarbonylation. Decarboxylation and decarbonylation are used interchangeably with the terminology of hydrogenation in the production of HBD because hydrogenation occurs as one carbon in the fat or fatty acid in the feed escapes.

In general, vegetable oil used as feed for bio-diesel is composed of triglycerides. Hydrogenation of these ester-type triglycerides yields a C15-C18 paraffin material, which can be used as biodiesel as the boiling point of this material falls within the diesel range. However, because paraffin diesel has a high pour point, it may be treated with isomerization to improve the low temperature stability of HBD in order to maintain liquid at low temperatures. Currently, biodiesel is used only a few percent compared to conventional petroleum diesel, and thus isomerized selectively as needed.

There are literatures that disclose HBD manufacturing techniques using hydrotreating, and US 4,992,605 uses crude palm oil as a feed to produce biodiesel using CoMo, NiMo, or transition metals with existing commercial hydrotreating catalysts. The process is starting.

In US 2007/0175795, Ni, Co, Fe, Mn, W, Ag, Au, Cu, Pt, Zn, Sn, Ru, Mo, Sb, V, Ir, Cr, Pd as a component of a catalyst for hydrogenation of triglycerides It is disclosed that it can be used.

US Pat. No. 7,232,935 discloses a catalytic process for producing HBD using a vegetable oil as a feed followed by an isomerization step after the hydrogenation step.

US 7279018 discloses a patent for producing a product by mixing about 0-20% of an oxide with hydrogenated isomerized HBD.

US 2007/0010682 also includes a hydrotreating process and an isomerization process, wherein the feedstock contains at least 5% by weight of free fatty acids and diluent, and the diluent: feedstock ratio is limited to 5-30: 1.

US 20060207166 discloses a process in which a hydrogenation process and an isomerization process are performed in one step using a catalyst having a metal supported on a carrier having acidity.

As described above, in order to produce HBD, at present, an existing commercial hydrogenation catalyst can be used without a specialized hydrogenation catalyst or an improvement can be applied to the production of HBD. Conventional commercial hydrogenation catalysts have generally been applied with a substance such as an alumina carrier or silica alumina as a carrier.

However, when a commercial hydrogenation catalyst using an existing alumina or silica alumina carrier is used as a catalyst for the production process of HBD, the initial activity and selectivity are high, and there seems to be no problem in application. There was a problem of low stability.

Prior arts attempting to solve these problems are attempting to increase the durability of the catalytic reaction even a little by controlling the operation of the process such as recycling unreacted HBD fraction, but have not found a fundamental solution to the problem. The situation is increasing the durability of the catalyst at the level.

In order to overcome the above problems, an object of the present invention is to provide a catalyst for producing biodiesel with high catalyst durability and high activity.

It is also an object of the present invention to provide a method for producing biodiesel using the catalyst.

In addition, another object of the present invention is to provide a biodiesel produced by the above production method.

One embodiment of the present invention for achieving the above object is an embodiment of the present invention provides a catalyst for producing a bio-diesel is supported on the catalyst used in the hydrogenation reaction or carboxylation reaction as an active ingredient in a strong water-resistant carrier.

One embodiment of the present invention provides a catalyst for producing a biodiesel containing a Group VIB metal as an active ingredient in a carrier having a strong water resistance.

Another embodiment of the present invention provides a catalyst further comprising a group VIB or VIIB metal to group VIB metal as an active ingredient in a strong water-resistant carrier.

Another embodiment of the present invention provides a catalyst for producing biodiesel, wherein the water-resistant catalyst carrier is zirconia, titania, aluminum phosphate, niobia, zirconium phosphate, titanium phosphate, silicon carbide, carbon, or a mixture thereof.

Another embodiment of the present invention provides a catalyst for producing biodiesel, wherein the metal group VIB is Mo or W and comprises 0.1 to 70% by weight of the active ingredient.

