CN104120038A - Method for reducing oil acid value - Google Patents
Method for reducing oil acid value Download PDFInfo
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- CN104120038A CN104120038A CN201310148744.3A CN201310148744A CN104120038A CN 104120038 A CN104120038 A CN 104120038A CN 201310148744 A CN201310148744 A CN 201310148744A CN 104120038 A CN104120038 A CN 104120038A
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- oil plant
- alcohol
- monohydroxy
- acid
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- 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
Abstract
The invention discloses a method for reducing the oil acid value. The method includes subjecting an oil material, monohydric alcohol and a catalyst to mixing contact, wherein the catalyst is acid type ion exchange resin. The method for reducing the oil acid value provided by the invention can effectively reduce the oil acid value. While simplifying the technological process, the method can further acquire biodiesel with an acid value up to the BD100 acid value standard.
Description
Technical field
The present invention relates to a kind of method that reduces oilseed acid value.
Background technology
The main component of biofuel is lipid acid mono alkyl ester (abbreviation fatty acid ester), and it can be that triglyceride level and single hydroxyl alcohol (are generally low-carbon alcohol, as C by grease
1-C
8monohydroxy-alcohol) carry out transesterification reaction and obtain, also can obtain by the esterification of lipid acid and single hydroxyl alcohol.
CN101906355A discloses a kind of method of utilizing food waste recycling oil preparing biological diesel oil, and the method comprises the steps: first the waste cooking oil removing impurities processing of coming unstuck; Under the catalysis of the stock oil that acid-catalyzed esterification reaction waste cooking oil generates through degumming process at the vitriol oil, carry out acid-catalyzed esterification reaction with anhydrous methanol, the free fatty acids in stock oil is changed into biofuel; After acid-catalyzed esterification reaction, the glycerin fatty acid ester in stock oil carries out base-catalyzed transesterification with methyl alcohol and reacts under the effect of sodium hydroxide, and reaction product is biofuel and glycerine; The reacted reactant of base-catalyzed transesterification carries out settlement separate, and upper strata product water washing and rectification obtains biofuel, and lower floor's product obtains glycerine and methyl alcohol after processing.
CN101113358A discloses a kind of method of recycling sewer oil, and the method comprises that sewer oil is refining and utilizes refining sewer oil to react under complex acid catalyst and proper temperature with methyl alcohol, can obtain biofuel.Wherein, sewer oil is refining to be referred to: first sewer oil is filtered under 10-50 DEG C of condition, sewer oil after filtration carries out normal pressure dehydration or under 750mm mercury column, 50-100 DEG C condition after vacuum hydro-extraction under 105-120 DEG C of condition, add atlapulgite to decolour and purify, obtaining refining sewer oil.
CN1412278A discloses a kind of method that adopts acidic catalyst method preparing biological diesel oil from high acid value waste animal and plant oil, it adopts methyl alcohol and sulfuric acid as catalyzer, carry out according to the operation of dehydration, esterification and transesterify, phase-splitting, decolouring, raw material first dewaters under the vacuum of 60-100 DEG C, then, at 40-85 DEG C, the consumption of methyl alcohol and sulfuric acid is respectively 10-15% and the 2-6% of oil from high acid value waste animal and plant weight, carry out esterification and transesterification reaction 1.5-6 hour, separate fatty acid methyl ester phase, can obtain biofuel 90-125 DEG C of decolouring with atlapulgite.
The problem that acid catalysis exists is that speed of response is slower, in addition, has a large amount of spent acid, waste water generation.
DE3444893A1 discloses a kind of method that natural fat by containing free fatty acids and natural oil are prepared fatty acid alkyl ester, first, oil plant is carried out to pre-esterification treatment, with acid catalyst, normal pressure, 50-120 DEG C, free fatty acids and alcohol are carried out to esterification, then add the acid catalyst of leaving over pre-esterification in excessive base metal catalysts and carry out transesterification reaction.
