CN114790410A

CN114790410A - Co-production system and process of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester

Info

Publication number: CN114790410A
Application number: CN202210413279.0A
Authority: CN
Inventors: 周红茹
Original assignee: Individual
Current assignee: Hunan Zhonggu Oil Technology Co ltd
Priority date: 2022-04-20
Filing date: 2022-04-20
Publication date: 2022-07-26

Abstract

The invention discloses a co-production system and a process of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, wherein the co-production system comprises a fatty acid extraction system, an alcoholysis system, a ferulic acid methyl ester extraction system, a fatty acid methyl ester extraction system and a phytosterol extraction system. Compared with the prior art, the co-production system and the process are used for realizing deep processing of rice bran oil, and can improve the added value of products.

Description

Co-production system and process of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester

Technical Field

The invention relates to the technical field of oil deep processing equipment, in particular to a system and a process for co-producing ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester.

Background

The rice bran oil is oil prepared by squeezing or leaching rice bran generated in the rice processing process, the rice bran contains lipase with high activity, triglyceride is hydrolyzed into free fatty acid and glycerol or glycerol mono/diglyceride, the rice bran is easy to rancidity, the acid value of the rice bran crude oil is generally high, the vast majority of the acid value is 16-40 mgKOH/g, and the acid value is even as high as 50-60 mgKOH/g. In addition, the crude rice bran oil has dark color and large decoloring difficulty, and is very difficult to process into national standard first-grade rice bran oil. Most of rice bran oil products in China are national standard four-grade oil, the selling price is generally low, the adopted processing technology is physical refining, the refining consumption is about 1.2 times of the acid value, and the profit margin is limited.

The ferulic acid methyl ester is used as a novel daily chemical raw material, is mainly used as a whitening agent and a sun-screening agent, has already been approved by the FDA in the United states in safety, and has already been applied to some international known brands. The method is reported in literature that methanol and ferulic acid are used as raw materials, strong acid cation exchange resin is used as a catalyst, and methyl ferulate is directly synthesized by esterification; but the large-scale industrial production is not yet known.

The raw materials for industrially producing the phytosterol mainly comprise deodorized distillate of vegetable oil, vegetable oil asphalt, tall oil asphalt and tall oil. Currently, around 70% or more of the commercial phytosterols are derived from deodorizer distillates internationally. The current common methods are as follows: organic solvent extraction, chemical method, adsorption method, enzymatic method and supercritical CO ₂ Extraction methods, and the like.

Common organic solvents used for extracting phytosterols include chloroform-methanol, chloroform-methanol-water, n-hexane, dichloromethane, acetone, and the like. The organic solvent is used for extracting the phytosterol, and the method has the advantages of no need of special instruments, is the most common, simple and easy-to-implement extraction method, and can be operated in common laboratories. The disadvantages are large solvent consumption, high toxicity of part of the extractant and poor safety.

The adsorption method is a method for separating the phytosterol according to the selectivity difference of the adsorbent to different components, the purity of the extracted phytosterol is high, but the elution time is too long, and the solvent consumption is large.

The chemical method mainly utilizes chemical reaction to prepare various derivatives of the sterol, increases physical differences of various sterols, and then adopts a physical separation method, including a complexation method, a saponification method and the like. The complexation method utilizes the complexation of sterol and organic acid, halogen alkaline earth metal salt, etc. to make the solubility of sterol produce large difference after complexation so as to attain the effect of separation and extraction. The phytosterol obtained by the method has high purity and recovery rate, but the solvent is difficult to recover, and the production cost is high. The saponification method is to hydrolyze ester under the action of alkali to generate carboxylate and alcohol, and then obtain the organic substance to be extracted, but the method has low utilization rate of raw materials, and low purity and yield of products.

The enzyme method is a method for improving the purity and recovery rate of the phytosterol by catalyzing the esterification process by using enzyme, but the enzyme has high price and short service life.

Supercritical CO ₂ The extraction method is to select the operation conditions, separate and purify the phytosterol remained in an extractor after the fatty acid and triglyceride with higher solubility are extracted, or directly use the prepared phytosterol product to enter the separation system for separation, but the equipment is complex and the cost is high.

At present, the main raw materials for preparing the biodiesel in China are various waste animal and vegetable oil and byproducts in the oil refining process, such as kitchen waste oil, illegal cooking oil, frying waste oil, acidified oil, fatty acid deodorized distillate and the like.

The production method of biodiesel currently adopts an acid or base catalysis method. The used acidic catalyst is usually sulfuric acid, phosphoric acid, hydrochloric acid, organic sulfonic acid and the like, wherein concentrated sulfuric acid is the most commonly used acidic catalyst due to low price and rich resources; the basic catalysts used are preferably NaOH, KOH and sodium methoxide.

The liquid base catalysis method has the characteristics of low reaction temperature, high speed, high yield, small corrosion to equipment and the like, but because the liquid base catalysis method can perform saponification reaction with free fatty acid in the raw oil, the existence of soap can cause the emulsification of reaction products, and the subsequent separation is difficult, so the requirements on the acid value and the water content of the raw oil are strict. The liquid acid catalysis method has lower requirements on raw materials, but has low reaction yield and serious corrosion on equipment.

For the reasons, in the industrial production of biodiesel, an acid catalyst is generally adopted, and in the selection of equipment, an enamel reaction kettle is generally adopted as a core device for esterification or transesterification, and conventional tower-type or kettle-type reduced pressure distillation is adopted to produce refined biodiesel. The temperature of conventional tower type reduced pressure distillation is 220-230 ℃, reflux ratio is required to be balanced in the reduced pressure distillation process, entrainment phenomenon is difficult to avoid, and indexes of three items of acid value, free glycerin and total glycerin of a product exceed standards; in the long-time distillation process, polymerization reaction can occur between carbon-carbon double bonds of unsaturated fatty acid in the crude methyl ester, so that the plant asphalt is generated, and the product yield is greatly reduced. In the production process, after the esterification or ester exchange reaction is finished, the acid or alkaline catalyst needs to be neutralized, and the acid or alkaline catalyst needs to be washed by water to remove the neutralized product, so that a large amount of industrial wastewater is inevitably generated, and the cost of wastewater treatment is increased for enterprises.

In addition, the biodiesel industrially produced at present is a mixture of fatty acid methyl esters with different carbon numbers, and the product can only be sold as biodiesel, so that the additional value is generally not high.

Disclosure of Invention

The invention aims to provide a co-production system and a co-production process of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, which are used for realizing deep processing of rice bran oil and improving the additional value of products.

In order to achieve the purpose, the invention provides the following scheme:

the invention discloses a co-production system of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, which comprises the following components:

the fatty acid extraction system comprises a first distillation unit, wherein the first distillation unit is used for distilling and separating the degummed dried rice bran raw oil to obtain a first light component substance and a first heavy component substance; the first light component material comprises fatty acid, and the first heavy component material comprises deacidified rice bran oil;

the alcoholysis system comprises an alcoholysis unit, a second separation unit and a second drying unit which are sequentially connected, wherein the alcoholysis unit is connected with the first distillation unit and is used for carrying out alcoholysis reaction on the first heavy component substances, the second separation unit is used for centrifugally separating products of the alcoholysis reaction to obtain crude biodiesel and byproducts, and the second drying unit is used for removing methanol from the crude biodiesel to obtain methanol-removed crude biodiesel;

the methyl ferulate extraction system comprises a second distillation unit, the second distillation unit is connected with the second drying unit and is used for distilling and separating the methanol-removed crude biodiesel to obtain a second light component substance and a second heavy component substance; the second light component material comprises ferulic acid methyl ester, and the second heavy component material comprises crude biodiesel;

a fatty acid methyl ester extraction system, wherein the fatty acid methyl ester extraction system comprises a third distillation unit, and the third distillation unit is connected with the second distillation unit and is used for distilling and separating the second heavy component substance to obtain a third light component substance and a third heavy component substance; the third light component material comprises fatty acid methyl ester, and the third light component material comprises crude phytosterol;

the plant sterol extraction system comprises a fourth distillation unit, the fourth distillation unit is connected with the third distillation unit and is used for distilling and separating the third heavy component substance to obtain a fourth light component substance and a fourth heavy component substance; the fourth light component material comprises phytosterol, and the fourth heavy component material comprises rice bran wax.

