CN101649252B - Alkali-refining process of vegetable oil with high content of unsaturated acid - Google Patents
Alkali-refining process of vegetable oil with high content of unsaturated acid Download PDFInfo
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- CN101649252B CN101649252B CN2009100343994A CN200910034399A CN101649252B CN 101649252 B CN101649252 B CN 101649252B CN 2009100343994 A CN2009100343994 A CN 2009100343994A CN 200910034399 A CN200910034399 A CN 200910034399A CN 101649252 B CN101649252 B CN 101649252B
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Abstract
The invention relates to an alkali-refining process of vegetable oil with high content of unsaturated acid, belonging to the technical field of the vegetable oil refining. Adopting the long-time mixing/short-time mixing (two-time soapstock removing) and one-time washing or adopting long-time mixing/short-time mixing (one-time soapstock removing) and two-time washing, the invention optimally combines together the prior various alkali-refining processes. The invention adopts three centrifugal machines, wherein the two-time soapstock removing is carried out by the No. 1 centrifugal machine and the No. 2 centrifugal machine, and the washing is carried out by the No. 3 centrifugal machine; and the one-time soapstock removing is carried out by the No. 1 centrifugal machine, and the two-time washing is carried out by the No. 2 centrifugal machine and the No. 3 centrifugal machine. The invention overcomes the defect that the prior various alkali-refining processes can not meet the refining of part of oil with high content of unsaturated acid, such as the corn oil, and the invention has good alkali-refining effect and high comprehensive benefit, is beneficial to the improvement of the product quality and the economic benefit, can realize alkali-refining process by one-time soapstock removing and one-time washing through controlling a sluice valve which is arranged in a pipe and has wide application range and high economic benefit.
Description
Technical field
The present invention relates to the high alkali-refining process of vegetable oil of a kind of content of unsaturated acid, belong to the vegetable oil refining technical field.
Background technology
The typical alkali-refining process of existing vegetables oil is for once taking off soap, a washing process; This technology is divided into " long mixing " alkali-refining process and " short mixing " alkali-refining process according to the length of neutralization reaction time again; Above-mentioned alkali-refining process is only applicable to the oil plant of crude oil quality better; If the original quality of vegetables oil is very poor, then need adopt twice alkali-refining process (twice take off soap)+washing process or an alkali-refining process (once taking off soap)+twice washing process.
Be directed to the oil plant that often changes as corn wet goods crude oil quality, above-mentioned any technology all can't satisfy the needs of alkali refining.
Summary of the invention
The purpose of this invention is to provide the high alkali-refining process of vegetable oil of a kind of content of unsaturated acid; Solve the alkali refining that existing alkali-refining process can't satisfy the oil plant that often changes like corn wet goods crude oil quality; Realize that through the present invention alkali refining is effective; Comprehensive benefit is high, helps improving the quality of products and economic benefit.
The objective of the invention is to realize through following technical scheme; The alkali-refining process of vegetable oil that a kind of content of unsaturated acid is high; It is characterized in that; Described technology successively by long mix, short mix with take off soap for twice, washing step combines or by longly mix, short mixed with once take off soap, twice washing step combines, the oil after the washing gets into next workshop section after the moisture eliminator drying.
Described length is mixed, short exit of mixing the modified jar of acidifying in the operation connects the vertical-overflow pipeline that is provided with, the fixing different modified time of valve regulated raw oil acidifying of some height on the pipeline; Exit in alkali time-delay jar connects the vertical-overflow pipeline that is provided with, the time of the different valve regulated alkali neutralization reaction of fixing some groups of height on the pipeline.
Described to take off soap, washing step for twice be the oil of acidifying after modified gets into first alkali mixing tank through pump delivery and alkali lye from the alkali jar, and when crude oil acid value 2～4, alkali lye is 20 Baume alkali lye, 113.1～226.2L/H; Oil after first alkali mixer mixing gets into alkali time-delay jar and carries out neutralization reaction, and neutralization reaction is after 80～90 ℃ of pump delivery to heater heats, and oil gets into first whizzer that takes off soap through pipe laying and takes off soap; The oil that takes off behind the soap gets into second alkali mixing tank with alkali lye from the alkali jar; When crude oil acid value 2～4, alkali lye is 20 Baume alkali lye, 28.3～56.6L/H, and second of mixed oil entering setting is taken off the soap whizzer and take off soap; Taking off the soap whizzer through second takes off vegetables oil behind the soap and gets into heater heats to 90 ℃; In the washing mixing tank with from the hot water of BW T with from the phosphoric acid solution thorough mixing of acid jar, add hot water quality account for 5～10% of oil quality, add phosphoric acid solution quality account for 0.05 of oil quality～0.2 ‰; Get into the washing surge tank subsequently; Get into the washing whizzer then and wash separation, the oil after the washing gets into moisture eliminator 19, and dried oil gets into next workshop section.
