CN114773155B - Process for separating glycerin from biodiesel byproduct - Google Patents
Process for separating glycerin from biodiesel byproduct Download PDFInfo
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- CN114773155B CN114773155B CN202210450416.8A CN202210450416A CN114773155B CN 114773155 B CN114773155 B CN 114773155B CN 202210450416 A CN202210450416 A CN 202210450416A CN 114773155 B CN114773155 B CN 114773155B
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- glycerol
- biodiesel
- treatment
- separating
- neutralization
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- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 title claims abstract description 668
- 239000003225 biodiesel Substances 0.000 title claims abstract description 76
- 239000006227 byproduct Substances 0.000 title claims abstract description 76
- 238000000034 method Methods 0.000 title claims abstract description 25
- 230000008569 process Effects 0.000 title claims abstract description 19
- 235000011187 glycerol Nutrition 0.000 title claims description 230
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 239000002699 waste material Substances 0.000 claims abstract description 29
- 238000009835 boiling Methods 0.000 claims abstract description 27
- 239000002253 acid Substances 0.000 claims abstract description 26
- 230000003197 catalytic effect Effects 0.000 claims abstract description 25
- 238000003756 stirring Methods 0.000 claims abstract description 19
- 235000014113 dietary fatty acids Nutrition 0.000 claims abstract description 18
- 239000000194 fatty acid Substances 0.000 claims abstract description 18
- 229930195729 fatty acid Natural products 0.000 claims abstract description 18
- 150000004665 fatty acids Chemical class 0.000 claims abstract description 18
- 238000002156 mixing Methods 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 235000019387 fatty acid methyl ester Nutrition 0.000 claims abstract description 12
- 239000000047 product Substances 0.000 claims abstract description 10
- 229930195730 Aflatoxin Natural products 0.000 claims abstract description 8
- XWIYFDMXXLINPU-UHFFFAOYSA-N Aflatoxin G Chemical compound O=C1OCCC2=C1C(=O)OC1=C2C(OC)=CC2=C1C1C=COC1O2 XWIYFDMXXLINPU-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000005409 aflatoxin Substances 0.000 claims abstract description 8
- 239000003513 alkali Substances 0.000 claims abstract description 8
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 8
- 239000000126 substance Substances 0.000 claims abstract description 7
- 238000004821 distillation Methods 0.000 claims abstract description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 36
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 27
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 27
- 230000020477 pH reduction Effects 0.000 claims description 22
- 229920001661 Chitosan Polymers 0.000 claims description 21
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 16
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 16
- 239000003085 diluting agent Substances 0.000 claims description 15
- 238000005189 flocculation Methods 0.000 claims description 14
- 230000016615 flocculation Effects 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 14
- 239000008139 complexing agent Substances 0.000 claims description 12
- ZNCPFRVNHGOPAG-UHFFFAOYSA-L sodium oxalate Chemical compound [Na+].[Na+].[O-]C(=O)C([O-])=O ZNCPFRVNHGOPAG-UHFFFAOYSA-L 0.000 claims description 10
- 239000002244 precipitate Substances 0.000 claims description 9
- 229940039790 sodium oxalate Drugs 0.000 claims description 9
- 210000005253 yeast cell Anatomy 0.000 claims description 9
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 8
- 239000011259 mixed solution Substances 0.000 claims description 8
- 238000000967 suction filtration Methods 0.000 claims description 5
- 229940037003 alum Drugs 0.000 claims description 4
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 4
- 229940103272 aluminum potassium sulfate Drugs 0.000 claims description 4
- 238000010790 dilution Methods 0.000 claims description 4
- 239000012895 dilution Substances 0.000 claims description 4
- 239000012065 filter cake Substances 0.000 claims description 4
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 4
- GRLPQNLYRHEGIJ-UHFFFAOYSA-J potassium aluminium sulfate Chemical compound [Al+3].[K+].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O GRLPQNLYRHEGIJ-UHFFFAOYSA-J 0.000 claims description 4
- 238000000746 purification Methods 0.000 abstract description 3
- 238000000576 coating method Methods 0.000 abstract 1
- 239000000314 lubricant Substances 0.000 abstract 1
- 239000012535 impurity Substances 0.000 description 23
- 229910017053 inorganic salt Inorganic materials 0.000 description 17
- 230000000694 effects Effects 0.000 description 16
- 238000002360 preparation method Methods 0.000 description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 239000000243 solution Substances 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 8
- ZYGHJZDHTFUPRJ-UHFFFAOYSA-N coumarin Chemical compound C1=CC=C2OC(=O)C=CC2=C1 ZYGHJZDHTFUPRJ-UHFFFAOYSA-N 0.000 description 8
- 238000001556 precipitation Methods 0.000 description 7
- 238000007127 saponification reaction Methods 0.000 description 6
- 239000012458 free base Substances 0.000 description 5
- 230000003472 neutralizing effect Effects 0.000 description 5
- 238000005809 transesterification reaction Methods 0.000 description 5
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 4
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 description 4
- 229960000956 coumarin Drugs 0.000 description 4
- 235000001671 coumarin Nutrition 0.000 description 4
- 238000005886 esterification reaction Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 229910021645 metal ion Inorganic materials 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000011056 performance test Methods 0.000 description 4
- SCVFZCLFOSHCOH-UHFFFAOYSA-M potassium acetate Chemical compound [K+].CC([O-])=O SCVFZCLFOSHCOH-UHFFFAOYSA-M 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 239000000344 soap Substances 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- -1 amino cations Chemical class 0.000 description 3
- 230000000536 complexating effect Effects 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000008394 flocculating agent Substances 0.000 description 3
- 125000000524 functional group Chemical group 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 238000005303 weighing Methods 0.000 description 3
