CN215799388U - Device for separating methyl oleate and methyl linoleate by using biodiesel - Google Patents
Device for separating methyl oleate and methyl linoleate by using biodiesel Download PDFInfo
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- CN215799388U CN215799388U CN202120619281.4U CN202120619281U CN215799388U CN 215799388 U CN215799388 U CN 215799388U CN 202120619281 U CN202120619281 U CN 202120619281U CN 215799388 U CN215799388 U CN 215799388U
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Abstract
The utility model discloses a device for separating methyl oleate and methyl linoleate from biodiesel, which comprises a biodiesel storage tank, an ethanol storage tank, a fractionation kettle, a filter, a methyl linoleate flash evaporation device and a methyl oleate flash evaporation device; the biodiesel storage tank is sequentially connected with the ethanol storage tank, the fractionation kettle and the filter; the filter is respectively connected with a methyl linoleate flash evaporation device and a methyl oleate flash evaporation device; the methyl oleate flash evaporation device comprises a methyl oleate flash evaporation heater, a vacuum methyl oleate flash evaporation tank and a methyl oleate storage tank; the filter is connected with the methyl oleate flash evaporation heater, the vacuum methyl oleate flash evaporation tank and the methyl oleate storage tank in sequence. According to the device, the methyl oleate device and the methyl linoleate device are arranged in the device, the methyl oleate and the methyl linoleate are separated from the biodiesel, waste residues and waste gases are not generated by adopting the device, the environment pollution is avoided, and the ethanol flashed off can be recycled, so that the raw materials are saved.
Description
Technical Field
The utility model relates to the technical field of oil refining, in particular to a device for separating methyl oleate and methyl linoleate from biodiesel.
Background
The biodiesel oil is fatty acid methyl ester or ethyl ester prepared by ester-converting vegetable oil (such as oleum Rapae, soybean oil, peanut oil, corn oil, cottonseed oil, etc.), animal oil (such as fish oil, lard, beef tallow, mutton fat, etc.), waste oil or microbial oil with methanol or ethanol. Biodiesel is a typical 'green energy source', and has the characteristics of good environmental protection performance, good engine starting performance, good fuel performance, wide raw material source, renewability and the like. The vigorous development of the biodiesel has important strategic significance on economic sustainable development, energy source replacement promotion, environmental pressure reduction and urban atmospheric pollution control.
The components of the biodiesel are complex, the biodiesel is basically composed of various fatty acid methyl esters, the condensation point of the saturated fatty acid methyl ester in the biodiesel is generally separated at 5-0 ℃, the condensation point and the cold filter plugging point of the biodiesel can be reduced, products with high added values can be obtained, and the economic benefit of the biodiesel industry chain is improved.
However, the prior chemical reaction method is adopted to separate the methyl oleate and the methyl linoleate, when the methyl oleate is obtained, the separation of the methyl linoleate can generate waste residues and waste gases to cause environmental pollution,
therefore, the problem to be solved by those skilled in the art is how to provide a simple preparation method, environment-friendly and pollution-free device for separating methyl oleate and methyl linoleate from biodiesel.
SUMMERY OF THE UTILITY MODEL
In view of the above, the utility model provides a device for separating methyl oleate and methyl linoleate from biodiesel, which is characterized by comprising a biodiesel storage tank, an ethanol storage tank, a fractionation kettle, a filter, a methyl linoleate flash evaporation device and a methyl oleate flash evaporation device;
the biodiesel storage tank is sequentially connected with the ethanol storage tank, the fractionation kettle and the filter; the filter is respectively connected with the methyl linoleate flash evaporation device and the methyl oleate flash evaporation device;
the methyl oleate flash evaporation device comprises a methyl oleate flash evaporation heater, a vacuum methyl oleate flash evaporation tank and a methyl oleate storage tank; the filter is sequentially connected with the methyl oleate flash evaporation heater, the vacuum methyl oleate flash tank and the methyl oleate storage tank.
The utility model has the following beneficial effects: according to the device, the methyl oleate device and the methyl linoleate device are arranged in the device, the methyl oleate and the methyl linoleate are separated from the biodiesel, waste residues and waste gases are not generated by adopting the device, the environment pollution is avoided, and the ethanol flashed off can be recycled, so that the raw materials are saved.
Preferably, the methyl linoleate flash evaporation device comprises a flash evaporation heater I, an atmospheric flash evaporation tank, a flash evaporation heater II, a vacuum flash evaporation tank and a methyl linoleate storage tank;
the filter is sequentially connected with the flash heater I, the normal-pressure flash tank, the flash heater II, the vacuum flash tank and the methyl linoleate storage tank.
