CN104232298A - Oil and fat refining process - Google Patents
Oil and fat refining process Download PDFInfo
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- CN104232298A CN104232298A CN201410380068.7A CN201410380068A CN104232298A CN 104232298 A CN104232298 A CN 104232298A CN 201410380068 A CN201410380068 A CN 201410380068A CN 104232298 A CN104232298 A CN 104232298A
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Abstract
The invention provides an oil and fat refining process which comprises the following steps: a degumming and alkali refining process, a decoloring process and a deodorizing process, wherein a proper amount of phosphoric acid is added in the degumming and alkali refining process, so that non-hydrated phospholipid is converted into hydrated phospholipid, the sedimentation velocity of the phospholipid is accelerated, the oil content of oil feet is reduced, and the hydration effect is enhanced; and a clay regeneration process is added in the decoloring process, so that waste clay is prevented from becoming an industrial waste residue, and an even more important fact is that the recycling of the clay not only has better social benefit in environmental protection and treatment of three wastes, but also has certain economic benefit.
Description
Technical field
The present invention relates to lipid technique, particularly relate to a kind of oil refining process.
Background technology
Oil and fat refining, refers to the general designation of the series of processes removing contained solid impurity, free fatty acids, phosphatide, colloid, wax, pigment, peculiar smell etc. in vegetables oil.In the recent decade, along with edible oil factory large scale development, refining raw food oil technical development is rapid, and fats and oils processing has become the very considerable essential industry of one.But, because small profit margin processed by crude oil and refining processed oil, therefore, production cost reduce and energy-conservation, seem particularly important.Meanwhile, lower environmental influence in oil and fat refining, and waste such as effectively to utilize become important topic at the relation technological researching.In addition, people constantly propose new requirement to edible oil quality and quality, and except raising organoleptic quality and high stability, edible oil also must meet various nutrition aspects performance, reduce and generate trans fatty acid when deodorization, reduce and come from external contaminant and the polymkeric substance etc. such as agricultural chemicals.For adapting to these requirements, the necessary constantly timely replacement of refining techniques, makes many new refinery practices arise at the historic moment.Application number is that 201110161814.X discloses a kind of oil and fat refining method, and its step comprises acid-respons, depickling, comes unstuck and drying, and this invention effectively avoids the problem of grease emulsifying, fat degumming difficulty.But this invented technology is also imperfect, does not relate to the decolouring of grease, deodorizing technology, and the oil quality after refining is poor.
Summary of the invention
For the deficiency that prior art exists, the invention provides a kind of oil refining process.
For realizing object of the present invention, technical scheme of the present invention is as follows:
A kind of oil refining process, its processing step is as follows:
(1) come unstuck alkali-refining process: by crude oil through crude oil strainer removing impurity laggard enter plate type steam heating device, be heated to 75-80 DEG C, send into acid-respons tank after adding 80% phosphoric acid mixing, stop 15-30min, be delivered to plate type water cooler afterwards and be cooled to 60-75 DEG C, add sig water, enter neutralization reaction tank after mixing, stop 30-45min, enter whizzer and be separated, oil after separation enters vacuum drier dehydration, proceeds to bleaching workshop section;
(2) decoloration process: the alkali refining oil that comes unstuck delivers to plate heater by transferpump, be heated to 115-130 DEG C, enter carclazyte mixing tank and enter bleaching tower with overflow after quantitative carclazyte mixing 15-30min, stop 30-45min, deliver into vertical filter by transferpump oil is separated with carclazyte, oil is dried up by steam, enters deodorization workshop section, and the spent bleaching clay of separation is by reclaiming process recycle;
(3) deodorizing technology: enter deodorizing tower after being preheated by bleached oil, interchanger and crude oil heat exchange is entered after oil stops 90-120min in deodorizing tower, be no more than 250 DEG C, finally enter plate type water cooler and be cooled to less than 60 DEG C, add 50% saturated aqueous citric acid solution through pocket type, bar type polish filter filter after add nitrogen enter storage irrigated area.
Preferably, in step (1), the concentration of sig water controls at 10 ~ 24 ° of Be ', and the temperature of neutralization reaction is 60-65 DEG C.The add-on of phosphoric acid is the 0.28-0.3% of oil mass.