- SXRSQZLOMIGNAQ-UHFFFAOYSA-N Glutaraldehyde Chemical compound O=CCCCC=O SXRSQZLOMIGNAQ-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 210000004027 cell Anatomy 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000012153 distilled water Substances 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 150000002596 lactones Chemical group 0.000 description 2
- 235000011056 potassium acetate Nutrition 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000007171 acid catalysis Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 238000005815 base catalysis Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 210000002421 cell wall Anatomy 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- CPCIOUMUZMHAAR-UHFFFAOYSA-N chromen-2-one;sodium Chemical compound [Na].C1=CC=C2OC(=O)C=CC2=C1 CPCIOUMUZMHAAR-UHFFFAOYSA-N 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229910003460 diamond Inorganic materials 0.000 description 1
- 239000010432 diamond Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000021588 free fatty acids Nutrition 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000001678 irradiating effect Effects 0.000 description 1
- 239000000693 micelle Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009210 therapy by ultrasound Methods 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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
-
- 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
- C07C29/92—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound by a consecutive conversion and reconstruction
-
- 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
-
- 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 application relates to the field of biodiesel byproduct purification methods, and particularly discloses a process for separating glycerol from biodiesel byproducts. A process for separating glycerol from biodiesel by-products comprising the steps of: and (3) acidizing: adding acid liquor into the biodiesel byproduct, stirring and mixing, adjusting the pH value to be 1-5 to obtain acidified glycerol, and separating the acidified glycerol to obtain crude glycerol; and (3) neutralization treatment: adding catalytic waste liquid into the crude glycerol, stirring and mixing, and separating to obtain neutralized glycerol; and (3) low-boiling removal: the neutralization glycerol is dehydrated and treated with low-boiling substances to obtain low-boiling glycerol; distillation treatment; the catalytic waste liquid comprises the following substances in parts by weight: 20-30 parts of water, 15-20 parts of free alkali, 1-2 parts of fatty acid, 2-3 parts of fatty acid methyl ester and 4-5 parts of aflatoxin decomposition product. The industrial glycerol disclosed by the application can be used for preparing lubricants, coatings and the like, and has the advantages of high purity and proper pH value.
Description
Technical Field
The application relates to the field of biodiesel byproduct purification methods, in particular to a process for separating glycerol from biodiesel byproducts.
Background
At present, when biological glycerol is produced, swill-cooked dirty oil, vegetable acidified oil and the like are generally used as raw materials, and biodiesel, biodiesel byproducts and catalytic waste liquid are obtained through transesterification. The cost reduction of biodiesel can also be achieved by increasing the utilization and/or added value of biodiesel by-products.
The biodiesel byproduct is often used as feed because of the large amount of impurities that are doped in the biodiesel byproduct and the difficulty in recycling the biodiesel byproduct. The biodiesel by-product is usually acidified to a crude glycerol pH of around 2 before use as feed. And (3) neutralizing the pH value of the acidified crude glycerol to obtain industrial glycerol with proper pH value, and then adding sodium hydroxide into the crude glycerol as a neutralizer material to perform a neutralization reaction.
In view of the above-mentioned related art, the inventors considered that in the case of neutralizing crude glycerin with sodium hydroxide alone as a neutralizing agent, the residual fatty acid in crude glycerin would undergo saponification reaction with sodium hydroxide, resulting in the disadvantage of poor purity of the obtained industrial glycerin.
Disclosure of Invention
In order to overcome the defect of poor purity of industrial glycerol, the application provides a process for separating glycerol from biodiesel byproducts, which adopts the following technical scheme:
a process for separating glycerol from biodiesel by-products comprising the steps of: and (3) acidizing: adding acid liquor into the biodiesel byproduct, stirring and mixing, adjusting the pH value to be 1-5 to obtain acidified glycerol, and separating the acidified glycerol to obtain crude glycerol; and (3) neutralization treatment: adding catalytic waste liquid into the crude glycerol, stirring and mixing, and separating to obtain neutralized glycerol; and (3) low-boiling removal: the neutralization glycerol is dehydrated and treated with low-boiling substances to obtain low-boiling glycerol; distillation treatment: distilling the low-boiling glycerin, and separating to obtain industrial glycerin; the catalytic waste liquid comprises the following substances in parts by weight: 20-30 parts of water, 15-20 parts of free alkali, 1-2 parts of fatty acid, 2-3 parts of fatty acid methyl ester and 4-5 parts of aflatoxin decomposition product.
By adopting the technical scheme, the biodiesel byproduct is firstly subjected to acidification treatment, and in the process, fatty acid soap in the biodiesel byproduct is dissociated to obtain fatty acid and inorganic salt, so that the viscosity of the biodiesel byproduct is reduced, the clarity of the biodiesel byproduct is improved, and the quality of the biodiesel byproduct is improved. After the fatty acid and the fatty acid methyl ester are separated from the biodiesel byproduct by layering, the fatty acid and part of the fatty acid methyl ester can be removed, so that part of impurities in the crude glycerol are removed.
Secondly, because the acidized crude glycerin has larger acidity and is unfavorable for direct use, the application further adopts catalytic waste liquid to neutralize the crude glycerin, and free alkali in the catalytic waste liquid can neutralize H in the crude glycerin + And the neutralization is carried out, so that the pH of the crude glycerol is improved, and the subsequent application of the crude glycerol is facilitated.
