CN115806856A - Lard refining process - Google Patents
Lard refining process Download PDFInfo
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- CN115806856A CN115806856A CN202211596128.XA CN202211596128A CN115806856A CN 115806856 A CN115806856 A CN 115806856A CN 202211596128 A CN202211596128 A CN 202211596128A CN 115806856 A CN115806856 A CN 115806856A
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- 238000000034 method Methods 0.000 title claims abstract description 85
- 238000007670 refining Methods 0.000 title claims abstract description 70
- 239000003921 oil Substances 0.000 claims abstract description 197
- 238000009835 boiling Methods 0.000 claims abstract description 42
- 238000003723 Smelting Methods 0.000 claims abstract description 38
- 239000010779 crude oil Substances 0.000 claims abstract description 31
- 238000004332 deodorization Methods 0.000 claims abstract description 29
- 239000002994 raw material Substances 0.000 claims abstract description 17
- 230000036571 hydration Effects 0.000 claims abstract description 16
- 238000006703 hydration reaction Methods 0.000 claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 16
- 238000004140 cleaning Methods 0.000 claims abstract description 15
- 239000012535 impurity Substances 0.000 claims abstract description 14
- 239000010699 lard oil Substances 0.000 claims abstract description 13
- 230000001877 deodorizing effect Effects 0.000 claims abstract description 8
- 238000003756 stirring Methods 0.000 claims description 79
- 238000010438 heat treatment Methods 0.000 claims description 48
- 239000003513 alkali Substances 0.000 claims description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 35
- 238000005086 pumping Methods 0.000 claims description 19
- 238000001816 cooling Methods 0.000 claims description 14
- 238000002347 injection Methods 0.000 claims description 14
- 239000007924 injection Substances 0.000 claims description 14
- 238000005507 spraying Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 10
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 9
- 239000000194 fatty acid Substances 0.000 claims description 9
- 229930195729 fatty acid Natural products 0.000 claims description 9
- 150000004665 fatty acids Chemical class 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 9
- 239000000344 soap Substances 0.000 claims description 9
- 230000018044 dehydration Effects 0.000 claims description 8
- 238000006297 dehydration reaction Methods 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000005520 cutting process Methods 0.000 claims description 7
- 239000012153 distilled water Substances 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 7
- 239000002480 mineral oil Substances 0.000 claims description 7
- 235000010446 mineral oil Nutrition 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 239000008234 soft water Substances 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- 239000001397 quillaja saponaria molina bark Substances 0.000 claims 1
- 229930182490 saponin Natural products 0.000 claims 1
- 150000007949 saponins Chemical class 0.000 claims 1
- 230000009286 beneficial effect Effects 0.000 abstract description 4
- 235000019198 oils Nutrition 0.000 description 161
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 6
- 238000004062 sedimentation Methods 0.000 description 6
- 241000931143 Gleditsia sinensis Species 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000004519 grease Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000000243 solution Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 235000021588 free fatty acids Nutrition 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 235000011837 pasties Nutrition 0.000 description 1
- 230000002085 persistent effect Effects 0.000 description 1
- 150000003904 phospholipids Chemical class 0.000 description 1
- 235000015277 pork Nutrition 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005185 salting out Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000008159 sesame oil Substances 0.000 description 1
- 235000011803 sesame oil Nutrition 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
Abstract
The invention discloses a lard refining process, which comprises an oil boiling process and a refining process; the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting under negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil; the refining process comprises the following steps: and (3) carrying out hydration degumming, alkalization deacidification, adsorption decoloration and deacidification deodorization on the crude oil prepared in the oil boiling process to obtain the finished lard oil. The beneficial effects of the invention are: the refining process of the invention has the oil boiling procedure and the refining procedure to thoroughly remove impurities, and is beneficial to improving the quality of the finished lard product.
Description
Technical Field
The invention relates to the technical field of lard oil refining, in particular to a lard oil refining process.
Background
Lard, also known as lard or lard by Chinese. It is edible oil extracted from pork, which is a yellowish translucent liquid in the initial state and is white or yellowish solid at normal temperature. The lard oil mainly comprises saturated higher fatty acid glycerol and unsaturated higher fatty acid glycerol.