Preferably, the method further comprises a pretreatment system for treating the rice bran raw oil to obtain the degummed and dried rice bran raw oil; the pretreatment system comprises an impurity removal unit, a degumming unit, a first separation unit and a first drying unit which are sequentially connected; the impurity removal unit is used for receiving the rice bran raw oil and filtering impurities in the rice bran raw oil; the degumming unit is used for refining and degumming the rice bran raw oil after impurity removal so as to separate colloid; the first separation unit is used for carrying out centrifugal separation on the product obtained by the degumming unit to obtain degummed rice bran raw oil and the colloid; the first drying unit is used for drying the degummed rice bran raw oil to obtain degummed dried rice bran raw oil; and the first drying unit is connected with the first distillation unit so as to convey the obtained degummed dried rice bran raw oil to the first distillation unit.

Preferably, the impurity removal unit comprises a sixth heat exchanger, a filter and a first temporary storage tank which are connected in sequence; an inlet of the sixth heat exchanger is used for receiving the raw rice bran oil, and an outlet of the sixth heat exchanger is connected with an inlet of the filter; an outlet of the filter is connected with an inlet of the first temporary storage tank so as to temporarily store the filtered rice bran raw oil in the first temporary storage tank;

the degumming unit comprises an acid quantitative pump and an oil refining kettle; an inlet of the oil refining kettle is connected with an outlet of the first temporary storage tank so as to receive the filtered rice bran raw oil; the acid quantitative pump is connected with the oil refining pot so as to pump acidic auxiliary materials required by the degumming reaction of the rice bran raw oil into the oil refining pot;

the first separation unit comprises a seventh heat exchanger, a first centrifugal machine and a second temporary storage tank; an inlet of the seventh heat exchanger is connected with an outlet of the oil refining kettle to receive refined degumming products of the oil refining kettle; an inlet of the first centrifuge is connected with an outlet of the seventh heat exchanger so as to centrifugally separate the refined degumming product to obtain the degummed rice bran raw oil and the colloid; an inlet of the second temporary storage tank is connected with an outlet of the first centrifuge so as to temporarily store the degummed rice bran raw oil;

the first drying unit comprises an eighth heat exchanger, a first dryer and a first vacuum pump, wherein an inlet of the eighth heat exchanger is connected with an outlet of the second temporary storage tank so as to receive the degummed rice bran raw oil; an inlet of the first dryer is connected with an outlet of the eighth heat exchanger to dry the degummed rice bran raw oil to obtain the degummed dried rice bran raw oil; and the inlet of the first vacuum pump is connected with the outlet of the first dryer so as to pump the degummed dried rice bran raw oil to the outlet of the first dryer.

Preferably, the system further comprises a first refining system, wherein the first refining system comprises a fifth distillation unit, and the fifth distillation unit is connected with the third distillation unit to distill and separate the third light component substances into fifth light component substances and fifth heavy component substances; the fifth light component substance comprises a mixture of methyl palmitate, methyl oleate and methyl linoleate, and the fifth heavy component substance comprises methyl stearate.

Preferably, the system further comprises a second refining system, wherein the second refining system comprises a sixth distillation unit, and the sixth distillation unit is connected with the fifth distillation unit to distill and separate the fifth light component substances into sixth light component substances and sixth heavy component substances; the sixth light component substance comprises methyl palmitate and the sixth heavy component substance comprises a mixture of methyl oleate and methyl linoleate.

Preferably, the fifth distillation unit comprises a fourth heat exchanger, a fifth short-path distiller, a fifth heavy component tank, a fifth light component tank, a ninth cold trap, a tenth cold trap and a seventh vacuum pump; an inlet of the fourth heat exchanger is used for receiving the third light component substances, and an outlet of the fourth heat exchanger is connected with an inlet of the fifth short-path distiller; a heavy component outlet of the fifth short-path distiller is connected with the fifth heavy component tank to inject the fifth heavy component substance into the fifth heavy component tank; a light component outlet of the fifth short path distiller is connected to the fifth light component tank to inject the fifth light component material into the fifth light component tank; a vacuumizing port of the fifth short-path distiller is connected with the ninth cold trap, the tenth cold trap and the seventh vacuum pump in series so as to vacuumize the fifth short-path distiller through the seventh vacuum pump, and the condensable gas component from the fifth short-path distiller is collected through the ninth cold trap and the tenth cold trap; and/or

The sixth distillation unit comprises a fifth heat exchanger, a sixth short-path distiller, a sixth heavy component tank, a sixth light component tank, an eleventh cold trap, a twelfth cold trap and an eighth vacuum pump; an inlet of the fifth heat exchanger is used for receiving the fifth light component substances, and an outlet of the fifth heat exchanger is connected with an inlet of the sixth short-path distiller; a heavies outlet of the sixth short path distiller is connected to the sixth heavies tank for injection of the sixth heavies species into the sixth heavies tank; a lights outlet of the sixth short path distiller is connected to the sixth lights tank to inject the sixth lights into the sixth lights tank; and a vacuumizing port of the sixth short-path distiller is connected with the eleventh cold trap, the twelfth cold trap and the eighth vacuum pump in series, so that the sixth short-path distiller is vacuumized by the eighth vacuum pump, and condensable gas components from the sixth short-path distiller are collected by the eleventh cold trap and the twelfth cold trap.

Preferably, the first distillation unit comprises a ninth heat exchanger, a first short-path distiller, a first heavy component tank, a first light component tank, a first cold trap, a second cold trap and a second vacuum pump; an inlet of the ninth heat exchanger is used for receiving the degummed dried rice bran raw oil, and an outlet of the ninth heat exchanger is connected with an inlet of the first short-path distiller; a heavies outlet of the first short path distiller is connected to the first heavies tank for injection of the first heavies material into the first heavies tank; a light component outlet of the first short path distiller is connected to the first light component tank to inject the first light component material into the first light component tank; the vacuumizing port of the first short-path distiller is connected with the first cold trap, the second cold trap and the second vacuum pump in series, so that the first short-path distiller is vacuumized through the second vacuum pump, and condensable gas components from the first short-path distiller are collected through the first cold trap and the second cold trap; and/or

The second distillation unit comprises a first heat exchanger, a second short-range distiller, a second heavy component tank, a second light component tank, a third cold trap, a fourth cold trap and a fourth vacuum pump; the inlet of the first heat exchanger is used for receiving the methanol-removed crude biodiesel, and the outlet of the first heat exchanger is connected with the inlet of the second short-path distiller; the heavy component outlet of the second short-path distiller is connected with the second heavy component tank so as to inject the second heavy component material into the second heavy component tank; a light component outlet of the second short path distiller is connected with the second light component tank to inject the second light component material into the second light component tank; the vacuum pumping port of the second short path distiller is sequentially connected with the third cold trap, the fourth cold trap and the fourth vacuum pump in series, so that the second short path distiller is vacuumized by the fourth vacuum pump, and condensable gas components from the second short path distiller are collected by the third cold trap and the fourth cold trap; and/or

The third distillation unit comprises a second heat exchanger, a third short-range distiller, a third heavy component tank, a third light component tank, a fifth cold trap, a sixth cold trap and a fifth vacuum pump; the inlet of the second heat exchanger is used for receiving the second heavy component material, and the outlet of the second heat exchanger is connected with the inlet of the third short-path distiller; the heavies outlet of the third short path distiller is connected to the third heavies tank to inject the third heavy components into the third heavies tank; a light component outlet of the third short path distiller is connected to the third light component tank to inject the third light component material into the third light component tank; a vacuumizing port of the third short-path distiller is sequentially connected with the fifth cold trap, the sixth cold trap and the fifth vacuum pump in series, so that the third short-path distiller is vacuumized by the fifth vacuum pump, and condensable gas components from the third short-path distiller are collected by the fifth cold trap and the sixth cold trap; and/or

The fourth distillation unit comprises a third heat exchanger, a fourth short-range distiller, a fourth heavy component tank, a fourth light component tank, a seventh cold trap, an eighth cold trap and a sixth vacuum pump; the inlet of the third heat exchanger is used for receiving the third heavy component substance, and the outlet of the third heat exchanger is connected with the inlet of the fourth short-path distiller; the heavies outlet of the fourth short path distiller is connected to the fourth heavies tank to inject the fourth heavies material into the fourth heavies tank; a light component outlet of the fourth short path distiller is connected to the fourth light component tank to inject the fourth light component material into the fourth light component tank; and a vacuumizing port of the fourth short-range distiller is sequentially connected with the seventh cold trap, the eighth cold trap and the sixth vacuum pump in series, so that the fourth short-range distiller is vacuumized by the sixth vacuum pump, and condensable gas components from the fourth short-range distiller are trapped by the seventh cold trap and the eighth cold trap.