Adopt above-mentioned technical scheme's beneficial effect: the vacuum flash evaporation and the normal-pressure flash evaporation are arranged, so that the purity of the methyl linoleate can be further improved, and the stable performance of the methyl linoleate can be ensured.
Preferably, the device also comprises a filtrate temporary storage tank, a methyl oleate temporary storage tank and a solid methyl oleate storage tank;
the filter is respectively connected with the filtrate temporary storage tank and the solid methyl oleate storage tank;
the solid methyl oleate storage tank is sequentially connected with the methyl oleate temporary storage tank and the methyl oleate flash evaporation heater;
the filtrate temporary storage tank is connected with the flash evaporation heater I.
Adopt above-mentioned technical scheme's beneficial effect: the purpose of setting up the jar of keeping in is to reach the effect of buffering, avoids the material too much and influences subsequent technology.
Preferably, the refrigerator also comprises a freezing chamber, and the filter is arranged in the freezing chamber.
Adopt above-mentioned technical scheme's beneficial effect: the purpose of the freezer compartment is to be able to ensure that the temperature is at a certain temperature.
Preferably, still include a plurality of circulating pumps, be equipped with the circulating pump between the fractionation cauldron with the filter, filtrate temporary storage tank with between the flash heater I, the vacuum flash tank with between the flash heater, flash heater II with between the ordinary pressure flash tank.
Adopt above-mentioned technical scheme's beneficial effect: the purpose of the circulation pump is to generate power to drive the material into the required equipment.
Application of methyl linoleate and methyl oleate:
1. used as plant-based synthetic lubricating oil raw material, surface active base material, leather and rubber softener, petroleum exploration non-fluorescent slurry lubricant, plastic plasticizer, water repellent agent, toughening agent of resin, and also used for organic synthesis.
2. It is used as detergent, emulsifier, wetting agent and stabilizer intermediate, and is widely used in various emulsified products, perfume solvent and lubricant for sprayed product.
The utility model separates the two to increase the applicability of the product.
According to the technical scheme, compared with the prior art, the utility model discloses and provides the device for separating the methyl oleate and the methyl linoleate from the biodiesel, the low condensation point of the biodiesel is utilized, the ethanol is used as a solvent for fractionation and separation, the environment is protected, the ethanol can be recycled, the separation of the methyl oleate and the methyl linoleate is realized by adopting a chemical reaction, and the environment is seriously polluted by waste residues and waste gases;
in the utility model, the methyl oleate and the methyl linoleate are separated by freezing and separating by using a solvent method, so that the products have wider application;
for the biodiesel industry, the industrial chain of biodiesel is extended, the separation of methyl oleate and methyl linoleate increases economic benefits, and the additional value of biodiesel products is increased.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic diagram of the structure of the methyl oleate and methyl linoleate provided by the utility model;
FIG. 2 is a schematic diagram of the structure of a methyl oleate plant and a methyl linoleate flash distillation plant provided by the utility model;
1-biodiesel storage tank, 2-fractionation kettle, 3-filter, 4-ethanol storage tank, 5-methyl linoleate flash evaporation device, 6-methyl oleate flash evaporation device, 7-circulating pump I, 8-circulating pump II, 9-circulating pump III, 10-circulating pump IV, 11-circulating pump V, 12-circulating pump VI, 13-freezing chamber and 14-ethanol recovery system.
51-a flash heater I, 52-an atmospheric flash tank, 53-a flash heater II, 54-a vacuum flash tank, 55-a methyl linoleate storage tank, 56-a filtrate temporary storage tank, 61-a methyl oleate flash heater, 62-a vacuum methyl oleate flash tank, 63-a methyl oleate storage tank, 64-a methyl oleate temporary storage tank and 65-a solid methyl oleate storage tank.
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 derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The embodiment of the utility model discloses a device for separating methyl oleate and methyl linoleate from biodiesel, which comprises a biodiesel storage tank 1, an ethanol storage tank 4, a fractionation kettle 2, a filter 3, a methyl linoleate flash evaporation device 65 and a methyl oleate flash evaporation device 6;
the biodiesel storage tank 1 is sequentially connected with an ethanol storage tank 4, a fractionation kettle 2 and a filter 3; the filter 3 is respectively connected with a methyl linoleate flash evaporation device 65 and a methyl oleate flash evaporation device 6;
the methyl oleate flash device 6 comprises a methyl oleate flash heater 61, a vacuum methyl oleate flash tank 62 and a methyl oleate storage tank 63; the filter 3 is connected with a methyl oleate flash heater 61, a vacuum methyl oleate flash tank 62 and a methyl oleate storage tank 63 in sequence.
