CN104262105A - Glycerine refining method - Google Patents
Glycerine refining method Download PDFInfo
- Publication number
- CN104262105A CN104262105A CN201410548097.XA CN201410548097A CN104262105A CN 104262105 A CN104262105 A CN 104262105A CN 201410548097 A CN201410548097 A CN 201410548097A CN 104262105 A CN104262105 A CN 104262105A
- Authority
- CN
- China
- Prior art keywords
- glycerine
- acid
- phase splitter
- alcohols
- raw
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/88—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/94—Use of additives, e.g. for stabilisation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a glycerine refining method which comprises the following steps: adding alcohol and an inorganic acid into crude glycerine to form a fatty acid, first glycerine and an inorganic acid salt, and separating the first glycerine by using a first phase splitter; adding ferric trichloride into the separated first glycerine to form second glycerine, an iron soap and impurities, and separating the second glycerine by using a second phase splitter; distilling the second glycerine to form the refined glycerine. According to the scheme, the crude glycerine is preprocessed by using different auxiliaries before the step of distilling the glycerine, the substances like the fatty acid, salt, soap and ester in the glycerine are removed, so that the distilling and purifying steps lead the glycerine to a higher purity degree; in addition, the technological process in the scheme is simpler in comparison with an existing refining method, and is suitable for continuous commercialized batch production.
Description
Technical field
The present invention relates to a kind of glycerine method of refining.
Background technology
In grease production, as oil splitting, saponification, grease alcoholysis, except can obtaining natural acid, soap, fatty acid methyl ester, also can produce the sugar water of about about 10%.Glycerine sugar water is the main source of natural glycerin, natural glycerin output more than 90% from oil and fat product.And for example, in biofuel volume production, produce 1 ton of biofuel and about produce 100 kg of glycerin.In many industrial production, glycerine often exists with by-product form, in such as soap production, produces glycerine when fat saponification produces soap (alkali soap).Therefore, reasonably develop these by products, meet environmental protection theory.
Pure glycerine is a kind of colourless pleasantly sweet glutinous shape liquid, can generate various derivative, as Biodegradable plastics material acid, produce raw material 1,3 propylene glycol of diesel oil antifreezing agent glyceryl ether and PTT.Because glycerine is nontoxic, therefore food, medicine, with chemical field all have important application.
Because glycerine viscosity is high and mobility is not good, in order to obtain the glycerine of high purity (more than 99.5% purity), traditional heating mode is infeasible by glycerine heating evaporation purifying, and in various purification technique, when glycerol source is from fermenter, raw glycerine contains olefin polymer, ketone, double key carbon compound and other insatiable hunger and closes organic pollution materials, use ion exchange method, membrane separation process, with vacuum distillation method purification of glycerol, first above-mentioned pollution substance must be removed, just can carry out glycerine refining.And when glycerol source is from biofuel, because of in production of biodiesel process, for improving reaction conversion ratio, often add excessive methyl alcohol and alkali catalyst, these alkali and methyl alcohol are all dissolved in byproduct glycerine, these raw glycerines from biofuel contain the materials such as soap, salt and ester, if use vacuum distillation method, thin film separation or ion exchange methods glycerine, glycerol polymerization is easily there is and Ion-exchange particles lost efficacy during production, glycerine purity is unstable, purification efficiency is not high, and production, maintenance and running cost are high.In sum, more easy pre-treating process is still needed to carry out refined glycerol to improve glycerine purity at present.
Summary of the invention
The object of this invention is to provide a kind of technique simple and be applicable to a large amount of quantity-produced glycerine method of refining, refining can go out highly purified glycerine by the method.
For achieving the above object, the technical solution used in the present invention is as follows:
A kind of glycerine method of refining, is characterized in that: comprise the steps:
(1) in raw glycerine, add alcohols and mineral acid, form lipid acid, the first glycerine and inorganic acid salt, and isolate described first glycerine with the first phase splitter; The part by weight of described raw glycerine and described alcohols is between 1:0.5 ~ 1:2.0, and the interpolation of described raw glycerine and described mineral acid must control the pH value of glycerine solution between 3.0 ~ 5.0;
(2) in isolated described first glycerine, add iron trichloride, form the second glycerine, iron soap and impurity, and isolate described second glycerine with the second phase splitter; The part by weight of described first glycerine and described iron trichloride is between 1:0.001 ~ 1:0.1;
(3) described second glycerine is distilled, form refined glycerol.