Another embodiment of the present invention, the metal group VIII is Ni, Pd, or Pt, and provides a catalyst for producing biodiesel, characterized in that contained in 0 to 60% by weight of the active ingredient.

In another embodiment of the present invention, the metal VIIB group is Co, Ru, Fe, Mn, or Ir, and provides a catalyst for producing biodiesel, characterized in that it comprises 0 to 60% by weight of the active ingredient.

Another embodiment of the present invention, the Group VIB metal provides a catalyst for producing biodiesel, characterized in that containing 1 to 40% by weight relative to the carrier.

Another embodiment of the present invention, the Group VIII or VIIB metal catalyst for producing biodiesel, characterized in that containing 1 to 20% by weight relative to the carrier.

Another embodiment of the present invention, in the presence of the catalyst for producing biodiesel, provides a method for producing biodiesel through a hydrogenation reaction or a decarboxylation reaction.

Another embodiment of the present invention, the biodiesel production is a biodiesel, characterized in that the feed to the biomass of vegetable oil, vegetable fat, animal fat, fish oil, renewable fat, vegetable fatty acid, animal fatty acid or a mixture thereof Provide a way to.

Another embodiment of the present invention, in the case of the fat, the number of carbons constituting each chain of triglyceride is 1 to 28 fat, the fatty acid, characterized in that the number of carbon 1 to 28 fatty acids It provides a method for producing a biodiesel.

In another embodiment of the present invention, the biodiesel production provides a method for producing biodiesel, characterized in that additionally mixed with one or more hydrocarbon mixtures (0 to 99%) in addition to the biomass as a feed. do.

Another embodiment of the present invention, the process of pre-processing the feed through the hydrogenation process, the process of separating the unreacted hydrogen after the hydrogenation deoxidation reaction, the process of cooling, separating the generated hydrocarbon (hydrocarbon), adding the isomerization function It provides a method for producing biodiesel through a process including an isomerization process.

Another embodiment of the present invention provides a biodiesel produced by the biodiesel manufacturing method.

The biodiesel production catalyst according to the present invention can increase the durability of the catalyst by solving the catalyst leaching problem, while having a high long-term activity during HBD production.

1 is a flowchart of an HBD process when 100% vegetable oil is used as a feed.
2 is a process flowchart used when a hydrocarbon is mixed with vegetable oil as a feed.

Hereinafter, the present invention will be described in detail.

In the case of using a commercial hydrogenation catalyst in the HBD manufacturing process, long-term stability was a problem, as described above, the prior art tried to overcome the problem through the process operation control, but it was insufficient.

The inventors of the present invention confirmed the root cause of the durability of the catalyst, not the process operation control method, which is that when the conventional commercial hydrogenation catalyst is applied directly to the HBD manufacturing process, water is generated by side reactions, As the hydrogenation catalyst component melted by water, it was found that the catalytically active point collapsed and the deactivation proceeded.

Based on this, the inventor of the present invention minimized the deactivation of the catalyst by the water generated by the product by introducing a high dispersion of the active point having a hydrogenation function to the carrier which is resistant to water masses. In the case of using a conventional commercial hydrogenation catalyst was confirmed to maintain the long-term catalyst activity more than two times.

Vegetable oil is mainly composed of triglycerides. As shown in the figure below, normal paraffins and hydrogen by-products are equivalent to C ₁₄ -C ₁₈ triglycerides by hydrogen and propane, H ₂ O, CO , CO ₂ Etc. are generated.

At this time, the generated paraffins are C ₁₄ ～ C ₁₈ and are referred to as HBD because they correspond to diesel oil. The H ₂ O produced by the reaction necessarily involves a reaction of dissolving the catalyst component. Using a commercially available hydrogenation catalyst, Group III + Group IV metal / carrier catalyst, the rate of H 2 O generation in the HBD reaction is about 10 wt%. In the early stage of the reaction, the catalyst component dissolves little, but after a certain period, the phenomenon of rapid washing occurs (Leaching effect) occurs, resulting in rapid catalyst deactivation.