Preferably, in step (2), the reclaiming process of carclazyte is the carclazyte that will be separated, drop in leaching device, add after sulfuric acid preheating, after immersion, release mixing oil, add sulfuric acid again, lixiviate for several times, obtains spent bleaching clay of deoiling after drying, carries out roasting afterwards, carry out acidification with sulfuric acid after cooling, washing, dry grinding obtain the Regeneration Bleaching Clay.Each extraction time is 15min-20min, and temperature is 55-60 DEG C, and roasting time is 60-70min, and the sulfuric acid concentration of acidifying is 7%-10%.
Preferably, in step (3), bleached oil pre-heating temperature controls at 280-300 DEG C.
Beneficial effect: the invention provides a kind of oil refining process, its step includes the alkali-refining process that comes unstuck, decoloration process, deodorizing technology, add appropriate phosphoric acid coming unstuck in alkali-refining process, non-hydratable phospholipid is not only made to be converted into hydrated phospholipid, also accelerate the settling velocity of phosphatide simultaneously, reduce the oleaginousness of oil foot, improve aquation effect.Add clay regeneration technique in decoloration process, avoiding spent bleaching clay becomes industrial residue, the more important thing is that the recycling of carclazyte not only has good social benefit in environment protection and the disposal of three wastes, also has certain economic benefit simultaneously.
Embodiment
The technique means realized for making the present invention, creation characteristic, reaching object and effect is easy to understand, below in conjunction with embodiment, setting forth the present invention further.
Embodiment 1:
Get 1000kg rape oil crude oil, first by crude oil through crude oil strainer removing impurity laggard enter plate type steam heating device, be heated to 75 DEG C, add after 80% phosphoric acid 2.8kg mixes and send into acid-respons tank, stop 15min, be delivered to plate type water cooler afterwards and be cooled to 60 DEG C, add sig water, concentration of lye is 10 ° of Be ', neutralization reaction tank is entered after mixing, temperature of reaction is 60 DEG C, stop 30min, enter whizzer to be separated, oil after separation enters vacuum drier dehydration, proceed to bleaching workshop section, the alkali refining oil that comes unstuck delivers to plate heater by transferpump, be heated to 115 DEG C, enter carclazyte mixing tank and enter bleaching tower with overflow after quantitative carclazyte mixing 15min, stop 30min, deliver into vertical filter by transferpump oil is separated with carclazyte, oil is dried up by steam, enter deodorization workshop section.By bleached oil pre-add, deodorizing tower is entered after 280 DEG C, interchanger and crude oil heat exchange is entered after oil stops 90min in deodorizing tower, be no more than 250 DEG C, finally enter plate type water cooler and be cooled to less than 60 DEG C, add 50% saturated aqueous citric acid solution through pocket type, bar type polish filter filter after add nitrogen enter storage irrigated area.
Embodiment 2:
Get 1000kg rape oil crude oil, first by crude oil through crude oil strainer removing impurity laggard enter plate type steam heating device, be heated to 78 DEG C, add after 80% phosphoric acid 2.9kg mixes and send into acid-respons tank, stop 20min, be delivered to plate type water cooler afterwards and be cooled to 70 DEG C, add sig water, concentration of lye is 20 ° of Be ', neutralization reaction tank is entered after mixing, temperature of reaction is 63 DEG C, stop 40min, enter whizzer to be separated, oil after separation enters vacuum drier dehydration, proceed to bleaching workshop section, the alkali refining oil that comes unstuck delivers to plate heater by transferpump, be heated to 120 DEG C, enter carclazyte mixing tank and enter bleaching tower with overflow after quantitative carclazyte mixing 20min, stop 40min, deliver into vertical filter by transferpump oil is separated with carclazyte, oil is dried up by steam, enter deodorization workshop section.By bleached oil pre-add, deodorizing tower is entered after 290 DEG C, interchanger and crude oil heat exchange is entered after oil stops 100min in deodorizing tower, be no more than 250 DEG C, finally enter plate type water cooler and be cooled to less than 60 DEG C, add 50% saturated aqueous citric acid solution through pocket type, bar type polish filter filter after add nitrogen enter storage irrigated area.