Meanwhile, the catalytic waste liquid is added into the crude glycerin, and the aflatoxin decomposition product in the catalytic waste liquid can be combined with H + The reaction, i.e. coumarin sodium saltAnd H is + And (3) reacting to obtain coumarin through lactone ring recovery. When free base and H + After neutralization, the active functional groups of the coumarin compete to neutralize the free base in the glycerol, and the aflatoxin decomposition product is formed again, so that the coumarin precipitates again to neutralize the glycerol. The glycerol in the neutralized glycerol is not easy to carry out transesterification reaction with residual fatty acid methyl ester in the neutralized glycerol through competitive circulation of the aflatoxin decomposition product on the free base, so that the transesterification product and the free base are inhibited from producing saponification products, and the clarity of the neutralized glycerol is further improved.
Finally, the water and inorganic salt in the neutralized glycerol are removed through low boiling point removal treatment, and the industrial glycerol with proper pH and high purity is obtained after rectification treatment.
Preferably, the acidification treatment further comprises a dilution pretreatment: the diluent adopted in the dilution pretreatment comprises any one or more of methanol, ethanol and water, and the mass ratio of the diluent to the crude glycerol is 0.25-1:1.
By adopting the technical scheme, the diluent is added into the biodiesel byproduct to dilute and pretreat the biodiesel byproduct, and as the solubility of inorganic salt and the like in the diluent is higher than that of the inorganic salt in the glycerol, part of the inorganic salt in the glycerol can be transferred into the diluent, and the inorganic salt is removed along with the diluent when the low-boiling removal is carried out subsequently, so that the impurities in the industrial glycerol are reduced. Meanwhile, the proportion between the diluent and the biodiesel byproducts is optimized, the viscosity of the biodiesel byproducts can be effectively reduced, the contact mixing effect between the acid liquid and the biodiesel byproducts is improved, namely the layering effect between the glycerol and the grease after the acidification treatment is improved, and the separation effect and the purity of the industrial glycerol are improved.
Preferably, the neutralization treatment further comprises flocculation treatment of the crude glycerin, and the flocculant adopted in the flocculation treatment comprises any one of alum, ferric trichloride, aluminum sulfate and aluminum potassium sulfate.
Through adopting above-mentioned technical scheme, this application has further optimized the component of flocculating agent, and the flocculating agent material that adopts in this application can be through modes such as electric neutralization, absorption bridging, effectively adsorb the impurity in the crude glycerine, further improves the purity of industry glycerine.
Preferably, the flocculant further comprises a complexing agent, wherein the complexing agent comprises sodium oxalate and chitosan in a mass ratio of 3-4:1-2, and the chitosan is yeast cell-loaded chitosan.
Through adopting above-mentioned technical scheme, this application technical scheme adopts sodium oxalate and the chitosan that supports the yeast cell to mutually support, and sodium oxalate can complex the metal ion in the crude glycerine, forms the complex and adsorbs the impurity in the crude glycerine, further gets rid of the impurity in the crude glycerine. Meanwhile, the chitosan adopted by the application has active amino cations, and can be matched with active functional groups on the cell walls of yeasts, so that impurities in the complex crude glycerol are adsorbed and complexed, and the purity of the industrial glycerol is improved.
Preferably, the flocculation treatment comprises the steps of: adding flocculant into the crude glycerol, stirring and mixing to obtain mixed solution, adjusting the temperature of the mixed solution to 70-90 ℃, stirring for 20-40min, carrying out suction filtration, and discarding filter cakes to obtain the acidified glycerol subjected to flocculation treatment.
Through adopting above-mentioned technical scheme, further optimized the step of flocculation treatment among the technical scheme of this application to reduce the viscosity decline of mixed solution, increased collision probability between the micelle, improved flocculation, absorption, the sedimentation effect of flocculation thing to impurity. Meanwhile, the application adopts proper stirring time, so that the collision probability of colloidal particles in the mixed solution can be further improved, the flocculation and precipitation effects of colloid in glycerol are improved, and the purity of industrial glycerol is improved.
Preferably, the temperature of the acidification treatment is 75-125 ℃, and the acid liquid adopted in the acidification treatment comprises one or two of phosphoric acid, sulfuric acid and acetic acid.
By adopting the technical scheme, the temperature of acidizing treatment is optimized, the proper acidizing temperature is realized, and H is effectively improved + The activity degree in the biodiesel byproduct is accelerated, so that the neutralization of OH in the biodiesel byproduct caused by base catalysis is accelerated - 。
At the same time, the fatty acid soap is dissociated into fatty acid and glycerin under acid catalysis, so that glycerin-coated fatty acid methyl ester and fatty acid are separated out in a layering way, and then the glycerin is separated out from the fatty acid methyl ester and the fatty acid through separation so as to remove impurities in industrial glycerin. And during neutralization, strong saponification reaction is not easy to occur, so that the industrial glycerin maintains proper viscosity, and the glycerin content in the industrial glycerin is improved.
According to the method, the acid liquor is further optimized, when phosphoric acid and sulfuric acid are used as acid liquor to neutralize the biodiesel byproducts, the acid liquor reacts with an alkali catalyst to generate precipitation, so that inorganic salts in the biodiesel byproducts are easily separated in a precipitation mode, and the content of glycerol in industrial glycerol is improved.
When acetic acid is used as acid liquor to neutralize biodiesel byproducts, the acetic acid reacts with potassium hydroxide to generate potassium acetate, and then the potassium acetate is precipitated after flash evaporation, so that inorganic salts in the biodiesel byproducts are effectively separated.