Adopt base catalysis method, owing to conventionally containing free fatty acids in natural fats and oils, in the situation that free fatty acids exists, need to use excessive base metal catalysts, therefore cause the requirement of base metal catalysts larger.In addition, reaction can produce fatty acid soaps, easily causes fatty acid ester layer and glycerin layer separation difficulty.
Can be found out by aforesaid method, while adopting prior art to prepare biofuel, need to carry out pre-treatment to raw material, in order to make the requisite quality of biofuel, also need to take complicated aftertreatment, cause technical process long, facility investment is large.
Summary of the invention
The object of the present invention is to provide a kind of method that reduces oilseed acid value, the method can effectively reduce the acid number of oil plant.In simplification of flowsheet, acid number can further be obtained reach the biofuel of BD100 acid number standard.
The invention provides a kind of method that reduces oilseed acid value, the method comprises contacts oil plant, monohydroxy-alcohol and catalyst mix, and wherein, described catalyzer is acid-type ion-exchange resin.
According to method provided by the invention, adopt acid-type ion-exchange resin as catalyzer, to oil plant without the pre-treatment of carrying out acid number reduction, directly adopt method of the present invention can obviously reduce the acid number of oil plant, and adopt method of the present invention, without the processing of carrying out again acid number reduction to contacting reacted material, can obtain the biofuel that acid number is lower, simplify technical process.
Under preferable case, when adopting fixed-bed reactor or knockout tower to carry out oil plant, when the mixing and contacting reaction of monohydroxy-alcohol and catalyzer, gaseous state monohydroxy-alcohol and liquid state oiling be counter current contact under the existence of acid-type ion-exchange resin, oil plant flows from top to bottom, monohydroxy-alcohol moves from the bottom up, when oil plant starts to contact gaseous state monohydroxy-alcohol, the reaction of the two is easier to carry out, but along with the consumption of oil plant, the reaction of the two more and more difficulty is carried out, but, the more past current downflow of oil plant, the concentration of monohydroxy-alcohol is increasing, the concentration that is reactant is larger, be conducive to promote oil plant to carry out with reacting to positive dirction of monohydroxy-alcohol, thereby can effectively reduce the acid number of oil plant.And the reduction that adopts fixed-bed reactor or knockout tower to carry out oilseed acid value is while processing, can also obtain acid number and reach the biofuel of BD100 acid number standard.
Other features and advantages of the present invention are described in detail the embodiment part subsequently.
Embodiment
Below the specific embodiment of the present invention is elaborated.Should be understood that, embodiment described herein only, for description and interpretation the present invention, is not limited to the present invention.
Comprise oil plant, monohydroxy-alcohol and catalyst mix are contacted according to the method for reduction oilseed acid value of the present invention, wherein, described catalyzer is acid-type ion-exchange resin.
According to method provided by the invention, as long as described catalyzer is the acid number that acid-type ion-exchange resin can effectively reduce oil plant.Described acid-type ion-exchange resin can be any one conventional acid-type ion-exchange resin using well known by persons skilled in the art.But the present inventor finds through a large amount of experiments, in the time that described acid-type ion-exchange resin is styrene sulfonic acid type ion exchange resin, is more conducive to the reduction of oilseed acid value.In addition, in order better to realize object of the present invention, the acid amount of preferred described catalyzer is 1-5mmol/g, more preferably 1.2-3mmol/g, and more preferably 1.2-2mmol/g, can make the acid number of oil plant further reduce.The acid amount of described catalyzer adopts temperature programmed desorption(TPD) analytical method (NH
3-TPD) obtain.