Embodiment 3:
Get 1000kg rape oil crude oil, first by crude oil through crude oil strainer removing impurity laggard enter plate type steam heating device, be heated to 80 DEG C, add after 80% phosphoric acid 3kg mixes and send into acid-respons tank, stop 30min, be delivered to plate type water cooler afterwards and be cooled to 75 DEG C, add sig water, concentration of lye is 24 ° of Be ', neutralization reaction tank is entered after mixing, temperature of reaction is 65 DEG C, stop 45min, enter whizzer to be separated, oil after separation enters vacuum drier dehydration, proceed to bleaching workshop section, the alkali refining oil that comes unstuck delivers to plate heater by transferpump, be heated to 130 DEG C, enter carclazyte mixing tank and enter bleaching tower with overflow after quantitative carclazyte mixing 30min, stop 45min, deliver into vertical filter by transferpump oil is separated with carclazyte, oil is dried up by steam, enter deodorization workshop section.By bleached oil pre-add, deodorizing tower is entered after 300 DEG C, interchanger and crude oil heat exchange is entered after oil stops 120min in deodorizing tower, be no more than 250 DEG C, finally enter plate type water cooler and be cooled to less than 60 DEG C, add 50% saturated aqueous citric acid solution through pocket type, bar type polish filter filter after add nitrogen enter storage irrigated area.
By above-mentioned 3 embodiments, from three groups of data in upper table, when use embodiment 2 processing parameter time, insoluble impurities is minimum, acid number and peroxide value minimum, be now conducive to most the refining of grease.
The invention provides a kind of oil refining process, its step includes the alkali-refining process that comes unstuck, decoloration process, deodorizing technology, add appropriate phosphoric acid coming unstuck in alkali-refining process, non-hydratable phospholipid is not only made to be converted into hydrated phospholipid, also accelerate the settling velocity of phosphatide simultaneously, reduce the oleaginousness of oil foot, improve aquation effect.Add clay regeneration technique in decoloration process, avoiding spent bleaching clay becomes industrial residue, the more important thing is that the recycling of carclazyte not only has good social benefit in environment protection and the disposal of three wastes, also has certain economic benefit simultaneously.
The foregoing is only embodiments of the invention; not thereby the scope of the claims of the present invention is limited; every utilize description of the present invention to do equivalent structure or equivalent flow process conversion; or be directly or indirectly used in other relevant technical fields, be all in like manner included in scope of patent protection of the present invention.
Claims (6)
1. an oil refining process, is characterized in that, its processing step is as follows:
(1) come unstuck alkali-refining process: by crude oil through crude oil strainer removing impurity laggard enter plate type steam heating device, be heated to 75-80 DEG C, send into acid-respons tank after adding 80% phosphoric acid mixing, stop 15-30min, be delivered to plate type water cooler afterwards and be cooled to 60-75 DEG C, add sig water, enter neutralization reaction tank after mixing, stop 30-45min, enter whizzer and be separated, oil after separation enters vacuum drier dehydration, proceeds to bleaching workshop section;
(2) decoloration process: the alkali refining oil that comes unstuck delivers to plate heater by transferpump, be heated to 115-130 DEG C, enter carclazyte mixing tank and enter bleaching tower with overflow after quantitative carclazyte mixing 15-30min, stop 30-45min, deliver into vertical filter by transferpump oil is separated with carclazyte, oil is dried up by steam, enters deodorization workshop section, and the spent bleaching clay of separation is by reclaiming process recycle;
(3) deodorizing technology: enter deodorizing tower after being preheated by bleached oil, interchanger and crude oil heat exchange is entered after oil stops 90-120min in deodorizing tower, be no more than 250 DEG C, finally enter plate type water cooler and be cooled to less than 60 DEG C, add 50% saturated aqueous citric acid solution through pocket type, bar type polish filter filter after add nitrogen enter storage irrigated area.
2. a kind of oil refining process according to claim 1, is characterized in that, in step (1), the concentration of sig water controls at 10 ~ 24oBe ', and the temperature of neutralization reaction is 60-65 DEG C.
3. a kind of oil refining process according to claim 1, is characterized in that, in step (1), the add-on of phosphoric acid is the 0.28-0.3% of oil mass.