According to the device, the methyl oleate device and the methyl linoleate device are arranged in the device, the methyl oleate and the methyl linoleate are separated from the biodiesel, waste residues and waste gases are not generated by adopting the device, the environment pollution is avoided, and the ethanol flashed off can be recycled, so that the raw materials are saved.
In one embodiment, methyl linoleate flash distillation apparatus 65 includes flash heater I, atmospheric flash tank 52, flash heater II, vacuum flash tank 54 and methyl linoleate storage tank 55; the filter 3 is sequentially connected with a flash heater I, an atmospheric flash tank 52, a flash heater II, a vacuum flash tank 54 and a methyl linoleate storage tank 6355. The vacuum flash evaporation and the normal-pressure flash evaporation are arranged, so that the purity of the methyl linoleate can be further improved, and the stable performance of the methyl linoleate can be ensured.
In one embodiment, a filtrate holding tank 56, a methyl oleate holding tank 64, and a solid methyl oleate holding tank 65; the filter 3 is respectively connected with the filtrate temporary storage tank 56 and the solid methyl oleate storage tank 65; the solid methyl oleate storage tank 65 is sequentially connected with a methyl oleate temporary storage tank 64 and a methyl oleate flash evaporation heater 61; the filtrate temporary storage tank 56 is connected with a flash heater I. The purpose of setting up the jar of keeping in is to reach the effect of buffering, avoids the material too much and influences subsequent technology.
In one embodiment, a freezing chamber is also included, and the filter 3 is installed in the freezing chamber. The purpose of the freezer compartment is to be able to ensure that the temperature is at a certain temperature.
In one embodiment, the system further comprises a plurality of circulating pumps, and the circulating pumps are arranged between the fractionation kettle 2 and the filter 3, between the filtrate temporary storage tank 56 and the flash heater I, between the vacuum flash tank 54 and the flash heater, and between the flash heater II and the normal-pressure flash tank 52. The purpose of the circulation pump is to generate power to drive the material into the required equipment.
The biodiesel is low-condensation-point biodiesel (fatty acid methyl ester), and the quality indexes are as follows: acid value is within 0.5mgKOH/g, no water and no impurity, about 50 percent of oleic acid methyl ester, about 47 percent of linoleic acid methyl ester and about 3 percent of other methyl ester.
The method for separating the methyl oleate and the methyl linoleate from the biodiesel by adopting the device comprises the following steps:
(1) pumping the biodiesel in the biodiesel storage tank 1 at the controlled temperature of (-10) DEG C into the fractionation kettle 2, starting a refrigerator and a cooling water pipe of the fractionation kettle 2, pumping the absolute ethanol solution in the ethanol storage tank 4 into the fractionation kettle 2, cooling at the speed of 2 ℃/h, controlling the stirring speed at 50-70 rpm, and cooling to (-15) DEG C; then continuously pumping chilled water into the fractionation kettle 2, cooling the chilled water through a coil pipe, controlling the stirring speed at 30 rpm according to the temperature of 0.1 ℃/h, keeping the temperature at (-22) DEG C, and standing the mixture for 8h to obtain a methyl oleate crystal-ethanol mixture; the mass ratio of the absolute ethyl alcohol solution to the biodiesel is 1: 2;
(2) pumping the methyl oleate crystal-ethanol mixture into a filter 3 through a circulating pump I to obtain a filter cake and a filtrate, feeding the filter cake into a solid methyl oleate storage tank 65, and feeding the filtrate into a filtrate temporary storage tank 56;
(3) starting a vacuum flash evaporation system and a vacuum pump until the vacuum degree of the flash evaporation system is within 50, liquefying a filter cake at normal temperature, then entering a temporary methyl oleate storage tank 64, continuously pumping the liquefied filter cake into a methyl oleate flash evaporation heater 61 through a circulating pump III 9 and a circulating pump IV 10 for heating, then pumping the heated filter cake into a vacuum methyl oleate flash evaporation tank 62 for flash evaporation at 80 ℃, flashing out a trace amount of ethanol gas, and storing the obtained methyl oleate into a methyl oleate storage tank 63;
(4) pumping the filtrate into a flash evaporation heater I51 through a circulating pump II 8 and a circulating pump V11, heating to 85 ℃, continuously entering a normal-pressure flash evaporation tank 52 for flash evaporation, cooling the ethanol obtained by flash evaporation, recovering the ethanol into an ethanol recovery system 14, pumping the methyl linoleate obtained by flash evaporation into a flash evaporation heater II 53 through a circulating pump VI 12 for heating, then entering a vacuum flash evaporation tank 54, controlling the temperature to be 80 ℃ for flash evaporation, flashing out a trace amount of ethanol gas, and storing the obtained methyl linoleate into a methyl linoleate storage tank 55.