The lard oil refined by the traditional refining method has relatively high impurity content, the impurities are not thoroughly removed, the refining process easily influences the quality of the lard oil, and the production requirement is difficult to meet.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, provides a lard refining process, and solves the problems that the traditional refining process is not thorough in impurities and affects the lard quality.
The purpose of the invention is realized by the following technical scheme:
a lard oil refining process comprises an oil boiling process and a refining process;
the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting under negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil;
the refining process comprises the following steps: the crude oil obtained in the oil boiling process is subjected to hydration degumming, alkalization deacidification, adsorption decoloration, deacidification deodorization to obtain the finished lard.
Further, the cleaning and crushing are carried out at the temperature of 4-12 ℃, the impurity is controlled to be less than or equal to 0.1 percent, and the size of the raw material cutting block is 3-8 mm.
The raw materials are conveyed to the crusher by the conveyor to be crushed after being unpacked on the unpacking platform, the size of each block is 3-8 mm, the crushed particles are uniform, and the raw residues or scorch can appear when the raw residues or scorch is too large or too small, and the raw residues or scorch is not beneficial to oil residue separation at the same time to influence the performance of the oil press.
Further, the smelting and boiling temperature of the negative pressure smelting is 140-160 ℃, and the boiling time is as follows: 150-240 min, smelting vacuum degree: -0.03 to-0.08 Mpa.
Heating the smelting cake and simultaneously starting a stirring device to ensure that the materials are heated uniformly and do not stick to the pot, and starting vacuum dehydration after the smelting temperature reaches 85 ℃ because the raw materials have large water content.
Further, the vacuum dehydration and deodorization adopts a water injection type vacuum injection pump to generate negative pressure in the smelting pot, a condenser is arranged in a vacuum pipeline, water molecules and peculiar smell micromolecule volatile matters flow into the tube array condenser along with vacuum, and the water molecules and the peculiar smell micromolecule volatile matters are forcibly condensed into distilled water to be collected in the liquid separating tank.
Further, the oil residue separation is carried out by adopting a vacuum negative pressure separator, the separated oil residue is squeezed by an oil residue conveying oil press, and the separated crude oil enters a cooling tank for rapid cooling.
Further, the hydration degumming is to pump the crude oil into a refining tank, stir at the rotating speed of 60rpm and heat to 65-70 ℃, add the soft water at the temperature of 65-75 ℃ into the refining tank in a spraying mode, continue stirring for 30-40min, adjust the stirring speed to 20-30rpm when the colloidal particles are in an obvious analysis state, and continue stirring for 10min. Stopping stirring, standing and settling for 4-6 h, and discharging oil residue.
And (3) carrying out hydration degumming to remove peptizing impurities such as phospholipid, protein, pituitous substances and the like in the grease. Putting the discharged oil foot into a salting-out tank, adding fine salt into transparent oil foot according to the proportion of 4-5 percent of the oil foot, heating to 100-110 ℃, slightly stirring, standing, settling for 20min, then, skimming upper floating oil, discharging lower water, heating white pasty oil foot to 100 ℃, adding boiling water with the amount of 1-1.5 times of the oil foot and 1.5 percent of fine salt, stirring, heating until the oil foot is viscous, standing for 2h, discharging the oil foot, pumping the oil into a refining tank for recycling after the oil foot is discharged.
Further, the alkalization deacidification is carried out to heat oil and alkali liquor to 30-40 ℃, the oil is quickly stirred in a refining pot, the alkali liquor is added in a spraying alkali adding mode within 10-15 min, the quick stirring is continued for about 30min after the alkali liquor is added, the oil is heated when the oil-soap begins to be in a separation state, the stirring speed is reduced, the oil temperature is raised to 60-65 ℃, the heating is stopped, the stirring speed is reduced, the stirring is continued for 15min, the stirring is stopped, the standing sedimentation is carried out, and the soapstock mixture after the alkali reaction enters a soapstock pool.
The alkalization deacidification is used for removing free fatty acid in the crude oil, increasing the transparency of the oil, reducing smoke point and preventing oxidative deterioration. When the alkali liquor is NaOH solution and the soapstock is sticky and in a relatively persistent suspension state after reaching the final temperature, adding clear water and dilute salt water which have the same temperature as the oil or slightly lower temperature than the oil for pressing water to increase the specific gravity of the soap particles after absorbing water and rapidly sink. Adding softened water into the alkalized grease for washing, removing residual soap in the grease, wherein the washing frequency is until the waste water is transparent and neutral.