Further, the interpolation of described raw glycerine and the described mineral acid pH value that must control glycerine solution is in being 4.0.
Further, described alcohols is methyl alcohol or ethanol.
Further, described mineral acid is phosphoric acid, hydrochloric acid or sulfuric acid.
Further, described first phase splitter and described second phase splitter are the liquid liquid/solid-liquor separation decanting vessel with baffle plate and tank level control, or plate separator.
Further, described distillation sequence comprises methanol stripper, moisture removal and glycerol distillation.
The beneficial effect of this programme is: this programme is before step (3) carries out glycerol distillation program, utilize different auxiliary agent that raw glycerine is carried out pre-treatment, be stripped of the materials such as lipid acid in glycerine, salt, soap and ester class, therefore carry out distillation purifying program and glycerine can be refined to high purity grades, and the technical process of this programme to compare existing method of refining more simple and easy, and be applicable to commercialization and produce in a large number continuously.
Embodiment
A kind of glycerine method of refining, comprises the steps:
First stage: add alcohols and mineral acid in raw glycerine, form lipid acid, the first glycerine and inorganic acid salt, and isolate the first glycerine with the first phase splitter.Specific as follows:
First, added by mineral acid in the raw glycerine in the first phase splitter, with the alkali in neutralized crude glycerine, adjust the pH value of raw glycerine simultaneously, make the soap in raw glycerine or fat hydrolysis be lipid acid, wherein mineral acid is sulfuric acid, hydrochloric acid or commercial phosphoric acid; Must control the pH value of glycerine solution when adding mineral acid between 3.0 ~ 5.0, take pH4.0 as the best; If when pH value is too high, significantly can reduce glycerin purification usefulness, if when pH value is too low, its purity promote and not obvious and acid ion easily and Fe
2+in conjunction with formation iron dirt material.
Then, appropriate alcohol analog assistant is added the first phase splitter, the reason of adding alcohol analog assistant is that glycerine has partial solubility to inorganic acid salt, and alcohols has comparatively low solubility to inorganic acid salt, therefore can improve the separating effect of inorganic acid salt in phase splitter.Raw glycerine and the part by weight of alcohols that adds are between 1:0.50 to 1:2.00; If the addition of alcohols is lower than above-mentioned scope, then can reduce glycerin purification rate, though and the addition increasing alcohol can increase glycerin purification rate, then can increase energy consumption during alcohols distillation in back segment operation when ratio is too high.
Due to lipid acid and glycerine mutual solubility low, the first phase splitter can be utilized to be separated into lipid acid upper strata, glycerine phase middle level and part insoluble inorganic acid salt and saponified lower floor.First phase splitter can be the liquid liquid/solid-liquor separation decanting vessel with baffle plate and tank level control, or plate separator.Lipid acid after separation separately stores, and the glycerine in middle level then continues to flow into next stage mutually.
The first stage is verified: get 100g raw glycerine with experimental data, select methyl alcohol respectively, ethanol is as the auxiliary agent of first stage, its addition is respectively 50ml, 100ml, 200ml, add phosphoric acid neutralization again and make pH=7.0, filter salt and saponified after, take out glycerin layer to reheat to 150 DEG C to remove alcohols, phosphoric acid, and moisture, finally pour separating funnel into, separation of fatty acids and glycerine, take out the glycerine after being separated and analyze glycerine purity, find along with methyl alcohol addition increases, glycerine purity also increases, respectively by 83.16% to 95.87%, and when changing methyl alcohol into ethanol, addition be 50 or 100 ml time, it is higher when glycerine purity all comparatively adds methyl alcohol, when ethanol addition is 100ml, glycerine purity is the highest by about 98.25%, but be 200 ml as increased ethanol addition again, then glycerine purity is down to 90.89% on the contrary.