The sulfuric acid, the phosphoric acid and the acetic acid are mutually matched to be used as the acid liquor, and when the acid liquor and inorganic salt in the biodiesel byproduct generate precipitation and are separated out, the pH adjusting speed of the biodiesel byproduct is stable, so that the possibility of esterification reaction of fatty acid and methanol in the biodiesel byproduct is reduced, and the separation effect of glycerol in industrial glycerol is further improved.
Preferably, the acidification step further comprises the step of carrying out irradiation treatment on the acidified glycerol, wherein the frequency of the irradiation treatment is 40-50Hz, the power is 80-120W, and the irradiation time is 2-4min.
By adopting the technical scheme, the method further optimizes the acidification step, adopts microwave irradiation to pretreat the acidified glycerol, can reduce the activation energy of the acidified glycerol and promote H + The activity in the acidified glycerol, thereby accelerating the neutralization reaction rate and dissociating the free fatty acid to form a layer. The viscosity of the acidified glycerol is effectively reduced, the layering definition of the glycerol and the fatty acid is improved, namely, the content of organic impurities in the acidified glycerol is reduced, and the purity of the industrial glycerol is improved.
Preferably, the mass ratio of the catalytic waste liquid to the crude glycerol is 2.5-5:1.
Through adopting above-mentioned technical scheme, this application technical scheme has optimized the ratio between catalytic waste liquid and the crude glycerine, when effectively neutralizing the acidizing fluid in the crude glycerine, can reduce the corrosion of low boiling glycerine to the rectifying tank of rectifying in-process.
At the same time, catalyze OH in waste liquid - The free small amount of fatty acid in the crude glycerol can be neutralized, saponification reaction further occurs, impurities in the crude glycerol are adsorbed to form precipitate, the impurity content in the crude glycerol is effectively reduced through separation of the precipitate, and the purity of the industrial glycerol is further improved.
Preferably, in the low-boiling removal step, the temperature of the low-boiling removal treatment is 150-220 ℃.
Through adopting above-mentioned technical scheme, this application technical scheme is through optimizing the temperature of taking off low boiling point processing, effectively gets rid of water, methyl alcohol and partial inorganic salt in the neutralization glycerol, simultaneously, and the glycerol can be stabilized and is present in the flash tank and be difficult for evaporating along with low boiling point thing to the purity of industry glycerol has been improved.
Preferably, the neutralization glycerol is subjected to a separation treatment prior to the low-boiling removal step, the separation treatment comprising the steps of: and adding ethanol into the neutralization glycerol until no precipitate is separated out from the neutralization glycerol, stopping adding ethanol, and carrying out suction filtration to obtain the neutralization glycerol subjected to separation treatment.
By adopting the technical scheme, the technical scheme further adopts ethanol to separate and treat the neutralization glycerol. Because the polarity of the ethanol is smaller than that of the methanol, the solubility of the inorganic acid salt in the ethanol is lower, and the subsequent precipitation and separation of the inorganic salt in the ethanol are facilitated, so that the phenomenon that the operation of a rectifying tank is influenced due to the excessively high inorganic salt precipitation amount in the subsequent rectifying process is effectively improved, and the glycerol purification rate is improved.
In summary, the present application has the following beneficial effects:
1. because the application adopts the catalytic waste liquid to neutralize the crude glycerin, on one hand, the catalytic waste liquidRecycling is performed, the utilization rate of waste is improved, and the possibility of environmental pollution caused by improper waste treatment is reduced; on the other hand, free base in the catalytic waste liquid neutralizes H in the crude glycerol + The recovery and rupture cycle of the lactone ring in the coumarin compete for free alkali, so that the esterification reaction is inhibited, the saponification reaction between the transesterification reaction product and the free alkali is inhibited, the clarity of crude glycerol is improved, the purity of industrial glycerol is improved, and meanwhile, the industrial glycerol obtains proper pH value, so that the industrial glycerol is directly used.
2. In the application, the temperature of the acidification treatment and the composition of the acid liquor are preferably adjusted, and the proper acidification temperature improves H + The activity in the acidified glycerol improves the acidifying effect of the acid liquid on biodiesel byproducts and reduces the occurrence of esterification reaction; meanwhile, after the acid liquor contacts with the biodiesel byproduct, the saponified material can be hydrolyzed, and the wrapping of the glycerol on the fatty acid methyl ester can be removed; and the method can also be combined with inorganic salt in the biodiesel byproduct to generate precipitate, so that impurities in the biodiesel byproduct are removed, and the prepared industrial glycerin has higher purity.
3. In the application, the complexing agent is preferably added into the flocculant, and as the sodium oxalate and the chitosan loaded with the yeast cells are mutually matched, the complexing effect of the yeast cells and the sodium oxalate on metal ions can be effectively promoted, and the content of the metal ions in the industrial glycerol is effectively reduced, so that the industrial glycerol has higher purity.
Detailed Description
The present application is described in further detail below with reference to examples.
In the embodiment of the present application, the selected instruments and devices are shown below, but not limited to:
instrument: the Suzhou gold diamond weighing apparatus system developed a PB-30L pH agent.
Medicine: the microwave irradiation equipment comprises deacylated chitosan with 75% of active substance content of Jiangsu Source biological technology Co., ltd, saccharomyces cerevisiae with 99% of Jiangsu Aofu biological technology Co., ltd, glutaraldehyde with 50% of Jinan Yuan chemical engineering Co., ltd, and SCWB-1S of Nanjing Shunchang environmental protection engineering Co., ltd.