Further, pumping the oil into a decoloring tank for adsorption decoloring, heating to 80-90 ℃, keeping the vacuum degree at 0.080MPa, adding argil after dewatering until no bubbles are generated on the oil surface, controlling the vacuum degree at 0.095MPa, and decoloring after 20-30 min, reducing the oil temperature and filtering out waste argil.
Dewatering until no bubble is generated to obtain the original thick sesame oil, discharging and storing or further adding argil for adsorption and decoloration, wherein an argil suction port valve is not suitable to be opened too much in the argil adding process to reduce the air suction amount.
Further, the deacidification and deodorization step comprises the steps of firstly feeding oil to be deodorized into a gas separator, removing air in the oil in vacuum, pumping the oil out by a pump, heating the oil by an oil-oil heat exchanger, heating the oil by a mineral oil heater to 240-265 ℃, feeding the oil into a deodorization tower from the top, and removing fatty acid and odor components in the oil.
Further, the addition amount of the argil is 2.5-5% of the oil weight.
The invention has the following advantages:
the refining process of the invention has the oil boiling procedure and the refining procedure to thoroughly remove impurities, which is beneficial to improving the quality of the finished lard product.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the embodiments of the present invention will be described in detail and completely with reference to the accompanying drawings.
Thus, the following detailed description of embodiments of the invention is not intended to limit the scope of the invention as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention.
It should be noted that the embodiments and features of the embodiments of the present invention may be combined with each other without conflict.
Example 1
A lard oil refining process comprises an oil boiling process and a refining process;
the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting under negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil;
the refining process comprises the following steps: the crude oil obtained in the oil boiling process is subjected to hydration degumming, alkalization deacidification, adsorption decoloration, deacidification deodorization to obtain the finished lard.
Cleaning and crushing are carried out at the temperature of 12 ℃, impurities are controlled to be less than or equal to 0.1 percent, and the size of a raw material cutting block is 3mm;
the smelting and boiling temperature of the negative pressure smelting is 140 ℃, and the boiling time is as follows: 240min, smelting vacuum degree: -0.08Mpa;
the vacuum dehydration and deodorization adopts a water injection type vacuum injection pump to generate negative pressure in the smelting pot, a condenser is arranged in a vacuum pipeline, water molecules and peculiar smell micromolecule volatile matters flow into a tube array condenser along with vacuum, and are forcibly condensed into distilled water to be collected in a liquid separating tank;
the oil residue separation is carried out by adopting a vacuum negative pressure separator, the separated oil residue is squeezed by an oil residue conveying oil press, and the separated crude oil enters a cooling tank for quick cooling;
the hydration degumming method comprises the steps of pumping crude oil into a refining tank, stirring at a rotating speed of 60rpm, heating to 65 ℃, adding soft water at 65 ℃ into the refining tank in a spraying mode, continuously stirring for 40min, adjusting the stirring speed to 20rpm when colloidal particles are in an obvious analysis state, and then continuously stirring for 10min. Stopping stirring, standing and settling for 4h, and discharging oil residue;
the method comprises the following steps of heating oil and alkali liquor to 40 ℃ by the alkalization deacidification, rapidly stirring the oil in a refining pot, adding the alkali liquor in a spraying alkali adding mode once within 15min, continuously and rapidly stirring for about 30min after the alkali liquor is added, heating the oil when the oil-soap begins to be in a separated state, reducing the stirring speed, stopping heating when the oil temperature is raised to 60 ℃, reducing the stirring speed, continuously stirring for 15min, stopping stirring, standing for sedimentation, and allowing a nigre mixture after alkali reaction to enter a gleditsia sinensis lam pond;
pumping oil into a decoloring tank for adsorption decoloring, heating to 90 ℃, controlling the vacuum degree to be 0.080MPa, dehydrating until no bubbles are generated on the oil surface, adding argil, controlling the addition amount of the argil to be 5% of the weight of the oil, controlling the vacuum degree to be 0.095MPa, decoloring after 20min, reducing the oil temperature and filtering out waste argil;
the deacidification and deodorization step comprises the steps of firstly feeding oil to be deodorized into a gas separator, removing air in the oil in vacuum, pumping out the oil by a pump, heating the oil by an oil-oil heat exchanger, heating the oil by a mineral oil heater to 240 ℃, feeding the oil into a deodorization tower from the top, and removing fatty acid and odor components in the oil.