Preferably, the alcoholysis unit comprises a methanol quantitative pump, an alcoholysis kettle, a first condenser, a catalyst adding port and an auxiliary material adding port; an inlet of the alcoholysis tank is connected to the first distillation unit to receive the first heavy ends; the methanol quantitative pump is connected with the alcoholysis kettle to pump methanol into the alcoholysis kettle; the first condenser is connected with the alcoholysis kettle to condense the gas discharged from the alcoholysis kettle; the catalyst adding port is connected with the alcoholysis kettle so as to add a catalyst required by alcoholysis reaction into the alcoholysis kettle; the auxiliary material adding port is connected with the alcoholysis kettle so as to add auxiliary materials required by alcoholysis reaction into the alcoholysis kettle;

the second separation unit comprises a tenth heat exchanger, a second centrifuge, a third temporary storage tank, a methanol recovery kettle, a second condenser, a catcher and a ninth vacuum pump; an inlet of the tenth heat exchanger is connected with an outlet of the alcoholysis kettle to receive the crude biodiesel and byproducts obtained by the alcoholysis reaction; the inlet of the second centrifuge is connected with the outlet of the tenth heat exchanger so as to centrifugally separate the crude biodiesel from the byproducts; the inlet of the third temporary storage tank is connected with the outlet of the second centrifuge so as to temporarily store the crude biodiesel; the methanol recovery kettle is connected with an outlet of the third temporary storage tank to receive the crude biodiesel; the second condenser is connected with the methanol recovery kettle so as to condense the gas discharged by the methanol recovery kettle; the catcher is connected with the second condenser to catch the condensable gas components from the methanol recovery kettle; the ninth vacuum pump is connected with the catcher to pump out the gas in the methanol recovery kettle;

the second drying unit comprises an eleventh heat exchanger, a second dryer and a third vacuum pump, wherein an inlet of the eleventh heat exchanger is connected with an outlet of the methanol recovery kettle so as to receive the crude biodiesel from which methanol is removed; an inlet of the second dryer is connected with an outlet of the eleventh heat exchanger so as to perform methanol removal treatment on the crude biodiesel to obtain methanol-removed crude biodiesel; the inlet of the third vacuum pump is connected with the outlet of the second dryer to pump the demethanized crude biodiesel to the outlet of the second dryer.

The invention also discloses a co-production process of the ferulic acid methyl ester, the phytosterol, the fatty acid and the fatty acid methyl ester, which comprises the following steps:

s1, distilling and separating the degummed dry rice bran raw oil at 50-300 Pa and 170-210 ℃ to obtain a first light component substance and a first heavy component substance, wherein the first light component substance comprises fatty acid, and the first heavy component substance comprises deacidified rice bran oil;

s2, carrying out alcoholysis reaction on the first heavy component substance, carrying out centrifugal separation on a product of the alcoholysis reaction to obtain crude biodiesel and a byproduct, and carrying out methanol removal on the crude biodiesel at the conditions of 50-300 Pa and 30-70 ℃ to obtain methanol-removed crude biodiesel;

s3, distilling and separating the methanol-removed crude biodiesel at the temperature of 120-160 ℃ under the pressure of 0-100 Pa to obtain a second light component substance and a second heavy component substance, wherein the second light component substance comprises methyl ferulate, and the second heavy component substance comprises crude biodiesel;

s4, distilling and separating the second heavy component substance at the temperature of 150-180 ℃ under the pressure of 0-50 Pa to obtain a third light component substance and a third heavy component substance, wherein the third light component substance comprises fatty acid methyl ester, and the third heavy component substance comprises crude phytosterol;

s5, distilling and separating the third heavy component substance at the temperature of 190-220 ℃ under the condition of 0-30 Pa to obtain a fourth light component substance and a fourth heavy component substance; the fourth light component material comprises phytosterol and the fourth heavy component material comprises rice bran wax.

Preferably, before step S1, a preprocessing step is further included, where the preprocessing step includes: filtering impurities in the raw rice bran oil; refining and degumming the rice bran raw oil after impurity removal to separate colloid; performing centrifugal separation on the refined degumming product to obtain degummed rice bran raw oil and the colloid; drying the degummed rice bran raw oil at the temperature of 80-120 ℃ under the pressure of 0-300 Pa to obtain degummed dried rice bran raw oil;

a refining step is also included after step S4, the refining step including: distilling and separating the third light component substance at the temperature of 160-170 ℃ under the condition of 0-50 Pa to obtain a fifth light component substance and a fifth heavy component substance; distilling and separating the fifth light component substance at the temperature of 150-165 ℃ under the pressure of 0-50 Pa to obtain a sixth light component substance and a sixth heavy component substance; the fifth light component substance comprises a mixture of methyl palmitate, methyl oleate and methyl linoleate, and the fifth heavy component substance comprises methyl stearate; the sixth light component substance comprises methyl palmitate and the sixth heavy component substance comprises a mixture of methyl oleate and methyl linoleate.

Compared with the prior art, the invention has the following technical effects:

1. the value of the rice bran oil is obviously improved, and benefits are created for enterprises.

(1) The co-production system can co-produce ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, and has various product types and high added value.

(2) According to the preferred scheme, the methyl palmitate, the methyl oleate, the methyl linoleate and the methyl stearate can be accurately separated from the mixed fatty acid methyl ester in a mode of refining the intermediate product, and the enterprise benefit is remarkably improved.

2. The biodiesel has better quality and higher yield.

(1) Can effectively avoid entrainment in the purification and refining process of the biodiesel, thereby ensuring that a plurality of indexes of 'acid value, soap content, free glycerin and total glycerin' meet the BD100 requirement.

(2) The preferred scheme of the invention adopts a short-path distillation mode, can effectively prevent the polymerization of materials and avoid the generation of plant asphalt, thereby improving the product yield.

3. The production energy consumption is reduced, and the production cost is saved.

The preferred scheme of the invention adopts a short-path distillation mode, and the temperature of the short-path distillation is lower under the condition of the same vacuum degree. For example, when fatty acid methyl ester is extracted, the temperature of short-path distillation is 160-170 ℃ at most, the separation temperature is lower than that of conventional tower type reduced pressure distillation, and the distillation separation time is shorter (generally about ten seconds).

4. Is environment-friendly.

(1) The preferred scheme of the invention adopts a short-path distillation mode, and the short-path distillation does not need direct steam, thereby avoiding water pollution and atmospheric pollution.

(2) The whole set of co-production equipment and the co-production process have no wastewater discharge and are environment-friendly.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required in the embodiments will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without creative efforts.

FIG. 1 is a schematic structural diagram of a main body part of a fatty acid extraction system;

FIG. 2 is a schematic structural view of a main portion of an alcoholysis system;

FIG. 3 is a schematic view of the main part of the extraction system for methyl ferulate;

FIG. 4 is a schematic structural view of a main part of a fatty acid methyl ester extraction system;

FIG. 5 is a schematic view of the main part of the phytosterol extraction system;

FIG. 6 is a schematic structural view of a main body part of the first refining system;

FIG. 7 is a schematic structural view of a main part of a second refining system;

FIG. 8 is a schematic structural view of a main body part of the pretreatment system;

description of the reference numerals:

the reference numerals are described in detail in table 1.