In the present invention, in order to solve this problem, the catalyst material used in the hydrogenation reaction or the carboxylization reaction is supported on a strong water-resistant carrier to provide a catalyst having high durability and high catalytic activity of the catalyst.

Strongly water-resistant carriers used in the present invention are zirconia, titania, aluminum phosphate, niobia, zirconium phosphate, titanium phosphate, silicon carbide, carbon or mixtures thereof.

The present invention is a specialized catalyst for producing diesel oil through hydrogenation or decarboxylation reaction from biomass (HBD, Hydrofined Bio-diesel), zirconia, titania, aluminum phosphate, niobia, zirconium phosphate, titanium phosphate, silicon carbide It is a catalyst in which an active substance having a hydrogenation function or a carboxyl leaving function is added to a carrier having a high water resistance such as, carbon or a mixture thereof. The present invention prevents the deactivation of the catalyst by water, which is a by-product generated during the HBD process, by using a carrier having a high water resistance, thereby dramatically increasing the durability of the catalyst.

The strong water-resistant catalyst used in the present invention is applicable not only to the HBD process but also to the hydrogenation reaction or the carboxyl leaving reaction using alumina, in which water is generated and the durability of the carrier is reduced.

When the catalyst of the present invention is used in the HBD reaction, the catalyst used for the hydrogenation reaction or carboxylization reaction can be used without limitation, but a catalyst for producing biodiesel in which a group VIB metal is supported as an active ingredient can be used.

In addition, the present invention may use a catalyst further comprising a group VIB or VIIB metal to the group VIB metal as an active ingredient in a strong water-resistant carrier.

As the active ingredient used in the present invention, Group VIB metal is more preferably Mo or W, Group VIII metal is Ni, Pd or Pt, Group VIIB Group Co, Ru, Fe, Mn, or Ir, but more preferably It is not limited.

Group VIB metal of the active ingredient of the present invention is contained in 0.1 to 70% by weight, the catalyst activity is very low when it is supported at 0.1% by weight or less, it does not act as a catalyst, when the VIB group is supported, the oxidation state As it is supported on the catalyst, it is difficult to support more than 70% by weight based on oxide. Preferably, Group VIB metal is used in an amount of 1 wt% to 40 wt%.

Group VIII metal or Group VIIB metal of the active ingredient of the present invention is included in 0 to 60% by weight, because it is difficult to support more than 60% by weight. Group VIII metal or Group VIIB metal is preferably used at 0 to 20% by weight.

Biodiesel production of the present invention biodiesel production may use the biomass of vegetable oil, vegetable fats, animal fats, fish oil, renewable fats (in English), vegetable fatty acids, animal fatty acids or mixtures thereof as a feed.

In the case of the fat, the number of carbons constituting each chain of the triglyceride is 1 to 28 fats, and in the case of the fatty acid, it is preferable to use fatty acids having 1 to 28 carbons, but is not limited thereto.

Biodiesel manufacturing can be used by mixing one or more hydrocarbon mixtures (0 to 99%) in addition to biomass as feed, preferably kerosene, diesel, LGO, recycled HBD, but is not limited thereto. .

The HBD manufacturing process includes pretreatment of the feed through hydrogenation, separation of unreacted hydrogen after hydrodeoxidation, cooling and separation of generated hydrocarbons, and addition of isomerization processes. It may include, but can be added or subtracted one or two steps according to the purpose of course.

Although a process of treating 100% vegetable oil as a feed is exemplarily described in FIG. 1, the present invention is not limited thereto.

2 is a process flow chart used when a hydrocarbon is mixed with vegetable oil as a feed. The difference is that a fractionator for separating hydrocarbons is included when using 100% vegetable oil.