Preparation example
Acid liquor preparation example
Preparation examples 1 to 6
Phosphoric acid (mass fraction 50%), sulfuric acid (mass fraction 50%), acetic acid (mass fraction 50%) were weighed respectively, and specific masses are shown in table 1, to obtain acid solutions 1 to 6.
TABLE 1 acid composition of preparation examples 1-6
Preparation example of Chitosan
Preparation example 7
4kg of chitosan was weighed as chitosan 1.
Preparation example 8
Weighing 10kg of Saccharomyces cerevisiae, carrying out aerobic propagation at 37 ℃, shaking by a shaking table for 24 hours, centrifuging, retaining solids, and washing with distilled water for 2 times to obtain wet cells. Suspending the obtained wet cells in distilled water, performing ultrasonic treatment at 19kHz for 30min, centrifuging, and discarding the clear liquid to obtain dead yeast cells. 3kg of chitosan and 50kg of acetic acid with the volume fraction of 3% are stirred and mixed to obtain chitosan solution. 4.5kg of a 50% sodium hydroxide solution and 0.1kg of a 25% glutaraldehyde solution were added to the chitosan solution, followed by stirring and mixing to obtain a crosslinked solution. Adding dead yeast cells into the crosslinked solution, stirring and mixing to obtain yeast immobilized chitosan serving as chitosan 2.
Complexing agent preparation example
Preparation examples 9 to 12
And respectively weighing sodium oxalate and chitosan, wherein the specific mass is shown in table 2, and stirring and mixing to obtain complexing agents 1-3.
TABLE 2 preparation examples 9-12 complexing agent composition
Flocculant preparation example
Preparation example 13
Alum, ferric trichloride, aluminum sulfate, aluminum potassium sulfate and complexing agent 1 are respectively weighed, and concrete mass is shown in Table 3, so as to prepare flocculant 1-5.
TABLE 3 preparation examples 13-17 flocculant composition
Preparation examples 18 to 20
The difference from preparation example 17 is that: the flocculant 6-8 was prepared using complexing agent 2-4 instead of complexing agent 1 in preparation example 17.
Examples
Examples 1 to 3
The application provides a process for separating glycerol in biodiesel byproducts, which comprises the steps of adding byproducts and acid liquor 1 into an acidification tank, regulating the temperature of liquid in the acidification tank to 75 ℃, continuously stirring and mixing, and regulating the pH=1 of the liquid in the acidification tank to obtain acidified glycerol. Pumping the acidified glycerine to a layering tank, carrying out multistage gravity sedimentation separation, and retaining a lower layer liquid to obtain crude glycerine. Pumping the crude glycerol into a neutralization tank, wherein the pumping amount of the crude glycerol is 10kg, adding 25kg of catalytic waste liquid into the neutralization tank, and continuously stirring and mixing to obtain the neutralization glycerol. And conveying the neutralized glycerol to a layering tank, separating again through multistage gravity sedimentation, conveying the lower layer liquid to a flash tank, carrying out vacuum flash evaporation treatment at 150 ℃, and removing low-boiling substances and water, wherein the liquid in the flash tank is the low-boiling glycerol. And (3) in the process of conveying the low-boiling-point removed glycerol to a rectifying tower, preheating the low-boiling-point removed glycerol by a heater, preheating the low-boiling-point removed glycerol to 140 ℃, heating the low-boiling-point removed glycerol to 205 ℃ in the rectifying tower, and condensing and refluxing to obtain the industrial glycerol 1.
The catalytic waste liquid comprises water, free alkali, fatty acid methyl ester and aflatoxin decomposition product, and the specific component content is shown in table 4
TABLE 4 catalytic waste liquid specific component content
Examples 2 to 4
The difference from example 1 is that: adjusting the ph=2, 4.5, 5 of the liquid in the acidification tank, industrial glycerol 2-4 was prepared.
Example 5
The difference from example 1 is that: the crude glycerol was pumped in an amount of 10kg, and 35kg of the catalytic waste liquid was added to the neutralization tank to obtain industrial glycerol 5.
Example 6
The difference from example 1 is that: the crude glycerol was pumped in an amount of 10kg, and 50kg of the catalytic waste liquid was added to the neutralization tank to obtain industrial glycerol 6.
Examples 7 to 8
The difference from example 1 is that: the temperature of the low boiling point removal treatment is controlled to be 180 ℃ and 220 ℃ respectively, and the industrial glycerin 7-8 is obtained.
Examples 9 to 10
The difference from example 1 is that: the temperature of the liquid in the acidification tank is respectively regulated to be 100 ℃ and 125 ℃ to prepare the industrial glycerol 9-10.
Example 11
The difference from example 1 is that: before the biodiesel by-product is added into the acidification tank, the biodiesel by-product is diluted, and 10kg of biodiesel by-product and 2.5kg of diluent are stirred and mixed to obtain diluted biodiesel by-product, so as to prepare the industrial glycerin 11.
It should be noted that the diluent includes, but is not limited to, one or more of methanol, ethanol and water, and methanol is used in this embodiment.
Example 12
The difference from example 11 is that: 10kg of biodiesel byproduct and 6kg of diluent are stirred and mixed to obtain diluted biodiesel byproduct, and industrial glycerin 12 is prepared.
Example 13
The difference from example 11 is that: 10kg of biodiesel byproduct and 10kg of diluent are stirred and mixed to obtain diluted biodiesel byproduct, and industrial glycerin 13 is prepared.