TABLE 1 description of reference numerals

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.

In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in further detail below.

Referring to fig. 1 to 5, the present embodiment provides a co-production system of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester (hereinafter referred to as co-production system), which includes a fatty acid extraction system 100, an alcoholysis system 200, a ferulic acid methyl ester extraction system 300, a fatty acid methyl ester extraction system 400 and a phytosterol extraction system 500.

The fatty acid extraction system 100 comprises a first distillation unit, and the first distillation unit is used for distilling and separating degummed dried rice bran raw oil to obtain a first light component substance and a first heavy component substance. The first light component material comprises fatty acid, and the first heavy component material comprises deacidified rice bran oil. The acid value of the crude rice bran oil is generally higher, most of the crude rice bran oil is 16-40 mgKOH/g (accounting for about 8-20% of the weight of the rice bran oil), and the content of the crude rice bran oil is even as high as 50-60 mgKOH/g (accounting for about 25-30% of the weight of the rice bran oil). Therefore, the fatty acid extracted by the first distillation unit has high purity and can be directly sold as a chemical raw material. In addition, because the physical extraction method is adopted, the oil loss in the extraction process is very low, and compared with the conventional physical deacidification process in oil refining, the method can obviously reduce the energy consumption and the production cost and also improve the economic benefit of enterprises.

The alcoholysis system 200 comprises an alcoholysis unit, a second separation unit and a second drying unit which are sequentially connected, wherein the alcoholysis unit is connected with the first distillation unit and used for carrying out alcoholysis reaction on a first heavy component substance, the second separation unit is used for carrying out centrifugal separation on a product of the alcoholysis reaction to obtain crude biodiesel and a byproduct, and the second drying unit is used for removing methanol from the crude biodiesel to obtain methanol-removed crude biodiesel.

The ferulic acid methyl ester extraction system 300 comprises a second distillation unit, and the second distillation unit is connected with a second drying unit and is used for distilling and separating the methanol-removed crude biodiesel to obtain a second light component substance and a second heavy component substance. The second light component material comprises ferulic acid methyl ester, and the second heavy component material comprises crude biodiesel. The ferulic acid methyl ester has an anti-oxidation effect, can prevent or delay oxidative deterioration of food components, and is generally used in an amount of 0.0025-0.1%. In addition, the ferulic acid methyl ester also has whitening, anti-inflammatory and other effects, and can be used in skin cosmetics to make skin have silk texture.

The fatty acid methyl ester extraction system 400 includes a third distillation unit coupled to the second distillation unit for distilling the second heavy component to separate a third light component and a third heavy component. The third lights comprise fatty acid methyl esters and the third lights comprise crude phytosterols.

The phytosterol extraction system 500 comprises a fourth distillation unit, wherein the fourth distillation unit is connected with the third distillation unit and is used for distilling and separating the third heavy component substance to obtain a fourth light component substance and a fourth heavy component substance. The fourth light component material comprises phytosterol, and the fourth heavy component material comprises rice bran wax. The phytosterol can be divided into three main classes of 4-demethyl sterol, 4-monomethyl sterol and 4, 4-dimethyl sterol, mainly including sitosterol, campesterol and stigmasterol, and also including avenasterol, spinasterol, morinda citrifolia sterol, arundosterol, cycloartenol and 24-methylene cycloartenol. The vegetable oil generally contains sterol, the rice bran oil, the wheat germ oil and the corn germ oil have higher sterol content, and most oil products contain no methyl sterol which accounts for more than 70 percent of the total sterol. The sterol classification table is detailed in table 2.

TABLE 2 sterol Classification Table

The total phytosterol content of several common vegetable oils is shown in table 3.

TABLE 3 Total sterol content in common vegetable oils

Oil name	Sterol content (%)	Oil name	Sterol content(％)
				Soybean oil	0.15～0.38	Olive oil	0.11～0.31
Rapeseed oil	0.35～0.51	Sunflower seed oil	0.35～0.75
				Rice bran oil	0.75～1.80	Tea oil	0.10～0.60
Corn oil	0.58～1.50	Wheat germ oil	1.30～2.60
				Palm oil	0.03～0.26	Sesame oil	0.17～0.30

The structure of the phytosterol is similar to that of cholesterol, and the structural characteristics of the phytosterol can competitively prevent the cholesterol from being absorbed by small intestine and discharge the cholesterol out of the body, thereby having the effects of reducing the cholesterol level in blood and preventing cardiovascular diseases. A large number of domestic and foreign researches show that the supplement of phytosterol can obviously reduce the content of total cholesterol and low-density lipoprotein cholesterol in blood, and has an auxiliary treatment effect on hyperlipidemia. In 9 months of 2000, the united states Food and Drug Administration (FDA) has formally approved phytosterols and phytosterol esters for use as food supplements, and may use "health-beneficial" labels. In 11 months in 2007, the phytosterol is evaluated as a new resource food in China, and passes the new resource food certification under the national new regulations in 2010.

The phytosterol has good oxidation resistance, can be used as food additive, and also can be used as raw material of animal growth agent for promoting animal growth and promoting animal health.

In addition, the phytosterol has the physiological characteristics of strong skin permeability, sebum secretion promotion, moisturizing and softening maintenance, and the sterol has the function of a softening agent in cosmetics.

The phytosterol extracted from the rice bran raw oil by the fourth distillation unit has high purity and good color, can obviously improve the additional value of the rice bran raw oil, and increases the economic benefit of enterprises.

In conclusion, the co-production system takes rice bran oil as a raw material, and can extract ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, so that the additional value of the product is obviously improved.

Further, the co-production system of this embodiment further includes a pretreatment system 800 for processing the rice bran raw oil to obtain degummed dried rice bran raw oil, and the degummed dried rice bran raw oil obtained by the pretreatment system 800 is provided for the fatty acid extraction system 100 to use. The pretreatment system 800 comprises an impurity removal unit, a degumming unit, a first separation unit and a first drying unit which are connected in sequence. The impurity removal unit is used for receiving the rice bran raw oil and filtering impurities in the rice bran raw oil. The degumming unit is used for refining and degumming the impurity-removed rice bran raw oil to separate colloid. The first separation unit is used for carrying out centrifugal separation on the product obtained by the degumming unit to obtain the degummed rice bran raw oil and the colloid. The first drying unit is used for drying the degummed rice bran raw oil to obtain the degummed dried rice bran raw oil. The first drying unit is connected with the first distillation unit so as to convey the obtained degummed dried rice bran raw oil to the first distillation unit.

Specifically, referring to fig. 8, in this embodiment, the impurity removing unit includes a sixth heat exchanger HE06, a filter F01, and a first temporary storage tank TST01, which are connected in sequence. The inlet of the sixth heat exchanger HE06 is used for receiving the raw rice bran oil, and the outlet of the sixth heat exchanger HE06 is connected with the inlet of the filter F01. The outlet of the filter F01 is connected with the inlet of the first temporary storage tank TST01, so that the filtered rice bran raw oil is temporarily stored in the first temporary storage tank TST 01. The degumming unit comprises an acid quantitative pump PA01 and an oil refining kettle OR 01. The inlet of the oil refining kettle OR01 is connected with the outlet of the first temporary storage tank TST01 to receive the filtered rice bran raw oil. An acid quantitative pump PA01 is connected with the oil refining kettle OR01 to pump acidic auxiliary materials (oxalic acid aqueous solution, phosphoric acid, citric acid and the like) required by the degumming reaction of the rice bran raw oil into the oil refining kettle OR 01. The first separation unit comprises a seventh heat exchanger HE07, a first centrifuge CE01 and a second holding tank TST 02. The inlet of the seventh heat exchanger HE07 is connected to the outlet of the oil refinery OR01 to receive the refined degumming product of the oil refinery OR 01. An inlet of the first centrifuge CE01 is connected with an outlet of the seventh heat exchanger HE07 to centrifugally separate the refined and degummed product to obtain degummed raw rice bran oil and colloid (the colloid is mainly phospholipid and can be sold directly). The inlet of the second holding tank TST02 is connected to the outlet of the first centrifuge CE01 for temporary storage of the degummed rice bran feedstock. The first drying unit comprises an eighth heat exchanger HE08, a first dryer DR01 and a first vacuum pump VP01, wherein an inlet of the eighth heat exchanger HE08 is connected with an outlet of the second temporary storage tank TST02 so as to receive degummed rice bran raw oil. An inlet of the first dryer DR01 is connected with an outlet of the eighth heat exchanger HE08 to dry the degummed rice bran raw oil to obtain the degummed dried rice bran raw oil. An inlet of a first vacuum pump VP01 is connected to an outlet of the first dryer DR01 to pump the degummed dried rice bran feedstock towards an outlet of the first dryer DR 01.