A blend of 1% DMDS in vegetable oil is used as the feed, which is simultaneously introduced into the HBD reactor and hydrogenated. The reactants are distilled from the stripper and sorted by boiling point to extract HBD, and the rest is recycled.

Hereinafter, an HBD-specific catalyst prepared using the technology of the present invention and a method of producing biodiesel through a hydrogenation process from biomass using the same will be described in detail as follows.

Example  One: Mo Of ZrO Preparation of ₂ Catalyst

A catalyst having about 10 wt% molybdenum was prepared using ZrO 2 having a diameter of 1 mm as a carrier.

Mo precursor used in the preparation was Ammonium heptamolybdate tetrahydrate (hereinafter referred to as "AHM"), and an aqueous solution prepared by dissolving AHM in distilled water was impregnated in a ZrO₂ carrier, and then dried at 150 ° C. for 2 hours and then at 500 ° C. for 2 hours. Mo / ZrO₂ was produced by continuous firing for a while (Molybdenum precursors in various forms other than AHM may be used, and the molybdenum metal precursor is not limited to AHM.)

6 cc of catalyst prepared according to the above procedure was charged into a cylindrical reactor, and then heated to 400 ° C. while flowing a reaction pressure of 45 bar and H 2 flow at a rate of 16 cc / min at room temperature, and pretreated for 3 hours when reaching 400 ° C. It was.

The soybean oil containing 1% DMDS (di-Methyl Disulfide) as feed was prepared using the pre-treated Mo / ZrO₂ catalyst at a reaction temperature of 350 ° C., a reaction pressure of 30 bar, and 100 cc / min of hydrogen. The reaction was carried out at a rate of 0.1 cc / min (LHSV = 1). Samples were sampled every 8 hours, and the reaction properties of the obtained product were simdist. The leaching of the catalyst was confirmed by ICP analysis. The results are shown in Tables 1 and 2.

Example  2: Nimo Of ZrO Preparation of ₂ Catalyst

A catalyst was prepared using ZrO 2 having a diameter of 1 mm as a carrier so that molybdenum was about 10 wt% and Ni was about 3 wt%. AHM was used as the Mo precursor used in the preparation, and Nickel nitrate hexahydrate (hereinafter, "NNH") was used as the Ni precursor, but various precursors may be used in the case of Mo and Ni metals, but are not limited thereto.

NiMo / ZrO₂ catalysts were prepared in the following order.

First, an aqueous solution prepared by dissolving AHM in distilled water was impregnated in a ZrO₂ carrier, and then dried at 150 ° C. for 2 hours, and subsequently calcined at 500 ° C. for 2 hours to prepare Mo / ZrO₂.

After NNH was dissolved in distilled water, the Mo / ZrO₂ catalyst was impregnated, dried at 150 ° C. for 2 hours, and subsequently calcined at 500 ° C. for 2 hours to prepare a NiMo / ZrO₂ catalyst.

Except for changing the pretreatment temperature to 320 degrees, the pretreatment and reaction was carried out in the same manner as in Example 1, the results are shown in Table 1 and Table 2.

Example  3: CoMo Of TiO Preparation of ₂ Catalyst

A catalyst was prepared using TiO 2 having a diameter of 1 mm as a carrier so that Mo was about 10 wt% and Co was about 3 wt%. AHM was used as the Mo precursor used in the preparation, and cobalt nitrate hexahydrate was used as the Co precursor (Mo, Co metal can be used in various precursors, but not limited to the precursor).

First, AHM was dissolved in distilled water, impregnated in a TiO₂ carrier, and then dried at 150 ° C. for 2 hours, and subsequently calcined at 500 ° C. for 2 hours to prepare Mo / TiO₂.

Cobalt nitrate hexahydrate was dissolved in distilled water, impregnated into the prepared Mo / TiO₂ catalyst, dried at 150 ° C. for 2 hours, and then calcined continuously at 500 ° C. for 2 hours to prepare a CoMo / TiO₂ catalyst. Pretreatment and reaction were carried out in the same manner as in Example 2, and the results are shown in Tables 1 and 2.