Example 2
A process for refining lard oil comprises an oil boiling procedure and a refining procedure;
the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting under negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil;
the refining process comprises the following steps: the crude oil obtained in the oil boiling process is subjected to hydration degumming, alkalization deacidification, adsorption decoloration, deacidification deodorization to obtain the finished lard.
Cleaning and crushing are carried out at 4 ℃, impurities are controlled to be less than or equal to 0.1 percent, and the size of a raw material cutting block is 8mm;
the smelting and boiling temperature of the negative pressure smelting is 160 ℃, and the boiling time is as follows: 150min, smelting vacuum degree: -0.03Mpa;
the vacuum dehydration and deodorization adopts a water injection type vacuum injection pump to generate negative pressure in the smelting pot, a condenser is arranged in a vacuum pipeline, water molecules and peculiar smell micro-molecule volatile matters flow along with vacuum to enter a tube array condenser, and the water molecules and the peculiar smell micro-molecule volatile matters are forcedly condensed into distilled water to be collected in a liquid separation tank;
the oil residue separation is carried out by adopting a vacuum negative pressure separator, the separated oil residue is squeezed by an oil residue conveying oil press, and the separated crude oil enters a cooling tank for quick cooling;
the hydration degumming is to pump the crude oil into a refining tank, stir at the rotating speed of 60rpm and heat to 70 ℃, add the soft water at the temperature of 75 ℃ into the refining tank in a spraying mode, continue stirring for 30min, adjust the stirring speed to 30rpm when the colloidal particles are in an obvious analysis state, and continue stirring for 10min. After stirring is stopped, standing and settling for 6 hours, and discharging oil residue;
the method comprises the following steps of heating oil and alkali liquor to 30 ℃ by the alkalization deacidification, rapidly stirring the oil in a refining pot, adding the alkali liquor in a spraying alkali adding mode for 10min, continuously and rapidly stirring for about 30min after the alkali liquor is added, heating the oil when the oil-soap begins to be in a separated state, reducing the stirring speed, stopping heating when the oil is heated to 65 ℃, reducing the stirring speed, continuously stirring for 15min, stopping stirring, standing for sedimentation, and allowing a nigre mixture after alkali reaction to enter a gleditsia sinensis lam pond;
pumping oil into a decoloring tank for adsorption decoloring, heating to 80 ℃, controlling the vacuum degree to be 0.080MPa, dehydrating until no bubbles are generated on the oil surface, adding argil, controlling the addition amount of the argil to be 2.5 percent of the weight of the oil, controlling the vacuum degree to be 0.095MPa, decoloring after 30min, reducing the oil temperature and filtering out waste argil;
the deacidification and deodorization step comprises the steps of firstly feeding oil to be deodorized into a gas separator, removing air in the oil in vacuum, pumping the oil out by a pump, heating the oil by an oil-oil heat exchanger, heating the oil by a mineral oil heater to 265 ℃, feeding the oil into a deodorization tower from the top, and removing fatty acid and odor components in the oil.
Example 3
A process for refining lard oil comprises an oil boiling procedure and a refining procedure;
the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting under negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil;
the refining process comprises the following steps: the crude oil obtained in the oil boiling process is subjected to hydration degumming, alkalization deacidification, adsorption decoloration, deacidification deodorization to obtain the finished lard.