Referring to fig. 8, when the pretreatment system 800 is used, the raw rice bran oil is pumped out by the first pump body P01, heated to an appropriate temperature by the sixth heat exchanger HE06, enters the filter F01, and enters the first temporary storage tank TST01 after being filtered. The raw rice bran oil in the first temporary storage tank TST01 is pumped into a refining kettle OR01 through a second pump body P02, and is subjected to degumming reaction in a refining kettle OR01 with acid pumped through an acid quantitative pump PA 01. The reacted materials are pumped out of an oil refining kettle OR01 through a third pump body P03, heated to a proper temperature through a seventh heat exchanger HE07 and then enter a first centrifuge CE01 for centrifugal separation, and the separated degummed rice bran raw oil enters a second temporary storage tank TST 02. The degummed rice bran raw oil is pumped out of the second temporary storage tank TST02 through a fourth pump body P04, and is heated to a proper temperature through an eighth heat exchanger HE08 and then enters a first dryer DR 01. Under the vacuum condition provided by a first vacuum pump VP01, water and small molecule volatile matters are removed, and the dried degummed rice bran raw oil is pumped into a fourth temporary storage tank TST04 through a fifth pump body P05.

In order to further improve the added value of the product, the co-production system of the present embodiment further includes a first refining system 600. The first refining system 600 includes a fifth distillation unit connected to the third distillation unit to distill and separate the third lights (i.e., fatty acid methyl esters) into a fifth lights and a fifth heavies. The fifth light component substance comprises a mixture of methyl palmitate, methyl oleate and methyl linoleate, and the fifth heavy component substance comprises methyl stearate.

Referring to fig. 6, in the present embodiment, the fifth distillation unit includes a fourth heat exchanger HE04, a fifth short path distiller SD05, a fifth heavy component tank RC05, a fifth light component tank LC05, a ninth cold trap CT09, a tenth cold trap CT10, and a seventh vacuum pump VP 07. An inlet of the fourth heat exchanger HE04 is for receiving the third light component, and an outlet of the fourth heat exchanger HE04 is connected to an inlet of the fifth short path distiller SD 05. The heavies outlet of the fifth short-path distiller SD05 is connected to a fifth heavies tank RC05 to inject a fifth heavies substance into the fifth heavies tank RC 05. The light component outlet of the fifth short path distiller SD05 is connected to a fifth light component tank LC05 to inject a fifth light component substance into a fifth light component tank LC 05. The vacuum pumping port of the fifth short-path distiller SD05 is connected in series with a ninth cold trap CT09, a tenth cold trap CT10 and a seventh vacuum pump VP07, so that the fifth short-path distiller SD05 is evacuated by the seventh vacuum pump VP07, and the condensable gas component from the fifth short-path distiller SD05 is trapped by the ninth cold trap CT09 and the tenth cold trap CT 10.

Referring to fig. 6, when the fifth distillation unit is used, the third light component substance is pumped into the fourth heat exchanger HE04 through the twenty-third pump body P23, and enters the fifth short-path distiller SD05 after being heated to a suitable temperature, and under the vacuum condition provided by the seventh vacuum pump VP07, the fifth light component substance and the fifth heavy component substance are obtained through differentiation. The fifth light component material flows into a fifth light component tank LC05 and is then pumped into a fourteenth temporary storage tank TST14 via a twenty-fourth pump body P24. The fifth component substance flows into a fifth component tank RC05, and then is pumped into a fifteenth temporary storage tank TST15 through a twenty-fifth pump body P25.

Referring to fig. 7, in order to further improve the added value of the product, the co-production system of the present embodiment further includes a second refining system 700. The second refining system 700 includes a sixth distillation unit connected to the fifth distillation unit to distill and separate the fifth light component materials into sixth light component materials and sixth heavy component materials. The sixth light component substance comprises methyl palmitate, and the sixth heavy component substance comprises a mixture of methyl oleate and methyl linoleate.

Referring to fig. 7, in the present embodiment, the sixth distillation unit includes a fifth heat exchanger HE05, a sixth short-path distiller SD06, a sixth heavy component tank RC06, a sixth light component tank LC06, an eleventh cold trap CT11, a twelfth cold trap CT12, and an eighth vacuum pump VP 08. The inlet of the fifth heat exchanger HE05 is used for receiving the fifth light component, and the outlet of the fifth heat exchanger HE05 is connected with the inlet of the sixth short path distiller SD 06. The heavies outlet of the sixth short-path distiller SD06 is connected to a sixth heavy components tank RC06 to inject a sixth heavy components stream into a sixth heavy components tank RC 06. A lights outlet of the sixth short path distiller SD06 is connected to a sixth lights tank LC06 to inject sixth lights into a sixth lights tank LC 06. The vacuum pumping port of sixth short-path distiller SD06 is connected in series with eleventh cold trap CT11, twelfth cold trap CT12 and eighth vacuum pump VP08, so that sixth short-path distiller SD06 is pumped by eighth vacuum pump VP08, and condensable gas components from sixth short-path distiller SD06 are trapped by eleventh cold trap CT11 and twelfth cold trap CT 12.

Referring to fig. 7, when the sixth distillation unit is used, the fifth light component substance is pumped out of the fourteenth temporary storage tank TST14 through the twenty-sixth pump body P26, is heated to an appropriate temperature by the fifth heat exchanger HE05, enters the sixth short-path distiller SD06, and is separated under a vacuum condition provided by the eighth vacuum pump VP08 to obtain the sixth light component substance and the sixth heavy component substance. The sixth light component material flows into a sixth light component tank LC06 and is then pumped into a sixteenth holding tank TST16 by a twenty-seventh pump body P27. The sixth heavy component material flows into a sixth heavy component tank RC06 and is then pumped via a twenty-eighth pump block P28 into a seventeenth holding tank TST 17.

Referring to fig. 1, in the present embodiment, the first distillation unit includes a ninth heat exchanger HE09, a first short path distiller SD01, a first heavy component tank RC01, a first light component tank LC01, a first cold trap CT01, a second cold trap CT02, and a second vacuum pump VP 02. An inlet of the ninth heat exchanger HE09 is used for receiving degummed dried rice bran raw oil, and an outlet of the ninth heat exchanger HE09 is connected with an inlet of the first short-path distiller SD 01. The heavies outlet of the first short path distiller SD01 is connected to a first heavies tank RC01 for injecting first heavies material into the first heavies tank RC 01. The lights outlet of the first short path distiller SD01 is connected to a first lights tank LC01 to inject a first lights into a first lights tank LC 01. The vacuum pumping port of first short-range distiller SD01 is connected in series with first cold trap CT01, second cold trap CT02 and second vacuum pump VP02, so that first short-range distiller SD01 is pumped vacuum by second vacuum pump VP02, and condensable gas components from first short-range distiller SD01 are trapped by first cold trap CT01 and second cold trap CT 02.