Subordinate phase: iron trichloride is added in the first glycerine of first stage generation, form impurity, the second glycerine and iron soap, and isolate the second glycerine with the second phase splitter.Specific as follows:
Due to the lipid acid of the isolated glycerine of the first phase splitter through the first stage still containing residual soap, various different molecular weight, pigment and other organic impuritys, therefore iron trichloride need be added in the second phase splitter, residual soap in making glycerine mutually and lower molecular weight lipid acid generate insoluble iron soap, increase saponified removal efficiency; Because saponified (<0.1%) of trace easily causes distillation tower in back segment operation to bubble, cause distillation tower liquid level to rise instantaneously and cause system operation unstable.After adding iron trichloride, above-mentioned glycerine is met and is separated into three layers, is then separated upper strata black impurity, middle level glycerine phase and lower floor's part inorganic acid salt class and saponified with the second phase splitter.Wherein the part by weight of the iron trichloride of the first glycerine and interpolation is between 1:0.001 to 1:0.1; If the addition of iron trichloride is lower than above-mentioned scope, then can be unfavorable for hydrolysis and the precipitation of residual soap during glycerine mutually, if now in the second phase splitter, lipid acid removal effect is not good, then residual soap will make subsequent filter block by the second phase splitter, and very easily cause distillation tower in back segment operation to bubble; If the adding proportion of iron trichloride auxiliary agent is too high, then may there is scale formation in excessive iron ion in equipment, reduces equipment use usefulness.Wherein the second phase splitter can be the Liquid liquid Separation or solid-liquor separation decanting vessel with baffle plate and tank level control, or plate separator.
Subordinate phase is verified: after getting the glycerine of purifying in 100mL previous experiments and the iron trichloride mixing of 5g, surveying its saponification value is 77.88mg KOH/g with experimental data; Get the glycerine of purifying in 100mL previous experiments, not adding iron trichloride, directly to survey its saponification value be 35.33mg KOH/g.In addition, due to the easy moisture absorption of iron trichloride, two hydrate (FeCl can be generated
3-2H
2and six hydrate (FeCl O)
3-6H
2o), the aqueous solution in acid, help hydrolysis glycerine mutually in residual soap, increase saponified removal efficiency, and can with glycerine mutually in lower molecular weight lipid acid is combined, grease molecular-weight average (i.e. saponification equivalent) increase in making glycerine mutually.
Phase III: the second glycerine is carried out distillation sequence, the second glycerine is made to form refined glycerol.Specific as follows:
Conventional distillation sequence can be adopted to carry out purifying to glycerine.The object of distillation obtains refining glycerine, three road continuous still batterys are carried out through alcohols distillation tower, moisture distillation tower and glycerol distillation tower, sequentially remove or reclaim alcohols, moisture and other impurity, these impurity may comprise the fatty acid soaps dissolved in glycerine, polyglycerol, water and salt.Alcohols distillation tower can obtain purity more than 99.5% alcohols, and alcohols is recyclable; And the glycerine purity at the bottom of moisture distillation tower tower can be increased to more than 85%, through glycerol distillation tower, glycerol concentration can distillation and concentration further.In the design of glycerol distillation tower, because considering that the glycerine boiling point under normal pressure is 290 DEG C, but just start to decompose and polymerization reaction take place at 204 DEG C, therefore distillation must be carried out in below 15torr condition at vacuum level requirements and use thin-film evaporator as reboiler, to reduce glycerol polymerization and to go bad.The product that collection glycerol distillation tower distillates can obtain highly purified refined glycerol.
Above embodiment is merely illustrative and not limiting to the invention, therefore all equivalences done according to the method described in patent claim of the present invention change or modify, and are included in patent claim of the present invention.
Claims (6)
1. a glycerine method of refining, is characterized in that: comprise the steps:
(1) in raw glycerine, add alcohols and mineral acid, form lipid acid, the first glycerine and inorganic acid salt, and isolate described first glycerine with the first phase splitter; The part by weight of described raw glycerine and described alcohols is between 1:0.5 ~ 1:2.0, and the interpolation of described raw glycerine and described mineral acid must control the pH value of glycerine solution between 3.0 ~ 5.0;
(2) in isolated described first glycerine, add iron trichloride, form the second glycerine, iron soap and impurity, and isolate described second glycerine with the second phase splitter; The part by weight of described first glycerine and described iron trichloride is between 1:0.001 ~ 1:0.1;
(3) described second glycerine is distilled, form refined glycerol.
2. a kind of glycerine method of refining according to claim 1, is characterized in that: the pH value that the interpolation of described raw glycerine and described mineral acid must control glycerine solution is in being 4.0.
3. a kind of glycerine method of refining according to claim 1, is characterized in that: described alcohols is methyl alcohol or ethanol.