Cleaning and crushing are carried out at the temperature of 8 ℃, impurities are controlled to be less than or equal to 0.1 percent, and the size of a raw material cutting block is 6mm;
the smelting and boiling temperature of the negative pressure smelting is 150 ℃, and the boiling time is as follows: 200min, smelting vacuum degree: -0.06Mpa;
the vacuum dehydration and deodorization adopts a water injection type vacuum injection pump to generate negative pressure in the smelting pot, a condenser is arranged in a vacuum pipeline, water molecules and peculiar smell micro-molecule volatile matters flow along with vacuum to enter a tube array condenser, and the water molecules and the peculiar smell micro-molecule volatile matters are forcedly condensed into distilled water to be collected in a liquid separation tank;
the oil residue separation is carried out by adopting a vacuum negative pressure separator, the separated oil residue is squeezed by an oil residue conveying oil press, and the separated crude oil enters a cooling tank for quick cooling;
the hydration degumming method comprises the steps of pumping crude oil into a refining tank, stirring at a rotating speed of 60rpm, heating to 68 ℃, adding soft water at 72 ℃ into the refining tank in a spraying mode, continuously stirring for 38min, adjusting the stirring speed to 25rpm when colloidal particles are in an obvious analysis state, and then continuously stirring for 10min. Stopping stirring, standing and settling for 5h, and discharging oil residue;
the method comprises the following steps of heating oil and alkali liquor to 35 ℃ by the alkalization deacidification, rapidly stirring the oil in a refining pot, adding the alkali liquor in a spraying alkali adding mode once within 12min, continuously and rapidly stirring for about 30min after the alkali liquor is added, heating the oil when the oil-soap begins to be in a separated state, reducing the stirring speed, stopping heating when the oil temperature is raised to 62 ℃, reducing the stirring speed, continuously stirring for 15min, stopping stirring, standing for sedimentation, and allowing a nigre mixture after alkali reaction to enter a gleditsia sinensis lam pond;
pumping oil into a decoloring tank for adsorption decoloring, heating to 85 ℃, controlling the vacuum degree to be 0.080MPa, dehydrating until no bubbles are generated on the oil surface, adding argil, controlling the addition amount of the argil to be 4% of the oil weight, controlling the vacuum degree to be 0.095MPa, decoloring after 30min, reducing the oil temperature and filtering out waste argil;
the deacidification and deodorization step comprises the steps of firstly feeding oil to be deodorized into a gas separator, removing air in the oil in vacuum, pumping out the oil by a pump, heating the oil by an oil-oil heat exchanger, heating the oil by a mineral oil heater to 260 ℃, feeding the oil into a deodorization tower from the top, and removing fatty acid and odor components in the oil.
Example 4
A lard oil refining process comprises an oil boiling process and a refining process;
the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting at negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil;
the refining process comprises the following steps: the crude oil obtained in the oil boiling process is subjected to hydration degumming, alkalization deacidification, adsorption decoloration, deacidification deodorization to obtain the finished lard.
Cleaning and crushing are carried out at the temperature of 6 ℃, impurities are controlled to be less than or equal to 0.1 percent, and the size of a raw material cutting block is 5mm;
the smelting and boiling temperature of the negative pressure smelting is 155 ℃, and the boiling time is as follows: 180min, smelting vacuum degree: -0.05Mpa;
the vacuum dehydration and deodorization adopts a water injection type vacuum injection pump to generate negative pressure in the smelting pot, a condenser is arranged in a vacuum pipeline, water molecules and peculiar smell micro-molecule volatile matters flow along with vacuum to enter a tube array condenser, and the water molecules and the peculiar smell micro-molecule volatile matters are forcedly condensed into distilled water to be collected in a liquid separation tank;
the oil residue separation is carried out by adopting a vacuum negative pressure separator, the separated oil residue is squeezed by an oil residue conveying oil press, and the separated crude oil enters a cooling tank for quick cooling;
the hydration degumming is to pump the crude oil into a refining tank, stir at the rotating speed of 60rpm and heat to 66 ℃, add the soft water at 66 ℃ into the refining tank in a spraying mode, continue stirring for 36min, adjust the stirring speed to 28rpm when the colloidal particles are in an obvious analysis state, and continue stirring for 10min. Stopping stirring, standing and settling for 4.5h, and discharging oil residue;
the alkalization deacidification method comprises the steps of heating oil and alkali liquor to 38 ℃, rapidly stirring the oil in a refining pot, adding the alkali liquor in a spraying alkali adding mode once within 13min, continuously and rapidly stirring for about 30min after the alkali liquor is added, heating the oil when the oil-soap begins to be in a separated state, reducing the stirring speed, stopping heating when the oil temperature is raised to 61 ℃, reducing the stirring speed, continuously stirring for 15min, stopping stirring, standing for sedimentation, and allowing a soapstock mixture after alkali reaction to enter a soapstock pool;
pumping oil into a decoloring tank for adsorption decoloring, heating to 86 ℃, controlling the vacuum degree to be 0.080MPa, dehydrating until no bubbles are generated on the oil surface, adding argil, controlling the addition amount of the argil to be 3.2% of the weight of the oil, controlling the vacuum degree to be 0.095MPa, decoloring after 27min, reducing the oil temperature and filtering out waste argil;
the deacidification and deodorization step comprises the steps of firstly feeding oil to be deodorized into a gas separator, removing air in the oil in vacuum, pumping out the oil by a pump, heating the oil by an oil-oil heat exchanger, heating the oil by a mineral oil heater to 250 ℃, feeding the oil into a deodorization tower from the top, and removing fatty acid and odor components in the oil.