Referring to fig. 1, when the first distillation unit is used, the degummed dried rice bran raw oil is pumped out of the fourth temporary storage tank TST04 through the sixth pump body P06, is heated to a suitable temperature through the ninth heat exchanger HE09, enters the first short-path distiller SD01, and is separated to obtain a first light component substance and a first heavy component substance under a vacuum condition provided by the second vacuum pump VP 02. The first light component material flows into the first light component tank LC01 and is then pumped into the fifth holding tank TST05 via the seventh pump body P07. The first heavy component material flows into the first heavy component tank RC01 and is pumped into the sixth temporary storage tank TST06 by the eighth pump body P08 in preparation for entering the alcoholysis system 200.

Referring to fig. 3, in the present embodiment, the second distillation unit includes a first heat exchanger HE01, a second short path distiller SD02, a second heavy component tank RC02, a second light component tank LC02, a third cold trap CT03, a fourth cold trap CT04, and a fourth vacuum pump VP 04. The inlet of the first heat exchanger HE01 is used for receiving the demethanized crude biodiesel, and the outlet of the first heat exchanger HE01 is connected with the inlet of the second short path distiller SD 02. The heavies outlet of the second short path distiller SD02 is connected to a second heavies tank RC02 to inject a second heavies species into a second heavies tank RC 02. The light component outlet of the second short path distiller SD02 is connected to a second light component tank LC02 to inject a second light component substance into a second light component tank LC 02. The vacuumizing port of the second short-path distiller SD02 is sequentially connected with a third cold trap CT03, a fourth cold trap CT04 and a fourth vacuum pump VP04 in series, so that the second short-path distiller SD02 is vacuumized by a fourth vacuum pump VP04, and the condensable gas component from the second short-path distiller SD02 is trapped by the third cold trap CT03 and the fourth cold trap CT 04.

Referring to fig. 3, when the second distillation unit is used, the methanol-removed crude biodiesel is pumped into the first heat exchanger HE01 through the fourteenth pump body P14, is heated to a suitable temperature through the first heat exchanger HE01, enters the second short-path distiller SD02, and is separated to obtain a second light component substance and a second heavy component substance under a vacuum condition provided by the fourth vacuum pump VP 04. The second light component flows into the second light component tank LC02, and then is pumped into the eighth temporary storage tank TST08 through the fifteenth pump body P15. The second heavy component substance flows into the second heavy component tank RC02, and is then pumped into the ninth temporary storage tank TST09 via the sixteenth pump body P16.

Referring to fig. 4, in the present embodiment, the third distillation unit includes a second heat exchanger HE02, a third short path distiller SD03, a third heavy component tank RC03, a third light component tank LC03, a fifth cold trap CT05, a sixth cold trap CT06, and a fifth vacuum pump VP 05. The inlet of the second heat exchanger HE02 is used for receiving the second heavy component substance, and the outlet of the second heat exchanger HE02 is connected with the inlet of the third short-path distiller SD 03. The heavies outlet of the third short path distiller SD03 is connected to a third heavies tank RC03 to inject a third heavy components substance into the third heavies tank RC 03. The light component outlet of the third short path distiller SD03 is connected to a third light component tank LC03 to inject a third light component substance into a third light component tank LC 03. The vacuumizing port of the third short-range distiller SD03 is sequentially connected with a fifth cold trap CT05, a sixth cold trap CT06 and a fifth vacuum pump VP05 in series, so that the third short-range distiller SD03 is vacuumized by a fifth vacuum pump VP05, and the condensable gas component from the third short-range distiller SD03 is trapped by the fifth cold trap CT05 and the sixth cold trap CT 06.

Referring to fig. 4, when the third distillation unit is in use, the second heavy component substance is pumped out of the ninth temporary storage tank TST09 through the seventeenth pump body P17, is heated to a suitable temperature by the second heat exchanger HE02, enters the third short-path distiller SD03, and is separated under a vacuum condition provided by the fifth vacuum pump VP05 to obtain a third light component substance and a third heavy component substance. The third light component flows into the third light component tank LC03, and then is pumped into the tenth temporary storage tank TST10 through the eighteenth pump body P18. The third heavy component substance flows into the third heavy component tank RC03 and is pumped into the eleventh intermediate tank TST11 via the nineteenth pump body P19.

Referring to fig. 5, in the present embodiment, the fourth distillation unit includes a third heat exchanger HE03, a fourth short path distiller SD04, a fourth heavy component tank RC04, a fourth light component tank LC04, a seventh cold trap CT07, an eighth cold trap CT08, and a sixth vacuum pump VP 06. The inlet of the third heat exchanger HE03 is used for receiving the third heavy component substance, and the outlet of the third heat exchanger HE03 is connected with the inlet of the fourth short-path distiller SD 04. The heavies outlet of the fourth short-path distiller SD04 is connected to a fourth heavies tank RC04 to inject a fourth heavies content into a fourth heavies tank RC 04. The light component outlet of the fourth short path distiller SD04 is connected to a fourth light component tank LC04 to inject a fourth light component substance into a fourth light component tank LC 04. A vacuum pumping port of the fourth short-path distiller SD04 is sequentially connected with a seventh cold trap CT07, an eighth cold trap CT08 and a sixth vacuum pump VP06 in series, so that the fourth short-path distiller SD04 is vacuumized by a sixth vacuum pump VP06, and condensable gas components from the fourth short-path distiller SD04 are trapped by the seventh cold trap CT07 and the eighth cold trap CT 08.

Referring to fig. 5, when the fourth distillation unit is in use, the third heavy component substance is pumped out of the eleventh temporary storage tank TST11 through the twentieth pump body P20, is heated to an appropriate temperature through the third heat exchanger HE03, enters the fourth short-path distiller SD04, and is separated under the vacuum condition provided by the sixth vacuum pump VP06 to obtain a fourth light component substance and a fourth heavy component substance. The fourth light component material flows into a fourth light component tank LC04 and is pumped into a twelfth holding tank TST12 by a twenty-first pump body P21. The fourth heavy component flows into a fourth heavy component tank RC04 and is pumped via a twenty-second pump body P22 into a thirteenth buffer tank TST 13.

Referring to fig. 2, in this embodiment, the alcoholysis unit includes a methanol quantitative pump PM01, an alcoholysis kettle E01, a first condenser CO01, a catalyst addition port CA01, and an auxiliary material addition port a 01. The inlet of alcoholysis vessel E01 is connected to the first distillation unit to receive the first heavy ends material. Methanol dosing pump PM01 was connected to alcoholysis kettle E01 to pump methanol into alcoholysis kettle E01. First condenser CO01 was connected to alcoholysis vessel E01 to condense the gas exiting alcoholysis vessel E01. Catalyst addition port CA01 was connected to alcoholysis kettle E01 to add the catalyst needed for the alcoholysis reaction to alcoholysis kettle E01. The auxiliary material adding port A01 is connected with the alcoholysis kettle E01 so as to add auxiliary materials required by the alcoholysis reaction into the alcoholysis kettle E01.

The second separation unit comprises a tenth heat exchanger HE10, a second centrifuge CE02, a third temporary storage tank TST03, a methanol recovery tank MR01, a second condenser CO02, a trap CAT01, and a ninth vacuum pump VP 09. An inlet of the tenth heat exchanger HE10 is connected to an outlet of the alcoholysis vessel E01 to receive the crude biodiesel and by-products from the alcoholysis reaction. The inlet of the second centrifuge CE02 is connected to the outlet of the tenth heat exchanger HE10 to centrifuge the crude biodiesel from the by-products. The inlet of the third temporary holding tank TST03 is connected to the outlet of the second centrifuge CE02 for temporary storage of crude biodiesel. The methanol recovery kettle MR01 is connected to the outlet of the third temporary storage tank TST03 to receive the crude biodiesel. Second condenser CO02 was connected to methanol recovery still MR01 to condense the gas discharged from methanol recovery still MR 01. A trap CAT01 was connected to second condenser CO02 to trap condensable gas components from methanol recovery vessel MR 01. A ninth vacuum pump VP09 was connected to trap CAT01 to pump out the gases in methanol recovery tank MR 01.