4. a kind of glycerine method of refining according to claim 1, is characterized in that: described mineral acid is phosphoric acid, hydrochloric acid or sulfuric acid.
5. a kind of glycerine method of refining according to claim 1, is characterized in that: described first phase splitter and described second phase splitter are the liquid liquid/solid-liquor separation decanting vessel with baffle plate and tank level control, or plate separator.
6. a kind of glycerine method of refining according to claim 1, is characterized in that: described distillation sequence comprises methanol stripper, moisture removal and glycerol distillation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410548097.XA CN104262105A (en) | 2014-10-16 | 2014-10-16 | Glycerine refining method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410548097.XA CN104262105A (en) | 2014-10-16 | 2014-10-16 | Glycerine refining method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104262105A true CN104262105A (en) | 2015-01-07 |
Family
ID=52153726
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410548097.XA Pending CN104262105A (en) | 2014-10-16 | 2014-10-16 | Glycerine refining method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104262105A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1083531A (en) * | 1992-08-29 | 1994-03-09 | 郭静峰 | Utilize useless vinasse to produce the method for glycerine |
| CN101633605A (en) * | 2008-07-23 | 2010-01-27 | 张伟民 | Method for preparing glycerin from byproduct in manufacture procedure of biodiesel |
| TW201024254A (en) * | 2008-12-17 | 2010-07-01 | Ind Tech Res Inst | Method for refining glycerin |
| KR101099367B1 (en) * | 2010-08-06 | 2011-12-29 | 제이씨케미칼(주) | Method for simultaneous refining of crude bio-diesel and crude glycerin in bio-diesel production process |
-
2014
- 2014-10-16 CN CN201410548097.XA patent/CN104262105A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1083531A (en) * | 1992-08-29 | 1994-03-09 | 郭静峰 | Utilize useless vinasse to produce the method for glycerine |
| CN101633605A (en) * | 2008-07-23 | 2010-01-27 | 张伟民 | Method for preparing glycerin from byproduct in manufacture procedure of biodiesel |
| TW201024254A (en) * | 2008-12-17 | 2010-07-01 | Ind Tech Res Inst | Method for refining glycerin |
| KR101099367B1 (en) * | 2010-08-06 | 2011-12-29 | 제이씨케미칼(주) | Method for simultaneous refining of crude bio-diesel and crude glycerin in bio-diesel production process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Hájek et al. | Treatment of glycerol phase formed by biodiesel production | |
| CN100376525C (en) | Method for refining glycerol being as byproduct of biology diesel oil | |
| CN109721471B (en) | Method for purifying glycerin from by-product of biodiesel production | |
| CN106146453A (en) | The preparation method of 1,3 propane sultone | |
| CN103189518A (en) | Method of preparing alkyl butyrate from fermented liquid using microorganisms | |
| CN103827072A (en) | Method for recovering acetic acid | |
| CN103772149A (en) | Method for refining crude glycerine being by-product of biodiesel | |
| KR101099367B1 (en) | Method for simultaneous refining of crude bio-diesel and crude glycerin in bio-diesel production process | |
| JP2005132836A (en) | Method for producing carboxylic acid-based compound | |
| CN104262102A (en) | Glycerine refining method | |
| KR20150011306A (en) | Method for preparing fatty acid alkyl ester using fat | |
| CN103664523A (en) | Method for refining biodiesel by-product crude glycerine | |
| TW201024254A (en) | Method for refining glycerin | |
| CN104262098A (en) | Comprehensive utilization method of biodiesel byproduct crude glycerol | |
| CN104262099A (en) | Glycerine refining method | |
| CN105264120B (en) | The preparation method of hydrocarbon | |
| CN104262100A (en) | Glycerine refining method | |
| CN102311307A (en) | Method for preparing octacosanol and triacontanol from rice bran wax | |
| CN104262105A (en) | Glycerine refining method | |
| CN104163832B (en) | A kind of glyphosate continuous production device and method | |
| CN104262106A (en) | Glycerine refining method | |
| CN104262104A (en) | Glycerine refining method | |
| CN104262101A (en) | Glycerine refining method | |
| CN104262103A (en) | Glycerine refining method | |
| CN103112968B (en) | Method for treating high-COD (Chemical Oxygen Demand) components in phenoxyalkanoic acid production wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20150107 |