4. a kind of oil refining process according to claim 1, it is characterized in that, in step (2), the reclaiming process of carclazyte is the carclazyte that will be separated, and drops in leaching device, add after sulfuric acid preheating, release mixing oil after immersion, then add sulfuric acid, lixiviate for several times, spent bleaching clay of deoiling is obtained after drying, carry out roasting afterwards, carry out acidification after cooling with sulfuric acid, washing, dry grinding obtain the Regeneration Bleaching Clay.
5. clay regeneration technique according to claim 4, is characterized in that, each extraction time is 15min-20min, and temperature is 55-60 DEG C, and roasting time is 60-70min, and the sulfuric acid concentration of acidifying is 7%-10%.
6. a kind of oil refining process according to claim 1, is characterized in that, in step (3), bleached oil pre-heating temperature controls at 280-300 DEG C.
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| CN201410380068.7A CN104232298A (en) | 2014-08-04 | 2014-08-04 | Oil and fat refining process |
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| CN201410380068.7A CN104232298A (en) | 2014-08-04 | 2014-08-04 | Oil and fat refining process |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105062670A (en) * | 2015-08-21 | 2015-11-18 | 崇州市白头甘泉工业油脂厂 | Refining method of grease |
| CN105132149A (en) * | 2015-07-31 | 2015-12-09 | 崇州市白头甘泉工业油脂厂 | Grease refining method |
| CN107033917A (en) * | 2017-04-21 | 2017-08-11 | 安徽家壹味食品有限公司 | A kind of agricultural use method of refining raw food oil waste liquid |
| CN107118845A (en) * | 2017-05-15 | 2017-09-01 | 邵阳学院 | A kind of food engineering oil refining process and its device |
| CN108192727A (en) * | 2018-03-29 | 2018-06-22 | 洛阳康贝源食品股份有限公司 | A kind of walnut oil refining technique |
| CN109289824A (en) * | 2018-11-23 | 2019-02-01 | 山东三星玉米产业科技有限公司 | Useless atlapulgite recycling utilization production technology |
| CN109852471A (en) * | 2019-03-07 | 2019-06-07 | 四川德阳市年丰食品有限公司 | It is a kind of to refine the small manufacture craft for squeezing rapeseed oil |
| CN109852472A (en) * | 2019-03-07 | 2019-06-07 | 四川德阳市年丰食品有限公司 | A kind of squeezing refining technique for manufacturing of rapeseed oil |
| CN112175728A (en) * | 2020-10-24 | 2021-01-05 | 河南华泰粮油机械股份有限公司 | Refining and sterilizing treatment method of medicinal coconut oil |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105132149A (en) * | 2015-07-31 | 2015-12-09 | 崇州市白头甘泉工业油脂厂 | Grease refining method |
| CN105062670A (en) * | 2015-08-21 | 2015-11-18 | 崇州市白头甘泉工业油脂厂 | Refining method of grease |
| CN107033917A (en) * | 2017-04-21 | 2017-08-11 | 安徽家壹味食品有限公司 | A kind of agricultural use method of refining raw food oil waste liquid |
| CN107118845A (en) * | 2017-05-15 | 2017-09-01 | 邵阳学院 | A kind of food engineering oil refining process and its device |
| CN108192727A (en) * | 2018-03-29 | 2018-06-22 | 洛阳康贝源食品股份有限公司 | A kind of walnut oil refining technique |
| CN109289824A (en) * | 2018-11-23 | 2019-02-01 | 山东三星玉米产业科技有限公司 | Useless atlapulgite recycling utilization production technology |
| CN109852471A (en) * | 2019-03-07 | 2019-06-07 | 四川德阳市年丰食品有限公司 | It is a kind of to refine the small manufacture craft for squeezing rapeseed oil |
| CN109852472A (en) * | 2019-03-07 | 2019-06-07 | 四川德阳市年丰食品有限公司 | A kind of squeezing refining technique for manufacturing of rapeseed oil |
| CN112175728A (en) * | 2020-10-24 | 2021-01-05 | 河南华泰粮油机械股份有限公司 | Refining and sterilizing treatment method of medicinal coconut oil |
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Application publication date: 20141224 |