The second drying unit comprises an eleventh heat exchanger HE11, a second dryer DR02 and a third vacuum pump VP03, wherein an inlet of the eleventh heat exchanger HE11 is connected with an outlet of the methanol recovery kettle MR01 so as to receive the crude biodiesel after methanol is removed. The inlet of the second drier DR02 is connected to the outlet of the eleventh heat exchanger HE11 to subject the crude biodiesel to a de-methanol treatment to obtain de-methanol crude biodiesel. The inlet of the third vacuum pump VP03 is connected to the outlet of the second dryer DR02 to pump the demethanised crude biodiesel towards the outlet of the second dryer DR 02.

Referring to fig. 2, when the alcoholysis unit is used, the first heavy component in the sixth temporary storage tank TST06 is pumped into the alcoholysis kettle E01 through the ninth pump body P09, and is mixed with the methanol pumped in the methanol quantitative pump PM01 in the alcoholysis kettle E01, and alcoholysis reaction occurs under the action of the catalyst added through the catalyst addition port CA 01. The reacted materials are pumped out of the alcoholysis kettle E01 through a tenth pump body P10, the temperature of the reacted materials is raised to a proper temperature through a tenth heat exchanger HE10, the reacted materials enter a second centrifuge CE02 for separation, the separated crude biodiesel enters a third temporary storage tank TST03, and byproducts are mainly glycerol and can be sold directly. The crude biodiesel in the third temporary storage tank TST03 is pumped into a methanol recovery kettle MR01 through an eleventh pump body P11, and under the vacuum condition provided by a ninth vacuum pump VP09, the gasified methanol is condensed by a second condenser CO02 and then turns into liquid, and flows into a methanol tank MT01 for further rectification treatment. After methanol recovery is finished, the crude biodiesel is pumped out of a methanol recovery kettle MR01 through a twelfth pump body P12, the temperature is raised to a proper temperature through an eleventh heat exchanger HE11, the crude biodiesel enters a second dryer DR02, moisture and small molecule volatile matters are removed under the vacuum condition provided by a third vacuum pump VP03, and the dried crude biodiesel is pumped into a seventh temporary storage tank TST07 through a thirteenth pump body P13.

First condenser CO01 is disposed on the top of alcoholysis kettle E01, and it serves to condense methanol vapor in the alcoholysis reaction process into liquid and reflux the liquid to the interior of alcoholysis kettle E01, thereby reducing methanol loss in the alcoholysis process.

The auxiliary material adding port A01 is arranged at the top of the alcoholysis kettle E01, so that the type and the quantity of auxiliary materials to be added can be flexibly controlled according to the properties of materials and different reaction processes, and the effect of alcoholysis reaction and the performance of biodiesel products are ensured.

The trap CAT01 is arranged between the ninth vacuum pump VP09 and the second condenser CO02, and can effectively trap methanol steam which is not condensed by the second condenser CO02, thereby ensuring the vacuum degree of the system.

In this example, a distillation unit is used in many places. It will be appreciated by those skilled in the art that there are many types of distillation units, as long as the distillation function is achieved. Because the short-path distillation can prevent the polymerization of materials, avoid the generation of plant asphalt, and simultaneously can reduce the energy consumption, the embodiment adopts the mode of short-path distillation.

Referring to fig. 1 to 5, this embodiment further provides a co-production process of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, which includes the following steps:

s1, distilling and separating the degummed dried rice bran raw oil at the temperature of 170-210 ℃ under the pressure of 50-300 Pa to obtain a first light component substance and a first heavy component substance, wherein the first light component substance comprises fatty acid.

S2, carrying out alcoholysis reaction on the first heavy component substance, centrifugally separating the product of the alcoholysis reaction to obtain crude biodiesel and a byproduct, and removing methanol from the crude biodiesel at the temperature of 30-70 ℃ under the pressure of 50-300 Pa to obtain the methanol-removed crude biodiesel.

S3, distilling and separating the methanol-removed crude biodiesel under the conditions of 0-100 Pa and 120-160 ℃ to obtain a second light component substance and a second heavy component substance, wherein the second light component substance comprises ferulic acid methyl ester.

S4, distilling and separating the second heavy component substance at the temperature of 150-180 ℃ under the pressure of 0-50 Pa to obtain a third light component substance and a third heavy component substance, wherein the third light component substance comprises fatty acid methyl ester.

S5, distilling and separating the third heavy component substance at 0-30 Pa and 190-220 ℃ to obtain a fourth light component substance and a fourth heavy component substance. The fourth light component material comprises phytosterols.

Referring to fig. 8, as a preferred embodiment, a preprocessing step is further included before step S1, and the preprocessing step includes: filtering impurities in the rice bran raw oil. Refining and degumming the impurity-removed rice bran raw oil to separate colloid. And (4) carrying out centrifugal separation on the refined and degummed product to obtain degummed rice bran raw oil and colloid. Drying the degummed rice bran raw oil at the temperature of 80-120 ℃ under the pressure of 0-300 Pa to obtain the degummed dried rice bran raw oil.

Referring to fig. 6 to 7, as a preferred embodiment, a refining step is further included after step S4, and the refining step includes: and distilling and separating the third light component substance at the temperature of 160-170 ℃ under the condition of 0-50 Pa to obtain a fifth light component substance and a fifth heavy component substance. Distilling and separating the fifth light component substance at the temperature of 150-165 ℃ under the condition of 0-50 Pa to obtain a sixth light component substance and a sixth heavy component substance.

The principle and the implementation mode of the present invention are explained by applying specific examples in the present specification, and the above descriptions of the examples are only used to help understanding the method and the core idea of the present invention; meanwhile, for a person skilled in the art, according to the idea of the present invention, the specific embodiments and the application range may be changed. In view of the above, the present disclosure should not be construed as limiting the invention.

Claims

1. A system for co-production of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, comprising:

a fatty acid methyl ester extraction system, wherein the fatty acid methyl ester extraction system comprises a third distillation unit, and the third distillation unit is connected with the second distillation unit and is used for distilling and separating the second heavy component substance to obtain a third light component substance and a third heavy component substance; the third lights comprise fatty acid methyl esters and the third lights comprise crude phytosterols;

the plant sterol extraction system comprises a fourth distillation unit, the fourth distillation unit is connected with the third distillation unit and is used for distilling and separating the third heavy component substance to obtain a fourth light component substance and a fourth heavy component substance; the fourth light component material comprises phytosterol and the fourth heavy component material comprises rice bran wax.

2. The co-production system of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester of claim 1, further comprising a pre-treatment system for processing the rice bran raw oil to obtain degummed dry rice bran raw oil; the pretreatment system comprises an impurity removal unit, a degumming unit, a first separation unit and a first drying unit which are sequentially connected; the impurity removal unit is used for receiving the rice bran raw oil and filtering impurities in the rice bran raw oil; the degumming unit is used for refining and degumming the impurity-removed rice bran raw oil to separate colloid; the first separation unit is used for carrying out centrifugal separation on the product obtained by the degumming unit to obtain degummed rice bran raw oil and the colloid; the first drying unit is used for drying the degummed rice bran raw oil to obtain degummed dried rice bran raw oil; and the first drying unit is connected with the first distillation unit so as to convey the obtained degummed dried rice bran raw oil to the first distillation unit.

3. The co-production system of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester of claim 2, wherein the impurity removal unit comprises a sixth heat exchanger, a filter and a first temporary storage tank which are connected in sequence; an inlet of the sixth heat exchanger is used for receiving the raw rice bran oil, and an outlet of the sixth heat exchanger is connected with an inlet of the filter; the outlet of the filter is connected with the inlet of the first temporary storage tank so as to temporarily store the filtered rice bran raw oil in the first temporary storage tank;

4. The system for co-producing ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, according to claim 1, further comprising a first refining system, wherein the first refining system comprises a fifth distillation unit, and the fifth distillation unit is connected with the third distillation unit to distill and separate the third light component substance into a fifth light component substance and a fifth heavy component substance; the fifth light component substance comprises a mixture of methyl palmitate, methyl oleate and methyl linoleate, and the fifth heavy component substance comprises methyl stearate.