In the present invention, described oil plant can be the grease of various routines, it can be for example biofuel crude product (conventionally containing triglyceride level, fatty acid ester and lipid acid etc.), also can be the various raw oil materials for the production of biofuel, as at least one in Vegetable oil lipoprotein, animal grease and microbial oil.Described Vegetable oil lipoprotein for example can comprise soybean oil, rapeseed oil, peanut oil, wunflower seed oil, plam oil, Oleum Cocois and come from the material that contains fatty group (comprising the tall oil producing in paper-making process) of fruit, stem, leaf, limb and the root of other various farm crop and wild plant.Described animal grease for example can comprise lard, butter, sheep oil, fish oil etc.Described oil plant can also be high-acid value grease, for example, can be frying oil, rotten waste oil, sewer oil or acidifying wet goods.Described acidification oil refers to that the byproduct soap stock that oil refining plant is produced carries out the oil that acidification obtains.Acidification oil is lipid acid in essence, wherein contains the Multiple components such as pigment and unacidified triglyceride level.The present invention can also adopt grease that unsaponifiable matter content is higher as oil plant, can reduce equally the acid number of oil plant.Described unsaponifiables refers to the material that can not play with sodium hydroxide or potassium hydroxide saponification reaction in grease.In described grease, the content of unsaponifiables for example can be for containing 0.1-10g unsaponifiables in grease described in every 100g.
According to method provided by the invention, can obtain low acid number oil plant to described oil plant without the pre-treatment of carrying out acid number reduction.Also there is no particular limitation for the acid number of described oil plant, for example, can be 0.8-200mgKOH/g.In the present invention, owing to adopting fixed-bed reactor or knockout tower, the gaseous state monohydroxy-alcohol that liquid state oiling is more and more denseer with concentration is contacted, and under the existence of acid-type ion-exchange resin catalyzer, be particularly suitable for high acid value oil plant to carry out the processing of acid number reduction.Preferably, to be applicable to acid number be the processing that the oil plant of 100-200mg KOH/g carries out acid number reduction to method of the present invention.Meanwhile, adopt method provided by the invention, utilize the oil plant (can be for example frying oil, rotten waste oil, sewer oil or acidifying wet goods) of high acid value can prepare acid number to reach the biofuel of BD100 acid number standard.Preferably, being applicable to acid number is the biofuel that the oil plant of 100-200mg KOH/g is prepared acid number and reach BD100 acid number standard.
In the present invention, described monohydroxy-alcohol can be C
1-C
6monohydroxy-alcohol, be preferably at least one in methyl alcohol, ethanol, propyl alcohol, vinyl carbinol, butanols and amylalcohol.Further, under preferable case, described monohydroxy-alcohol is methyl alcohol and/or ethanol.Described propyl alcohol can be n-propyl alcohol and/or Virahol, and described butanols can be the isomer of propyl carbinol and/or propyl carbinol, and described amylalcohol can be the isomer of Pentyl alcohol and/or Pentyl alcohol.
According to method provided by the invention, the mixing of described oil plant, monohydroxy-alcohol and catalyzer contacts and can in reactor well known by persons skilled in the art, carry out.Under preferable case, the mixing of described oil plant, monohydroxy-alcohol and catalyzer contacts in fixed-bed reactor or knockout tower to be carried out, now further preferred described oil plant and monohydroxy-alcohol counter current contact.Described fixed-bed reactor and knockout tower are fixed-bed reactor arbitrarily well known to those skilled in the art and knockout tower.
When the mixing of described oil plant, monohydroxy-alcohol and catalyzer contacts while carrying out in fixed-bed reactor, described monohydroxy-alcohol enters continuously from fixed-bed reactor bottom, described oil plant enters continuously from the top of fixed-bed reactor, described monohydroxy-alcohol contacts in the reactor that contains catalyzer with oil plant, the low acid number oil plant of contact gained is discharged from bottom, and boiling point is discharged from top lower than the logistics of low acid number oil plant.Described low acid number oil plant refers to the oil plant reducing with respect to raw material (oil plant) acid number.
When the mixing of described oil plant, monohydroxy-alcohol and catalyzer contacts while carrying out in the knockout tower that is comprising tower reactor and king-post, described monohydroxy-alcohol enters king-post continuously from the tower reactor of knockout tower bottom, described oil plant enters king-post continuously from the top of knockout tower, described monohydroxy-alcohol contacts in the king-post that contains catalyzer with oil plant, the low acid number oil plant of contact gained is discharged from tower reactor, and boiling point is discharged from king-post top lower than the logistics of low acid number oil plant.Described low acid number oil plant refers to the oil plant reducing with respect to raw material (oil plant) acid number.