It is described that once to take off soap, twice washing step be the oil of acidifying after modified gets into first alkali mixing tank through pump delivery and alkali lye from the alkali jar; When crude oil acid value 2～4; Alkali lye is 20 Baume alkali lye, 113.1～226.2L/H; Oil after first alkali mixer mixing gets into alkali time-delay jar and carries out neutralization reaction, and neutralization reaction is after 80～90 ℃ of pump delivery to heater heats, and oil gets into first whizzer that takes off soap through pipe laying and takes off soap; Washing for the first time is first and takes off the oil that the soap whizzer takes off behind the soap and be mixed into second alkali mixing tank with 93～97 ℃ hot water from BW T; Second of mixed oil entering taken off the soap whizzer and washed; Oil after the washing is through 88～92 ℃ of pump delivery to interchanger heating; Heating back with get into the washing mixing tank from the hot water of 93～97 ℃ of BW Ts with from the phosphoric acid solution thorough mixing of acid jar, add hot water quality account for 5～10% of oil quality, add phosphoric acid solution quality account for 0.05 of oil quality～0.2 ‰; Get into the washing surge tank subsequently; Get into the washing whizzer again and carry out the washing separation second time, the oil after the washing gets into moisture eliminator, and dried oil gets into next workshop section.
The present invention through adopt long mixing/short mix with take off for twice soap, once washing or long mixing/short mixed with once take off the alkali-refining process that soap, twice washing combine; Be optimum combination to existing various alkali-refining process; The present invention adopts 3 bench centrifuges; What is called is taken off soap for twice, once washing is that 1, No. 2 whizzer takes off soap, No. 3 whizzer washings; Once take off soap, twice washing is that No. 1 whizzer takes off soap, the washing of 2, No. 3 whizzers; The present invention has overcome existing various alkali-refining process and only has been suitable for the metastable oil plant refining like VT 18, rapeseed oil of oil plant quality; And can't satisfy the high refining of content of unsaturated acid like corn wet goods part oil plant; Alkali refining of the present invention is effective; Comprehensive benefit is high, helps improving the quality of products and economic benefit; The present invention also can realize once taking off soap and adds the once alkali-refining process of washing through controlling ducted gate valve, and the present invention is applied widely, has very high economic benefit.
Accompanying drawing is described
Fig. 1 is a process flow sheet of the present invention.
Embodiment
Further specify the present invention in conjunction with accompanying drawing and embodiment; As shown in Figure 1; Overflow outlet line 5 has been installed in long mixed, the short outlet that mixes the modified jar 5 of acidifying in the operation additional among the present invention "; the different valve of several groups of height through installing on the pipeline is regulated the modified time of raw oil acidifying, has installed overflow outlet line 8 additional in the outlet of alkali time-delay jar 8 ", regulate the time of alkali neutralization reaction through the different valve of installing on the pipeline of several groups of height; Through above Process configuration, realize long mixing on the alkali-refining process/short mutual switching that mixes.
As shown in Figure 1, take off soap whizzer 11, take off among both any one of soap whizzer 13 and all can form an alkali-refining process that takes off soap, a washing with washing whizzer 18.Its technological process is following: raw oil gets into sour mixing tank 4 through pipe laying 1 through interchanger 2,3 heating back, mixes with phosphoric acid solution from acid tube 27, gets into the modified jar 5 of acidifying subsequently; Oil after acidifying is modified delivers into alkali mixing tank 7 through pump 6, mixes with alkali lye from alkali jar 30, when crude oil acid value 2～4; Alkali lye is 20 Baume alkali lye, 113.1～226.2L/H, and mixed oil gets into alkali time-delay jars 8 and carries out neutralization reaction, with after pump 9 carry; 80～90 ℃ of heater via 10 heating, oil can select to get into any of taking off in the soap whizzer 11,13 through pipe laying remove to take off soap, and the oil that takes off behind the soap is carried through pump 14; Through 80～90 ℃ of interchanger 15 heating, get into washing mixing tank 16, and from the hot water of BW T 25 with from the phosphoric acid solution thorough mixing of acid jars 27; Add hot water quality account for 5～10% of oil quality; Add phosphoric acid solution quality account for 0.05 of oil quality～0.2 ‰, get into washing surge tank 17 subsequently, get into washing whizzer 18 then and wash separation; Oil after the washing gets into moisture eliminator 19, and dried oil gets into next workshop section.