5. The system for co-producing ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester, which comprises a second refining system, wherein the second refining system comprises a sixth distillation unit, and the sixth distillation unit is connected with the fifth distillation unit to distill and separate the fifth light component substance into a sixth light component substance and a sixth heavy component substance; the sixth light component substance comprises methyl palmitate, and the sixth heavy component substance comprises a mixture of methyl oleate and methyl linoleate.

6. The system for co-producing ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester of claim 5, wherein, the fifth distillation unit comprises a fourth heat exchanger, a fifth short-path distiller, a fifth heavy component tank, a fifth light component tank, a ninth cold trap, a tenth cold trap and a seventh vacuum pump; an inlet of the fourth heat exchanger is used for receiving the third light component substances, and an outlet of the fourth heat exchanger is connected with an inlet of the fifth short-path distiller; a heavy component outlet of the fifth short-path distiller is connected with the fifth heavy component tank to inject the fifth heavy component substance into the fifth heavy component tank; a light component outlet of the fifth short path distiller is connected to the fifth light component tank to inject the fifth light component material into the fifth light component tank; a vacuumizing port of the fifth short-path distiller is connected with the ninth cold trap, the tenth cold trap and the seventh vacuum pump in series so as to vacuumize the fifth short-path distiller through the seventh vacuum pump, and the condensable gas component from the fifth short-path distiller is collected through the ninth cold trap and the tenth cold trap; and/or

The sixth distillation unit comprises a fifth heat exchanger, a sixth short-path distiller, a sixth heavy component tank, a sixth light component tank, an eleventh cold trap, a twelfth cold trap and an eighth vacuum pump; an inlet of the fifth heat exchanger is used for receiving the fifth light component substances, and an outlet of the fifth heat exchanger is connected with an inlet of the sixth short-path distiller; a heavies outlet of the sixth short path distiller is connected to the sixth heavies tank for injection of the sixth heavies species into the sixth heavies tank; a light component outlet of the sixth short path distiller is connected to the sixth light component tank to inject the sixth light component material into the sixth light component tank; and a vacuumizing port of the sixth short-path distiller is connected with the eleventh cold trap, the twelfth cold trap and the eighth vacuum pump in series, so that the sixth short-path distiller is vacuumized by the eighth vacuum pump, and condensable gas components from the sixth short-path distiller are collected by the eleventh cold trap and the twelfth cold trap.

7. The system for co-producing ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester of claim 1, wherein the first distillation unit comprises a ninth heat exchanger, a first short-path distiller, a first heavy component tank, a first light component tank, a first cold trap, a second cold trap and a second vacuum pump; an inlet of the ninth heat exchanger is used for receiving the degummed dried rice bran raw oil, and an outlet of the ninth heat exchanger is connected with an inlet of the first short-path distiller; a heavies outlet of the first short path distiller is connected to the first heavies tank for injection of the first heavies material into the first heavies tank; a light component outlet of the first short path distiller is connected to the first light component tank to inject the first light component material into the first light component tank; the vacuumizing port of the first short-path distiller is connected with the first cold trap, the second cold trap and the second vacuum pump in series, so that the first short-path distiller is vacuumized through the second vacuum pump, and condensable gas components from the first short-path distiller are collected through the first cold trap and the second cold trap; and/or

The third distillation unit comprises a second heat exchanger, a third short-path distiller, a third heavy component tank, a third light component tank, a fifth cold trap, a sixth cold trap and a fifth vacuum pump; the inlet of the second heat exchanger is used for receiving the second heavy component material, and the outlet of the second heat exchanger is connected with the inlet of the third short-path distiller; the heavies outlet of the third short path distiller is connected to the third heavies tank to inject the third heavy components into the third heavies tank; a light component outlet of the third short path distiller is connected to the third light component tank to inject the third light component material into the third light component tank; a vacuumizing port of the third short-path distiller is sequentially connected with the fifth cold trap, the sixth cold trap and the fifth vacuum pump in series, so that the third short-path distiller is vacuumized through the fifth vacuum pump, and condensable gas components from the third short-path distiller are collected through the fifth cold trap and the sixth cold trap; and/or

The fourth distillation unit comprises a third heat exchanger, a fourth short-range distiller, a fourth heavy component tank, a fourth light component tank, a seventh cold trap, an eighth cold trap and a sixth vacuum pump; the inlet of the third heat exchanger is used for receiving the third heavy component substance, and the outlet of the third heat exchanger is connected with the inlet of the fourth short-path distiller; a heavies outlet of the fourth short path distiller is connected to the fourth heavies tank to inject the fourth heavies species into the fourth heavies tank; a light component outlet of the fourth short path distiller is connected to the fourth light component tank to inject the fourth light component material into the fourth light component tank; and a vacuumizing port of the fourth short-range distiller is sequentially connected with the seventh cold trap, the eighth cold trap and the sixth vacuum pump in series, so that the fourth short-range distiller is vacuumized by the sixth vacuum pump, and condensable gas components from the fourth short-range distiller are collected by the seventh cold trap and the eighth cold trap.

8. The co-production system of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester of claim 1, wherein, the alcoholysis unit comprises a methanol quantitative pump, an alcoholysis kettle, a first condenser, a catalyst addition port and an auxiliary material addition port; an inlet of the alcoholysis tank is connected to the first distillation unit to receive the first heavy ends; the methanol quantitative pump is connected with the alcoholysis kettle to pump methanol into the alcoholysis kettle; the first condenser is connected with the alcoholysis kettle so as to condense the gas discharged by the alcoholysis kettle; the catalyst adding port is connected with the alcoholysis kettle so as to add a catalyst required by alcoholysis reaction into the alcoholysis kettle; the auxiliary material adding port is connected with the alcoholysis kettle so as to add auxiliary materials required by alcoholysis reaction into the alcoholysis kettle;

the second drying unit comprises an eleventh heat exchanger, a second dryer and a third vacuum pump, wherein an inlet of the eleventh heat exchanger is connected with an outlet of the methanol recovery kettle so as to receive the crude biodiesel after methanol is removed; an inlet of the second dryer is connected with an outlet of the eleventh heat exchanger so as to perform methanol removal treatment on the crude biodiesel to obtain methanol-removed crude biodiesel; an inlet of the third vacuum pump is connected to an outlet of the second dryer to pump the demethanized biodiesel crude biodiesel to the outlet of the second dryer.

9. A co-production process of ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester is characterized by comprising the following steps:

s2, carrying out alcoholysis reaction on the first heavy component substance, carrying out centrifugal separation on a product of the alcoholysis reaction to obtain crude biodiesel and a byproduct, and carrying out methanol removal on the crude biodiesel under the conditions of 50-300 Pa and 30-70 ℃ to obtain methanol-removed crude biodiesel;

s3, distilling and separating the methanol-removed crude biodiesel under the conditions of 0-100 Pa and 120-160 ℃ to obtain a second light component substance and a second heavy component substance, wherein the second light component substance comprises ferulic acid methyl ester, and the second heavy component substance comprises crude biodiesel;

s5, distilling and separating the third heavy component substance at 0-30 Pa and 190-220 ℃ to obtain a fourth light component substance and a fourth heavy component substance; the fourth light component material comprises phytosterol and the fourth heavy component material comprises rice bran wax.

10. The process of co-producing ferulic acid methyl ester, phytosterol, fatty acid and fatty acid methyl ester of claim 9,

before step S1, a preprocessing step is further included, the preprocessing step including: filtering impurities in the raw rice bran oil; refining and degumming the rice bran raw oil after impurity removal to separate colloid; performing centrifugal separation on the refined degumming product to obtain degummed rice bran raw oil and the colloid; drying the degummed rice bran raw oil at the temperature of 80-120 ℃ under the pressure of 0-300 Pa to obtain degummed dried rice bran raw oil;