Example  4: NiW Of TiO Preparation of ₂ Catalyst

Using a TiO 2 having a diameter of 1 mm as a carrier, a catalyst was prepared such that tungsten was about 10 wt% and Ni was about 3 wt%. AHM was used as the W precursor used in the preparation, and NNH was used as the Ni precursor. In the case of W and Ni metals, various precursors may be used, and the present invention is not limited thereto.

NiW / TiO₂ catalysts were prepared in the following order.

An aqueous solution prepared by dissolving AMT in distilled water was impregnated in a TiO₂ carrier, dried at 150 ° C. for 2 hours, and then calcined continuously at 500 ° C. for 2 hours to prepare a W / TiO₂ catalyst.

After NNH was dissolved in distilled water, the W / TiO₂ catalyst was impregnated, dried at 150 ° C. for 2 hours, and subsequently calcined at 500 ° C. for 2 hours to prepare a NiW / TiO₂ catalyst.

Pretreatment and reaction were carried out in the same manner as in Example 1, and the results are shown in Tables 1 and 2.

Example  5: Nimo Preparation of A / C Catalyst

The catalyst was prepared using carbon having a diameter of 1 mm as a carrier so that molybdenum is about 15 wt% and Ni is about 5 wt%. AHM was used as the Mo precursor used in the preparation, and NNH was used as the Ni precursor (Mo, Ni metal may use various precursors, and the present invention is not limited thereto.)

NiMo / carbon catalysts were prepared in the following order.

First, an aqueous solution prepared by dissolving AHM and NNH in distilled water was impregnated in a carrier to carbon, and then dried at 300 ° C. for 2 hours to prepare a NiMo / C catalyst.

Pretreatment and reaction were carried out in the same manner as in Example 2, and the results are shown in Tables 1 and 2.

Example  6: Nimo Of AlPO4  Preparation of the catalyst

The catalyst was prepared using aluminum phosphate (AlPO 4) as a carrier such that molybdenum is about 15% by weight and Ni is about 5% by weight. The precursors of Ni and Mo are the same as in Example 2.

NiMo / AlPO 4 catalyst was prepared in the following order.

First, the aqueous solution prepared by dissolving AHM and NNH in distilled water was impregnated in an aluminum phosphate carrier, and then dried for 2 hours at 150 ° C., followed by pretreatment and reaction as in Example 2, and the results are shown in Table 1 and Table 2. It was.

Example  7: Nimo Of Nb2O5  Preparation of the catalyst

Using niobium oxide as a carrier, a catalyst was prepared such that molybdenum was about 7% by weight and Ni was about 2% by weight. The precursors of Ni and Mo are the same as in Example 2.

The NiMo / Nb 2 O 5 catalyst was impregnated under the same conditions as in Example 6, and pretreated and reacted under the same conditions as in Example 2. The results are shown in Table 1 and Table 2.

Comparative example  One: Nimo Of Al Preparation of ₂O₃ Catalyst

A catalyst was prepared using Al 2 O 3 having a diameter of 1 mm as a carrier so that molybdenum was about 10 wt% and Ni was about 3 wt%. AHM was used as the Mo precursor used in the preparation, and NNH was used as the Ni precursor, but various precursors may be used in the case of Mo and Ni metals, and the present invention is not limited thereto.

NiMo / Al₂O₃ catalysts were prepared in the following order.

First, an aqueous solution prepared by dissolving AHM in distilled water was impregnated into an Al₂O₃ carrier, and then dried at 150 ° C. for 2 hours, and subsequently calcined at 500 ° C. for 2 hours.

Mo / Al2O₃ was prepared.