Examples 14 to 18
The difference from example 1 is that: acid liquor 2-6 was used in place of acid liquor 1 in example 1 to prepare technical glycerol 14-18.
Example 19
The difference from example 1 is that: and (3) carrying out microwave irradiation pretreatment on the acidified glycerol, adjusting the frequency of microwave irradiation equipment to 40Hz, the power to 80W, and irradiating for 2min to obtain pretreated acidified glycerol, so as to prepare the industrial glycerol 19.
Example 20
The difference from example 1 is that: and (3) carrying out microwave irradiation pretreatment on the acidified glycerol, adjusting the frequency of microwave irradiation equipment to be 45Hz, and carrying out irradiation for 3min at the power of 100W to obtain pretreated acidified glycerol, so as to prepare the industrial glycerol 20.
Example 21
The difference from example 1 is that: and (3) carrying out microwave irradiation pretreatment on the acidified glycerol, adjusting the frequency of microwave irradiation equipment to be 50Hz, and carrying out irradiation for 4min at the power of 120W to obtain pretreated acidified glycerol, thereby preparing the industrial glycerol 21.
Example 22
The difference from example 19 is that: before neutralization treatment, flocculating treatment is carried out on the pretreated acidified glycerine, flocculating agent 1 is added into the crude glycerine, stirring and mixing are carried out for 20min, mixed liquor is obtained, the temperature of the mixed liquor is regulated to 70 ℃, standing is carried out, suction filtration is carried out, filter cakes are abandoned, and the flocculated crude glycerine is obtained, and the industrial glycerine 22 is prepared.
Examples 23 to 29
The difference from example 22 is that: flocculant 2-8 was used in place of flocculant 1 in example 22 to produce technical glycerol 23-29.
Example 30
The difference from example 22 is that: the temperature of the mixed solution was adjusted to 80℃and the stirring time was 30 minutes, thereby preparing industrial glycerin 30.
Example 31
The difference from example 22 is that: the temperature of the mixed solution was adjusted to 90℃and the stirring time was 40min, thereby preparing industrial glycerin 31.
Example 32
The difference from example 1 is that: before the lower liquid is conveyed to a flash tank, ethanol is added into the neutralization glycerol until no precipitate is separated out from the neutralization glycerol, the ethanol is stopped being added, the filtration is carried out, and a filter cake is abandoned, so that the neutralization glycerol after separation treatment is obtained, and the industrial glycerol 32 is prepared.
Comparative example
Comparative example 1
The difference from example 1 is that: 25kg of sodium hydroxide by mass fraction was added to the neutralization tank for neutralization to prepare technical glycerin 33.
Comparative example 2
The difference from example 1 is that: the glycerol byproduct was acidified with 10% by mass hydrochloric acid to produce technical glycerol 34.
Comparative example 3
The difference from example 1 is that: the industrial glycerin 35 is prepared by neutralizing the catalytic waste liquid which does not contain the decomposition product of aflatoxin.
Performance test
(1) pH value test: and detecting the pH of the industrial glycerol 1-35 by adopting a pH detector.
(2) And (3) detecting the purity of the glycerol: the glycerol content was measured according to GB/T13216-2008 glycerol test method.
Table 5 examples 1-18 performance test table
TABLE 6 Performance test tables for examples 19-32, comparative examples 1-3
The comparison of performance tests in combination with tables 5 and 6 can be found:
(1) Comparison of examples 1-4, examples 9-10 and comparative example 2 shows that: examples 1 to 4 and 9 to 10The glycerol content and pH in the obtained industrial glycerol are improved, which means that the pH and the temperature of the acidification treatment are optimized, and the pH is proper, so that H in the acid liquor + Can sufficiently neutralize OH in biodiesel byproduct - The occurrence of saponification reaction is reduced, and the possibility of condensation of biodiesel byproducts in acidic conditions is reduced; the dissociated fatty acid soap is stable, and the fatty acid methyl ester and fatty acid which are wrapped in the glycerol are separated out in a layering way, so that impurities in the biodiesel byproduct are reduced. As can be seen from tables 5 and 6, the preferred glycerol content and pH in the technical glycerol prepared in examples 2, 3 and 9 indicate that the preferred pH in examples 2 and 3 and the preferred acidification temperature in example 9.
(2) The comparison of examples 5-6, example 1 and comparative example 1, comparative example 3, can be found: the glycerol content and the pH value of the industrial glycerol prepared in the examples 5-6 are improved, which shows that the catalytic waste liquid is adopted to neutralize the crude glycerol, so that the utilization rate of waste is improved, and the environmental pollution is reduced; during neutralization, the transesterification reaction is inhibited, the generation of saponified matters is reduced, the clarity of the crude glycerol is improved, a small amount of free saponified matters in the crude glycerol can adsorb impurities and then precipitate, the content of the impurities in the crude glycerol is further reduced, and the purity of the industrial glycerol is improved. As can be seen from tables 5 and 6, the amount of glycerol and pH in the industrial glycerol obtained in example 5 were good, indicating that the amount of the catalytic waste liquid added was suitable.