Example 5
A lard oil refining process comprises an oil boiling process and a refining process;
the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting at negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil;
the refining process comprises the following steps: the crude oil obtained in the oil boiling process is subjected to hydration degumming, alkalization deacidification, adsorption decoloration, deacidification deodorization to obtain the finished lard.
Cleaning and crushing are carried out at the temperature of 4 ℃, impurities are controlled to be less than or equal to 0.1 percent, and the size of a raw material cutting block is 7mm;
the smelting and boiling temperature of the negative pressure smelting is 150 ℃, and the boiling time is as follows: 190min, smelting vacuum degree: -0.05Mpa;
the vacuum dehydration and deodorization adopts a water injection type vacuum injection pump to generate negative pressure in the smelting pot, a condenser is arranged in a vacuum pipeline, water molecules and peculiar smell micro-molecule volatile matters flow along with vacuum to enter a tube array condenser, and the water molecules and the peculiar smell micro-molecule volatile matters are forcedly condensed into distilled water to be collected in a liquid separation tank;
the oil residue separation is carried out by adopting a vacuum negative pressure separator, the separated oil residue is squeezed by an oil residue conveying oil press, and the separated crude oil enters a cooling tank for quick cooling;
the hydration degumming method comprises the steps of pumping crude oil into a refining tank, stirring at a rotating speed of 60rpm, heating to 69 ℃, adding soft water at 71 ℃ into the refining tank in a spraying mode, continuously stirring for 37min, adjusting the stirring speed to 26rpm when colloidal particles are in an obvious analysis state, and then continuously stirring for 10min. After stirring is stopped, standing and settling for 4.2 hours, and discharging oil residue;
the alkalization deacidification method comprises the steps of heating oil and alkali liquor to 36 ℃, rapidly stirring the oil in a refining pot, adding the alkali liquor in a spraying alkali adding mode once within 11min, continuously and rapidly stirring for about 30min after the alkali liquor is added, heating the oil when the oil-soap begins to be in a separated state, reducing the stirring speed, stopping heating when the oil temperature is increased to 63 ℃, reducing the stirring speed, continuously stirring for 15min, stopping stirring, standing for sedimentation, and allowing a soapstock mixture after alkali reaction to enter a soapstock pool;
pumping oil into a decoloring tank for adsorption decoloring, heating to 89 ℃, controlling the vacuum degree to be 0.080MPa, dehydrating until no bubbles are generated on the oil surface, adding argil, controlling the addition amount of the argil to be 3.8 percent of the weight of the oil, controlling the vacuum degree to be 0.095MPa, decoloring after 30min, reducing the oil temperature and filtering out waste argil;
the deacidification and deodorization step comprises the steps of firstly feeding oil to be deodorized into a gas separator, removing air in the oil in vacuum, pumping the oil out by a pump, heating the oil by an oil-oil heat exchanger, heating the oil by a mineral oil heater to 258 ℃, feeding the oil into a deodorization tower from the top, and removing fatty acid and odor components in the oil.
The refining process adopts the oil boiling procedure and the refining procedure, the refining process is finely controlled, the impurity removal rate is improved, the removal is more thorough, and the improvement of the quality of the finished lard product is facilitated.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof.
Claims (10)
1. A lard refining process is characterized in that: comprises an oil boiling procedure and a refining procedure;
the oil boiling procedure comprises the following steps: cleaning and crushing raw materials, smelting under negative pressure, dehydrating and deodorizing in vacuum, and separating oil residues to obtain crude oil;
the refining process comprises the following steps: and (3) carrying out hydration degumming, alkalization deacidification, adsorption decoloration and deacidification deodorization on the crude oil prepared in the oil boiling process to obtain the finished lard oil.