Taking knockout tower as example, a kind of process of preferred, concrete reduction oilseed acid value (can be also simultaneously the process of the low acid number biofuel of acquisition) is as described below: described knockout tower comprises tower reactor and king-post.In king-post, except the catalyst layer of acid-type ion-exchange resin is housed, arrange without other structures.Monohydroxy-alcohol enters the tower reactor of knockout tower bottom by certain flow, monohydroxy-alcohol gasifies at tower reactor temperature, enters king-post move up with gas phase.Oil plant enters king-post from knockout tower top and flows downward, in king-post, contact with monohydroxy-alcohol steam counter-flow, the water that unreacted monohydroxy-alcohol and reaction generate steams and directly enters rectifying tower from the upper outlet of knockout tower, monobasic alcohol and water is from rectifying tower separates, and monohydroxy-alcohol can refill tower reactor and participate in reaction.In tower reactor material, comprise low acid number oil plant (mainly containing fatty acid ester etc.) and glycerine, and the unreacted raw material oil plant of part.By this process, can obtain the oil plant of low acid number.In addition, discharging at the bottom of still is left standstill and separated after glycerine, obtain fatty acid ester through underpressure distillation, i.e. biofuel.Conventionally, primary first-order equation can obtain acid number and reach the biofuel of BD100 acid number standard.Wherein, the acid number that the acid number standard of the biofuel of BD100 refers to biofuel is below 0.8mgKOH/g.But obviously large or when obtaining the lower product of acid number, all or part of tower reactor material available pump is returned king-post top entrance again, carries out circulating reaction at raw material acid number.
According to method provided by the invention, in the time that the consumption of described monohydroxy-alcohol increases, can improve described oil plant and be converted into the transformation efficiency of lipid acid monobasic alcohol ester, thereby be conducive to reduce the acid number of oil plant.The cost that considers the process that reduces oilseed acid value, described monohydroxy-alcohol is preferably 0.01-1:1 with the feed weight ratio of oil plant, and more preferably 0.05-0.8:1, is particularly preferably 0.08-0.5:1.
According to method provided by the invention, temperature and pressure can reach good reaction effect within the specific limits, and temperature and pressure is excessive, can have a negative impact to the quality of the oil plant generating.In addition, in order to reduce the acid number of oil plant, obtain the biofuel of low acid number simultaneously, consider quality and the impact of pressure on equipment of oil plant, the temperature of described mixing contact is preferably 50-200 DEG C, and pressure is preferably 0.1-3MPa, and the liquid hourly space velocity of oil plant is 0.1-2h
-1.
The present inventor finds, by temperature and pressure being controlled at more suitably in scope, can further reduce the acid number of oil plant.For example the temperature of described mixing contact is 60-170 DEG C, more preferably 70-140 DEG C, and pressure is 0.1-0.7MPa, more preferably 0.1-0.3MPa, the liquid hourly space velocity of oil plant is 0.7-2h
-1.
In the time adopting method provided by the invention to prepare the biofuel of low acid number, in a kind of preferred implementation, described method provided by the invention also comprises in the material obtaining from mixing contact isolates lipid acid monobasic alcohol ester, the method of described separation can adopt conventional separation method to implement, for example, can adopt the method for underpressure distillation to realize.In further preferred embodiment, before described method provided by the invention also comprises isolate lipid acid monobasic alcohol ester in the material that obtains from mixing contact, isolate glycerine.The method of separation of glycerin can adopt conventional method to realize, for example, can realize by settlement separate method.Isolated glycerine can be recycled.
Below will describe the present invention by embodiment.In the present invention, described acid number refers under test conditions, in and the milligram number of the required potassium hydroxide of 1g oil plant free fatty acid, measure according to the indicator method in GB/T5530-1998 standard.
Following raw material, unless stated otherwise, is commercially available prod.