After dissolving 3.06 g of NNH in distilled water, the Mo / Al₂O₃ catalyst was impregnated, dried at 150 ° C. for 2 hours, and subsequently calcined at 500 ° C. for 2 hours to prepare a NiMo / Al₂O₃ catalyst.

Pretreatment and reaction were carried out in the same manner as in Example 2, and the results are shown in Tables 1 and 2.

Comparative example  2: CoMo Of Al Preparation of ₂O₃ Catalyst

A catalyst was prepared using Al 2 O 3 having a diameter of 1 mm as a carrier so that Mo was about 10 wt% and Co was about 3 wt%. AHM was used as the Mo precursor used in the preparation, and cobalt nitrate hexahydrate was used as the Co precursor. However, in the case of Mo and Co metal, various precursors may be used, and the present invention is not limited thereto.

First, AHM was dissolved in distilled water, impregnated in an Al₂O₃ carrier, and then dried at 150 ° C. for 2 hours, and subsequently calcined at 500 ° C. for 2 hours to prepare Mo / Al₂O₃.

Cobalt nitrate hexahydrate was dissolved in distilled water, impregnated into the prepared Mo / Al₂O₃ catalyst, dried at 150 ° C. for 2 hours, and then calcined continuously at 500 ° C. for 2 hours to prepare a CoMo / Al₂O₃ catalyst.

Pretreatment and reaction were carried out in the same manner as in Example 2, and the results are shown in Tables 1 and 2.

In the results shown in Table 1, the initial reactivity was good for the catalyst using Al₂O₃ as the carrier, but the yield decreased rapidly as the reaction time elapsed. On the other hand, in the case of a catalyst using a zirconia, titania, carbon, aluminum phosphate or niobia as a carrier, it can be seen that not only the initial reaction performance but also the long-term reaction performance is superior to the alumina supported catalyst. In particular, as shown in the table, the catalyst using zirconia, titania, carbon, aluminum phosphate, or niobia as a carrier has excellent water resistance and shows little catalyst dissolution. However, in the case of a catalyst using alumina as a carrier, the catalyst and carrier component As the reaction time elapses, the degree of dissolution of the catalyst and carrier components rapidly increases.

Claims (16)

It is a catalyst for producing biodiesel, in which a catalyst used for hydrogenation or carboxylization reaction is supported as an active ingredient on a strong water-resistant carrier,
The water resistant carrier is zirconia, titania, aluminum phosphate, niobia, zirconium phosphate, titanium phosphate, silicon carbide, carbon or mixtures thereof, and the active ingredient is Mo, W, Ni, Co, Ru, Fe or their Catalyst for producing biodiesel, characterized in that the mixture. delete delete delete The catalyst for producing biodiesel according to claim 1, wherein Mo or W is contained in an amount of 0.1-70% by weight of the active ingredient. The catalyst for producing biodiesel according to claim 1, wherein the Ni is included in up to 60% by weight of the active ingredient. The catalyst for producing biodiesel according to claim 1, wherein the Co, Ru, or Fe is included in up to 60% by weight of the active ingredient. delete delete A process for producing biodiesel via hydrogenation or decarboxylation in the presence of a catalyst according to claim 1. The biodiesel according to claim 10, wherein the biodiesel production is a biomass of a vegetable oil, vegetable fat, animal fat, fish oil, recycled fat, vegetable fatty acid, animal fatty acid, or a mixture thereof. How to manufacture diesel. 12. The biodiesel according to claim 11, wherein the fat is a fat having 1 to 28 carbons constituting each chain of triglycerides, and the fatty acid is a fatty acid having 1 to 28 carbons. How to manufacture. The method of claim 10, wherein the biodiesel production is a method for producing a biodiesel, characterized in that further mixing up to 99% by weight of one or more petroleum oil in addition to the biomass feed. The method of claim 13, wherein the petroleum fraction comprises kerosene, diesel, light gas oil (LGO), or recycled hydrofined bio-diesel (HBD). delete Biodiesel prepared according to claim 10.

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