2. The lard refining process of claim 1, characterized in that: the cleaning and crushing are carried out at the temperature of 4-12 ℃, the impurity is controlled to be less than or equal to 0.1 percent, and the size of the raw material cutting block is 3-8 mm.
3. The lard refining process of claim 1, characterized in that: the smelting and boiling temperature of the negative pressure smelting is 140-160 ℃, and the boiling time is as follows: 150-240 min, smelting vacuum degree: -0.03 to-0.08 Mpa.
4. The lard refining process of claim 1, characterized in that: the vacuum dehydration and deodorization adopts a water injection type vacuum injection pump to generate negative pressure in the smelting pot, a condenser is arranged in a vacuum pipeline, water molecules and peculiar smell micromolecule volatile matters flow into the tube array condenser along with vacuum, and the water molecules and the peculiar smell micromolecule volatile matters are forcibly condensed into distilled water to be collected in the liquid separating tank.
5. The lard refining process of claim 1, characterized in that: the oil residue separation is carried out by adopting a vacuum negative pressure separator, the separated oil residue is squeezed by an oil residue conveying oil press, and the separated crude oil enters a cooling tank for rapid cooling.
6. The lard refining process of claim 1, characterized in that: the hydration degumming method comprises the steps of pumping crude oil into a refining tank, stirring at the rotating speed of 60rpm, heating to 65-70 ℃, adding soft water at the temperature of 65-75 ℃ into the refining tank in a spraying mode, continuously stirring for 30-40min, adjusting the stirring speed to 20-30rpm when colloidal particles are in an obvious analysis state, and continuously stirring for 10min. Stopping stirring, standing and settling for 4-6 h, and discharging oil residue.
7. The lard refining process of claim 1, characterized in that: the method comprises the steps of heating oil and alkali liquor to 30-40 ℃, quickly stirring the oil in a refining pot, adding the alkali liquor in a spraying and alkali adding manner within 10-15 min, continuously and quickly stirring for about 30min after the alkali liquor is added, heating the oil when the oil-soap begins to be in a separated state, reducing the stirring speed, stopping heating when the oil temperature rises to 60-65 ℃, reducing the stirring speed, continuously stirring for 15min, stopping stirring, standing and settling, and allowing a soapstock mixture after alkali reaction to enter a saponin pool.
8. The lard refining process of claim 1, characterized in that: and (3) pumping the oil into a decoloring tank for adsorption decoloring, heating to 80-90 ℃, controlling the vacuum degree to be 0.095MPa, decoloring after 20-30 min after dewatering until no bubbles are generated on the oil surface, reducing the oil temperature and filtering out waste argil.
9. The lard refining process of claim 1, characterized in that: the deacidification and deodorization step comprises the steps of firstly feeding oil to be deodorized into a gas separator, removing air in the oil in vacuum, pumping out the oil by a pump, heating the oil by an oil-oil heat exchanger, heating the oil by a mineral oil heater to 240-265 ℃, feeding the oil into a deodorization tower from the top, and removing fatty acid and odor components in the oil.
10. The lard refining process of claim 8, characterized in that: the addition amount of the argil is 2.5-5% of the weight of the oil.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106350200A (en) * | 2016-08-28 | 2017-01-25 | 宁夏索米亚生态农业科技有限公司 | Process for refining crude vegetable oil |
| CN115029180A (en) * | 2022-06-14 | 2022-09-09 | 柞水县龙腾生态养殖有限公司 | Preparation method of emu oil |
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- 2022-12-13 CN CN202211596128.XA patent/CN115806856A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106350200A (en) * | 2016-08-28 | 2017-01-25 | 宁夏索米亚生态农业科技有限公司 | Process for refining crude vegetable oil |
| CN115029180A (en) * | 2022-06-14 | 2022-09-09 | 柞水县龙腾生态养殖有限公司 | Preparation method of emu oil |
Non-Patent Citations (1)
| Title |
|---|
| 胡前等: "猪油的连续精炼工艺与实践", 中国油脂, vol. 31, no. 3, pages 12 - 15 * |
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