Embodiment 1
In the king-post of knockout tower, filling 100 grams of styrene sulfonic acid type ion exchange resin (acid amount for 2.0mmol/g), is 0.15MPa at pressure, and king-post temperature is that under the condition of 74 DEG C, the biofuel crude product that is 9.5mgKOH/g by acid number is with 1h
-1liquid hourly space velocity from king-post top inject, methyl alcohol is injected to tower reactor, heating is vaporized, enter king-post, move up, wherein, the weight ratio of methyl alcohol and biofuel oil plant is 0.1:1, and the upper outlet of the water that unreacted methyl alcohol and reaction generate from knockout tower steams and enter alcohol rectifying tower.After methyl alcohol separates with water, methyl alcohol can refill tower reactor and participate in reaction.At the bottom of still, obtain the biofuel that acid number is 0.39mgKOH/g.
Embodiment 2
In the king-post of knockout tower, filling 100 grams of styrene sulfonic acid type ion exchange resin (acid amount for 1.7mmol/g), is 0.11MPa at pressure, and king-post temperature is that under the condition of 74 DEG C, the biofuel crude product that is 9.5mgKOH/g by acid number is with 0.9h
-1liquid hourly space velocity from king-post top inject, methyl alcohol is injected to tower reactor, heating is vaporized, enter king-post, move up, wherein, the weight ratio of methyl alcohol and biofuel is 0.4:1, and the water that unreacted methyl alcohol and reaction generate steams and enters alcohol rectifying tower from the upper outlet of knockout tower.After methyl alcohol separates with water, methyl alcohol can refill tower reactor and participate in reaction.At the bottom of still, obtain the biofuel that acid number is 0.34mgKOH/g.
Embodiment 3
In the king-post of knockout tower, filling 100 grams of styrene sulfonic acid type ion exchange resin (acid amount for 1.5mmol/g), is 0.11MPa at pressure, and king-post temperature is that under the condition of 65 DEG C, the biofuel crude product that is 9.5mgKOH/g by acid number is with 2h
-1liquid hourly space velocity from king-post top inject, methyl alcohol is injected to tower reactor, heating is vaporized, enter king-post, move up, wherein, the weight ratio of methyl alcohol and biofuel is 0.25:1, and the water that unreacted methyl alcohol and reaction generate steams and enters alcohol rectifying tower from the upper outlet of knockout tower.After methyl alcohol separates with water, methyl alcohol can refill tower reactor and participate in reaction.At the bottom of still, obtain the biofuel that acid number is 0.36mgKOH/g.
Embodiment 4
In the king-post of knockout tower, filling 100 grams of styrene sulfonic acid type ion exchange resin (acid amount for 1.2mmol/g), is 0.11MPa at pressure, and king-post temperature is that under the condition of 79 DEG C, the biofuel crude product that is 9.5mgKOH/g by acid number is with 1h
-1liquid hourly space velocity from king-post top inject, methyl alcohol is injected to tower reactor, heating is vaporized, enter king-post, move up, wherein, the weight ratio of methyl alcohol and biofuel is 0.06:1, and the water that unreacted methyl alcohol and reaction generate steams and enters alcohol rectifying tower from the upper outlet of knockout tower.After methyl alcohol separates with water, methyl alcohol can refill tower reactor and participate in reaction.At the bottom of still, obtain the biofuel that acid number is 0.74mgKOH/g.
Embodiment 5
In the king-post of knockout tower, fill 100 grams of styrene sulfonic acid type ion exchange resin (acid amount is 2.0mmol/g), be 0.13MPa at pressure, king-post temperature is, under the condition of 130 DEG C, to be 117mgKOH/g by acid number, and the acidification oil that unsaponifiable matter content is 6.0g/100g injects from king-post top with the liquid hourly space velocity of 1h-1, methyl alcohol is injected to tower reactor, heating is vaporized, and enters king-post, moves up, wherein, the weight ratio of methyl alcohol and acidification oil is 0.4:1.The water that unreacted methyl alcohol and reaction generate steams and enters alcohol rectifying tower from the upper outlet of knockout tower.After methyl alcohol separates with water, methyl alcohol can refill tower reactor and participate in reaction.At the bottom of still, obtain the biofuel that acid number is 0.77mgKOH/g.Tower reactor material available pump is returned king-post top entrance again, carries out circulating reaction.