(3) As can be seen from a comparison of examples 7-8, examples 11-13 and example 1: the glycerol content and pH of the industrial glycerol prepared in examples 7-8 and examples 11-13 are improved, which shows that the temperature of the low boiling removal treatment and the ratio of the diluent to the biodiesel byproduct are optimized, and the proper low boiling removal treatment temperature ensures that the glycerol is stable, methanol, water and part of inorganic salt are separated from the glycerol along with evaporation, so that the impurities in the neutralized glycerol are removed. Meanwhile, the proper addition amount of the diluent effectively reduces the viscosity of the biodiesel byproduct, and improves H during acidification + The movement effect in the biodiesel byproduct, thereby improving the neutralization of the biodiesel byproduct by the acid liquor and waterThe soap effect is relieved, the impurity content in the biodiesel by-product is reduced, and the purity of the industrial glycerin is improved. As can be seen from tables 5 and 6, the preferred glycerol content and pH in the technical glycerol prepared in example 7 and example 12 indicate that the vacuum flash temperature is suitable in example 7 and the ratio of methanol to biodiesel by-product in example 12 is suitable.
(4) The comparison of examples 14-15, examples 16-18 and example 1 can be found: the enhanced glycerol content and pH in the industrial glycerol produced in examples 14-18, which demonstrates that one or both of phosphoric acid, sulfuric acid, and acetic acid are used as the acid solution in the present application, and that the phosphoric acid and sulfuric acid are used with K in the biodiesel byproduct + And precipitate is generated, which can be separated and removed, and the content of inorganic salt in the biodiesel byproduct is reduced. By matching any two of sulfuric acid, phosphoric acid and acetic acid, OH in biodiesel byproducts is rapidly neutralized - And the pH is uniform in descending speed, the esterification reaction of biodiesel byproducts is inhibited, and inorganic salt is separated out through precipitation, so that the impurity content in industrial glycerol is reduced. As can be seen from Table 5, the technical glycerin obtained in example 16 is preferred in terms of glycerin content and pH, indicating that the ratio of the components in the acid solution is suitable.
(5) The comparison of examples 19-20 and example 1 can be found: the increase in both glycerol content and pH in the technical glycerol obtained in examples 19-20 demonstrates that the present application irradiates the acidified glycerol and optimizes the parameters of the irradiation to increase H + The activity degree in the acidified glycerol reduces the activation energy of the acidified glycerol, and enhances the neutralization effect of the acid liquor on biodiesel byproducts, so that fatty acid and fatty acid methyl ester are easier to separate out in a layering way, and the removal effect of impurities in the industrial glycerol is improved. As can be seen from Table 5, the technical glycerin obtained in example 19 has a preferable glycerin content and pH, and the irradiation treatment parameters in example 15 are preferable.
(6) As can be seen from the comparison of examples 22-25, examples 26-29, examples 30-31 and example 1: the improved glycerol content and pH in the industrial glycerol prepared in examples 22-31 suggests that the flocculant components are optimized in the application, and as alum, ferric trichloride, aluminum sulfate and aluminum potassium sulfate can form charged colloidal particles in the crude glycerol, the charged colloidal particles are adsorbed and co-flocculated with impurities by means of electrostatic adsorption, electric neutralization, bridging and the like. And sodium oxalate and chitosan loaded with yeast cells are used as complexing agents, the sodium oxalate complexes metal ions in the crude glycerol, and active amino cations on the chitosan not only activate active functional groups on the yeast cell walls, but also promote the activity of the sodium oxalate, improve the complexing effect on impurities in the crude glycerol, and improve the purity of the industrial glycerol by the mutual coordination of flocculation and complexing. As can be seen from tables 5 and 6, the preferred glycerol content and pH in the technical glycerol prepared in examples 29 and 30 indicate that the proportion of the components in the flocculant in example 29 is suitable and the parameters of the flocculation treatment in example 30 are suitable.
(7) As can be seen from the comparison of example 32 and example 1: the improvement of the glycerol content and the pH value in the industrial glycerol prepared in example 32 shows that the ethanol is added in the neutralization glycerol, and the ethanol has low polarity, so that part of inorganic salt dissolved in the neutralization glycerol can be separated out after the ethanol is added because the ethanol has low solubility in the ethanol, and the influence of inorganic salt separation on the distillation efficiency during distillation is reduced by separating and removing inorganic salt impurities in the neutralization glycerol.
The present embodiment is merely illustrative of the present application and is not intended to be limiting, and those skilled in the art, after having read the present specification, may make modifications to the present embodiment without creative contribution as required, but is protected by patent laws within the scope of the claims of the present application.
Claims (8)
1. A process for separating glycerol from biodiesel by-products, comprising the steps of:
and (3) acidizing: adding acid liquor into the biodiesel byproduct, stirring and mixing, adjusting the pH value to be 1-5 to obtain acidified glycerol, and separating the acidified glycerol to obtain crude glycerol;
and (3) neutralization treatment: adding catalytic waste liquid into the crude glycerol, stirring and mixing, and separating to obtain neutralized glycerol;
and (3) low-boiling removal: the neutralization glycerol is dehydrated and treated with low-boiling substances to obtain low-boiling glycerol;
distillation treatment: distilling the low-boiling glycerin, and separating to obtain industrial glycerin;
the catalytic waste liquid comprises the following substances in parts by weight: 20-30 parts of water, 15-20 parts of free alkali, 1-2 parts of fatty acid, 2-3 parts of fatty acid methyl ester and 4-5 parts of aflatoxin decomposition product;
the mass ratio of the catalytic waste liquid to the crude glycerin is 2.5-5:1;
the acidification step further comprises the step of carrying out irradiation treatment on the acidified glycerol, wherein the frequency of the irradiation treatment is 40-50Hz, the power is 80-120W, and the irradiation time is 2-4min.
2. A process for separating glycerol from biodiesel by-products in accordance with claim 1, wherein said acidification treatment further comprises a dilution pretreatment: the diluent adopted in the dilution pretreatment comprises any one or more of methanol, ethanol and water, and the mass ratio of the diluent to the biodiesel byproduct is 0.25-1:1.