As shown in Figure 1, take off soap whizzer 11 and take off soap whizzer 13 and can form with washing whizzer 18 and take off soap twice and add the once alkali-refining process of washing.Its technological process is following: raw oil gets into sour mixing tank 4 through pipe laying 1 through interchanger 2,3 heating back, mixes with phosphoric acid solution from acid tube 27, gets into the modified jar 5 of acidifying subsequently; Oil after acidifying is modified delivers into alkali mixing tank 7 through pump 6, mixes with alkali lye from alkali jar 30, when crude oil acid value 2～4; Alkali lye is 20 Baume alkali lye, 113.1～226.2L/H, and mixed oil gets into alkali time-delay jars 8 and carries out neutralization reaction, with after pump 9 carry; 80～90 ℃ of heater via 10 heating, oil can be selected to get into and taken off soap whizzer 11 and take off soap through pipe laying, and the oil that takes off behind the soap gets into alkali mixing tank 12; Mix with the alkali lye from alkali jar 30, when crude oil acid value 2～4, alkali lye is 20 Baume alkali lye, 28.3～56.6L/H; Mixed oil entering is taken off soap whizzer 13 and is taken off soap, and the oil after secondary takes off soap is carried through pump 14, through 80～90 ℃ of interchanger 15 heating; Get into washing mixing tank 16, and from the hot water of BW T 25 with from the phosphoric acid solution thorough mixing of acid jars 27, add hot water quality account for 5～10% of oil quality; Add phosphoric acid solution quality account for 0.05 of oil quality～0.2 ‰, get into washing surge tank 17 subsequently, get into washing whizzer 18 then and wash separation; Oil after the washing gets into moisture eliminator 19, and dried oil gets into next workshop section.
As shown in Figure 1, take off soap whizzer 11 and take off soap whizzer 13 alkali-refining process of alkali refining+twice washing of washing whizzer 18 compositions together.Its technological process is following: raw oil gets into sour mixing tank 4 through pipe laying 1 through interchanger 2,3 heating back, mixes with phosphoric acid solution from acid tube 27, gets into the modified jar 5 of acidifying subsequently; Oil after acidifying is modified delivers into alkali mixing tank 7 through pump 6, mixes with alkali lye from alkali jar 30, when crude oil acid value 2～4; Alkali lye is 20 Baume alkali lye, 113.1～226.2L/H, and mixed oil gets into alkali time-delay jars 8 and carries out neutralization reaction, with after pump 9 carry; 80～90 ℃ of heater via 10 heating, oil can be selected to get into and taken off soap whizzer 11 and take off soap through pipe laying, and the oil that takes off behind the soap gets into alkali mixing tank 12; Mix with hot water from BW T 25; Mixed oil gets into and takes off soap whizzer 13 and wash operation, here, alkali mixing tank 12 with take off soap whizzer 13 and all use as washing mixing tank and washing whizzer.Oil after the washing is carried through pump 14, through 80～90 ℃ of interchanger 15 heating, gets into washing mixing tank 16; With from the hot water of BW T 25 with from the phosphoric acid solution thorough mixing of acid jars 27, add hot water quality account for 5～10% of oil quality, add phosphoric acid solution quality account for 0.05 of oil quality～0.2 ‰; Get into washing surge tank 17 subsequently; Get into washing whizzer 18 then and carry out the washing separation second time, the oil after the secondary water washing gets into moisture eliminator 19, and dried oil gets into next workshop section.
Used acidifying is modified jar 5 among the present invention, alkali time-delay jars 8, interchanger 2,3,15, and sour mixing tank 4,16 takes off soap whizzer 11, takes off soap whizzer 13, washing whizzer 18, washing surge tank 17, moisture eliminator 19, alkali mixing tank 7,12 is currently available products.