Embodiment 6
Adopt the method identical with embodiment 1 to react, the acid amount of different is styrene sulfonic acid type ion exchange resin is 2.3mmol/g, obtains the biofuel that acid number is 0.72mgKOH/g at the bottom of still.
Embodiment 7
Adopt the method identical with embodiment 4 to react, the acid amount of different is styrene sulfonic acid type ion exchange resin is 1.0mmol/g, obtains the biofuel that acid number is 1.2mgKOH/g at the bottom of still.
Embodiment 8
Adopt the 100g acidification oil of embodiment 5 in autoclave, to carry out the reaction of oilseed acid value reduction, the weight ratio of methyl alcohol and acidification oil is 0.4:1, the add-on of styrene sulfonic acid type ion exchange resin (acid amount is 2.0mmol/g) is 6% of oil plant quality, reaction pressure is 0.6MPa, 130 DEG C of temperature of reaction, reaction times is 2.5 hours, obtains the biofuel that acid number is 7mgKOH/g after reaction.
Can obviously find out by above-described embodiment, adopt the method for reduction oilseed acid value provided by the invention, can effectively reduce the acid number of oil plant.And, adopt method provided by the invention, in simplification of flowsheet, can utilize the grease of high acid value, acquisition acid number reaches the biofuel of BD100 acid number standard.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characterictic described in above-mentioned embodiment, in reconcilable situation, can combine by any suitable mode, for fear of unnecessary repetition, the present invention is to the explanation no longer separately of various possible array modes.
In addition, also can carry out arbitrary combination between various embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (10)
1. reduce a method for oilseed acid value, the method comprises contacts oil plant, monohydroxy-alcohol and catalyst mix, it is characterized in that, described catalyzer is acid-type ion-exchange resin.
2. method according to claim 1, wherein, described catalyzer is styrene sulfonic acid type ion exchange resin.
3. method according to claim 1 and 2, wherein, the acid amount of described catalyzer is 1-5mmol/g.
4. method according to claim 1, wherein, described mixing contact is carried out in fixed-bed reactor, described monohydroxy-alcohol enters continuously from fixed-bed reactor bottom, described oil plant enters continuously from the top of fixed-bed reactor, described monohydroxy-alcohol contacts with catalyzer in fixed-bed reactor with oil plant, and the low acid number oil plant of contact gained is discharged from bottom, and boiling point is discharged from top lower than the logistics of low acid number oil plant.
5. method according to claim 1, wherein, described mixing contact is carried out in knockout tower, this knockout tower comprises tower reactor and king-post, described monohydroxy-alcohol enters king-post continuously from the tower reactor of knockout tower bottom, and described oil plant enters king-post continuously from the top of knockout tower, and described monohydroxy-alcohol contacts in the king-post that contains catalyzer with oil plant, the low acid number oil plant of contact gained is discharged from tower reactor, and boiling point is discharged from king-post top lower than the logistics of low acid number oil plant.
6. according to the method described in claim 4 or 5, wherein, the condition of described mixing contact comprises: temperature is 50-200 DEG C, and pressure is 0.1-3MPa, and the liquid hourly space velocity of oil plant is 0.1-2h
-1.
7. method according to claim 6, wherein, the condition of described mixing contact comprises: temperature is 60-170 DEG C, and pressure is 0.1-0.7MPa, and the liquid hourly space velocity of oil plant is 0.7-2h
-1.
8. according to the method described in any one in claim 1-5, wherein, described monohydroxy-alcohol is 0.01-1:1 with the feed weight ratio of oil plant.
9. method according to claim 8, wherein, the acid number of described oil plant is 0.8-200mgKOH/g.
10. method according to claim 8, wherein, described monohydroxy-alcohol is C
1-C
6monohydroxy-alcohol.
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