3. A process for separating glycerol from biodiesel by-products in accordance with claim 1, wherein: the neutralization treatment also comprises flocculation treatment of the crude glycerin, wherein a flocculant adopted in the flocculation treatment comprises any one of alum, ferric trichloride, aluminum sulfate and aluminum potassium sulfate.
4. A process for separating glycerol from biodiesel by-products in accordance with claim 3, wherein: the flocculant also comprises a complexing agent, wherein the complexing agent comprises sodium oxalate and chitosan with a mass ratio of 3-4:1-2, and the chitosan is chitosan loaded with yeast cells.
5. A process for separating glycerol from biodiesel by-products in accordance with claim 3, wherein said flocculation treatment comprises the steps of: adding flocculant into the crude glycerol, stirring and mixing to obtain mixed solution, adjusting the temperature of the mixed solution to 70-90 ℃, stirring for 20-40min, carrying out suction filtration, and discarding filter cakes to obtain the acidified glycerol subjected to flocculation treatment.
6. A process for separating glycerol from biodiesel by-products in accordance with claim 1, wherein: the temperature of the acidification treatment is 75-125 ℃, and the acid liquid adopted in the acidification treatment comprises one or two of phosphoric acid, sulfuric acid and acetic acid.
7. The process for separating glycerol from a biodiesel byproduct according to claim 1, wherein in said low-boiling removal step, the temperature of the low-boiling removal treatment is 150-220 ℃.
8. A process for separating glycerol from biodiesel by-products according to claim 1, characterized in that said neutralized glycerol is subjected to a separation treatment prior to said low-boiling removal step, said separation treatment comprising the steps of: and adding ethanol into the neutralization glycerol until no precipitate is separated out from the neutralization glycerol, stopping adding ethanol, and carrying out suction filtration to obtain the neutralization glycerol subjected to separation treatment.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101058528A (en) * | 2007-05-30 | 2007-10-24 | 吴江市方霞企业信息咨询有限公司 | Method of separating glycerin |
| CN101423456A (en) * | 2008-12-02 | 2009-05-06 | 昆明理工大学 | Recovery and purification method of glycerol as by-product of biodiesel production prepared by Jatrohpa curcas seed oil |
| EP2308818A1 (en) * | 2009-09-30 | 2011-04-13 | Rhodia Poliamida E Especialidades Ltda | Process for the purification of crude alkaline glycerol |
| CN102952000A (en) * | 2012-10-26 | 2013-03-06 | 江苏洁美生物能源有限公司 | Refining process of biodiesel byproduct crude glycerol |
| CN104262098A (en) * | 2013-12-11 | 2015-01-07 | 宁波杰森绿色能源科技有限公司 | Comprehensive utilization method of biodiesel byproduct crude glycerol |
| CN104262102A (en) * | 2014-10-16 | 2015-01-07 | 佛山市天晟隆油脂化工有限公司 | Glycerine refining method |
| CN109721471A (en) * | 2017-10-27 | 2019-05-07 | 中国石油化工股份有限公司 | A method of the Purifing of Glycerol from the by-product of production biodiesel |
| CN112694946A (en) * | 2021-01-19 | 2021-04-23 | 南昌大学 | Method for removing aflatoxin in grease |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BR112012025043A2 (en) * | 2010-04-02 | 2018-07-24 | Envirosource Inc | system and methods for processing glycerol |
| FR3002936B1 (en) * | 2013-03-06 | 2015-03-06 | Arkema France | USE OF SULFONIC ACID FOR THE RECOVERY OF GLYCEROL RESULTING FROM TRIGLYCERIDE TRANS-ESTERIFICATION REACTION |
-
2022
- 2022-04-27 CN CN202210450416.8A patent/CN114773155B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101058528A (en) * | 2007-05-30 | 2007-10-24 | 吴江市方霞企业信息咨询有限公司 | Method of separating glycerin |
| CN101423456A (en) * | 2008-12-02 | 2009-05-06 | 昆明理工大学 | Recovery and purification method of glycerol as by-product of biodiesel production prepared by Jatrohpa curcas seed oil |
| EP2308818A1 (en) * | 2009-09-30 | 2011-04-13 | Rhodia Poliamida E Especialidades Ltda | Process for the purification of crude alkaline glycerol |
| CN102952000A (en) * | 2012-10-26 | 2013-03-06 | 江苏洁美生物能源有限公司 | Refining process of biodiesel byproduct crude glycerol |
| CN104262098A (en) * | 2013-12-11 | 2015-01-07 | 宁波杰森绿色能源科技有限公司 | Comprehensive utilization method of biodiesel byproduct crude glycerol |
| CN104262102A (en) * | 2014-10-16 | 2015-01-07 | 佛山市天晟隆油脂化工有限公司 | Glycerine refining method |
| CN109721471A (en) * | 2017-10-27 | 2019-05-07 | 中国石油化工股份有限公司 | A method of the Purifing of Glycerol from the by-product of production biodiesel |
| CN112694946A (en) * | 2021-01-19 | 2021-04-23 | 南昌大学 | Method for removing aflatoxin in grease |
Non-Patent Citations (2)
| Title |
|---|
| 从生物柴油副产物中提纯甘油的预处理实验;王治敏等;《太阳能学报》;第34卷(第8期);第1458-1463页 * |
| 尤凯尔逊主编.《基本有机合成工艺学》.化学工业出版社,1960,第380-381段. * |
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