Claims (1)
1. alkali-refining process of vegetable oil that content of unsaturated acid is high; It is characterized in that; Described technology successively by long mix, short mix with take off soap for twice, washing step combines or by longly mix, short mixed with once take off soap, twice washing step combines, the oil after the washing gets into next workshop section after the moisture eliminator drying;
Described length is mixed, short exit of mixing the modified jar of acidifying in the operation connects the vertical-overflow pipeline that is provided with, the fixing different modified time of valve regulated raw oil acidifying of some height on the pipeline; Exit in alkali time-delay jar connects the vertical-overflow pipeline that is provided with, the time of the different valve regulated alkali neutralization reaction of fixing some groups of height on the pipeline;
Described to take off soap, washing step for twice be the oil of acidifying after modified gets into first alkali mixing tank through pump delivery and alkali lye from the alkali jar, and when crude oil acid value 2～4, alkali lye is 20 Baume alkali lye, 113.1～226.2L/H; Oil after first alkali mixer mixing gets into alkali time-delay jar and carries out neutralization reaction, and neutralization reaction is after 80～90 ℃ of pump delivery to heater heats, and oil gets into first whizzer that takes off soap through pipe laying and takes off soap; The oil that takes off behind the soap gets into second alkali mixing tank with alkali lye from the alkali jar; When crude oil acid value 2～4, alkali lye is 20 Baume alkali lye, 28.3～56.6L/H, and second of mixed oil entering setting is taken off the soap whizzer and take off soap; Taking off the soap whizzer through second takes off vegetables oil behind the soap and gets into heater heats to 90 ℃; In the washing mixing tank with from the hot water of BW T with from the phosphoric acid solution thorough mixing of acid jar, add hot water quality account for 5～10% of oil quality, add phosphoric acid solution quality account for 0.05 of oil quality～0.2 ‰; Get into the washing surge tank subsequently; Get into the washing whizzer then and wash separation, the oil after the washing gets into moisture eliminator, and dried oil gets into next workshop section;
It is described that once to take off soap, twice washing step be the oil of acidifying after modified gets into first alkali mixing tank through pump delivery and alkali lye from the alkali jar; When crude oil acid value 2～4; Alkali lye is 20 Baume alkali lye, 113.1～226.2L/H; Oil after first alkali mixer mixing gets into alkali time-delay jar and carries out neutralization reaction, and neutralization reaction is after 80～90 ℃ of pump delivery to heater heats, and oil gets into first whizzer that takes off soap through pipe laying and takes off soap; Washing for the first time is first and takes off the oil that the soap whizzer takes off behind the soap and be mixed into second alkali mixing tank with 93～97 ℃ hot water from BW T; Second of mixed oil entering taken off the soap whizzer and washed; Oil after the washing is through 88～92 ℃ of pump delivery to interchanger heating; Heating back with get into the washing mixing tank from the hot water of 93～97 ℃ of BW Ts with from the phosphoric acid solution thorough mixing of acid jar, add hot water quality account for 5～10% of oil quality, add phosphoric acid solution quality account for 0.05 of oil quality～0.2 ‰; Get into the washing surge tank subsequently; Get into the washing whizzer again and carry out the washing separation second time, the oil after the washing gets into moisture eliminator, and dried oil gets into next workshop section.
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Citations (5)
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|---|---|---|---|---|
| CN86105538A (en) * | 1986-07-25 | 1988-02-24 | 平乡县粮食局油脂加工厂 | A kind of method for refining raw food oil |
| CN1931982A (en) * | 2006-09-30 | 2007-03-21 | 白长军 | Mixed cotton seed oil refining process |
| CN1931983A (en) * | 2006-09-30 | 2007-03-21 | 白长军 | Improved caustic refining process for oil and fat |
| CN101238889A (en) * | 2008-03-14 | 2008-08-13 | 江南大学 | Method for refining rice bran oil by mixing crude rice bran oil refining technique |
| CN101455242A (en) * | 2008-12-26 | 2009-06-17 | 河南华泰粮油机械工程有限公司 | Rice bran first-level oil refinement production method |
-
2009
- 2009-08-28 CN CN2009100343994A patent/CN101649252B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86105538A (en) * | 1986-07-25 | 1988-02-24 | 平乡县粮食局油脂加工厂 | A kind of method for refining raw food oil |
| CN1931982A (en) * | 2006-09-30 | 2007-03-21 | 白长军 | Mixed cotton seed oil refining process |
| CN1931983A (en) * | 2006-09-30 | 2007-03-21 | 白长军 | Improved caustic refining process for oil and fat |
| CN101238889A (en) * | 2008-03-14 | 2008-08-13 | 江南大学 | Method for refining rice bran oil by mixing crude rice bran oil refining technique |
| CN101455242A (en) * | 2008-12-26 | 2009-06-17 | 河南华泰粮油机械工程有限公司 | Rice bran first-level oil refinement production method |
Non-Patent Citations (3)
| Title |
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| 仲琪生等.连续式低温长混工艺精炼棉籽毛油的实践.《中国棉花加工》.2008,(第1期), * |
| 周文龙.低温长混二次碱炼工艺在棉籽油精炼中的应用.《中国油脂》.2005,第30卷(第10期), * |
| 孙泽清.浅析大豆油连续碱炼的影响因素.《中国油脂》.2008,第33卷(第7期), * |
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Owner name: MAYANDE GROUP CO., LTD. Free format text: FORMER NAME: JIANGSU MUYANG MYANDE FOOD MACHINERY CO., LTD. |
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Address after: 225127 Yangzhou Province, Hanjiang Industrial Park, Jiangsu Road, No. 1, No. 1 Patentee after: Mayande Group Co., Ltd. Address before: 215127 No. 198, Ji'an Road, Hanjiang District, Jiangsu, Yangzhou Patentee before: Jiangsu Muyang Myande Food Machinery Co., Ltd. |
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