Example 2
The device for separating the methyl oleate and the methyl linoleate by the biodiesel is the same as that in the example 1.
The method for separating the methyl oleate and the methyl linoleate from the biodiesel by adopting the device comprises the following steps:
(1) pumping the biodiesel in the biodiesel storage tank 1 at the temperature of 0 ℃ into the fractionation kettle 2, starting a refrigerator and a cooling water pipe of the fractionation kettle 2, pumping the absolute ethanol solution in the ethanol storage tank 4 into the fractionation kettle 2, cooling at the speed of 3 ℃/h, controlling the stirring speed at 70 rpm, and cooling to the temperature of (-19) DEG C; then continuously pumping chilled water into the fractionation kettle 2, cooling the chilled water through a coil pipe, controlling the stirring speed at 50 rpm according to the temperature of 0.8 ℃/h, keeping the temperature at (-26) DEG C, and standing the mixture for 12h to obtain a methyl oleate crystal-ethanol mixture; the mass ratio of the absolute ethyl alcohol solution to the biodiesel is 2: 2;
(2) pumping the methyl oleate crystal-ethanol mixture into a filter 3 through a circulating pump I to obtain a filter cake and a filtrate, feeding the filter cake into a solid methyl oleate storage tank 65, and feeding the filtrate into a filtrate temporary storage tank 56;
(3) starting a vacuum flash evaporation system and a vacuum pump until the vacuum degree of the flash evaporation system is within 50, liquefying a filter cake at normal temperature, then entering a temporary methyl oleate storage tank 64, continuously pumping the liquefied filter cake into a methyl oleate flash evaporation heater 61 through a circulating pump III 9 and a circulating pump IV 10 for heating, then pumping the heated filter cake into a vacuum methyl oleate flash evaporation tank 62 for flash evaporation at 100 ℃, flashing out a trace amount of ethanol gas, and storing the obtained methyl oleate into a methyl oleate storage tank 63;
(4) pumping the filtrate into a flash evaporation heater I51 through a circulating pump II 8 and a circulating pump V11, heating to the temperature of 90 ℃, continuously entering a normal-pressure flash evaporation tank 52 for flash evaporation, cooling the ethanol obtained by flash evaporation, recovering the ethanol into an ethanol recovery system 14, pumping the methyl linoleate obtained by flash evaporation into a flash evaporation heater II 53 through a circulating pump VI 12 for heating, performing flash evaporation in a vacuum flash evaporation tank 54 at the temperature of 100 ℃, flashing off a trace amount of ethanol gas, and storing the obtained methyl linoleate into a methyl linoleate storage tank 55.
Example 3
The device for separating the methyl oleate and the methyl linoleate by the biodiesel is the same as that in the example 1.
The method for separating the methyl oleate and the methyl linoleate from the biodiesel by adopting the device comprises the following steps:
(1) pumping the biodiesel in the biodiesel storage tank 1 at the controlled temperature of (-5) DEG C into the fractionation kettle 2, starting a refrigerator and a cooling water pipe of the fractionation kettle 2, pumping the absolute ethanol solution in the ethanol storage tank 4 into the fractionation kettle 2, cooling at the speed of 2 ℃/h, controlling the stirring speed at 60 revolutions per minute, and cooling to (-17) DEG C; then continuously pumping chilled water into the fractionation kettle 2, cooling the chilled water through a coil pipe, controlling the stirring speed to 40 rpm according to the temperature of 0.6 ℃/h, keeping the temperature to be (-24) DEG C, and standing the mixture for 10h to obtain a methyl oleate crystal-ethanol mixture; the mass ratio of the absolute ethyl alcohol solution to the biodiesel is 1.5: 2;
(2) pumping the methyl oleate crystal-ethanol mixture into a filter 3 through a circulating pump I7 to obtain a filter cake and a filtrate, feeding the filter cake into a solid methyl oleate storage tank 65, and feeding the filtrate into a filtrate temporary storage tank 56;
(3) starting a vacuum flash evaporation system and a vacuum pump until the vacuum degree of the flash evaporation system is within 50, liquefying a filter cake at normal temperature, then entering a temporary methyl oleate storage tank 64, continuously pumping the liquefied filter cake into a methyl oleate flash evaporation heater 61 through a circulating pump III 9 and a circulating pump IV 10 for heating, then pumping the heated filter cake into a vacuum methyl oleate flash evaporation tank 62 for flash evaporation at 90 ℃, flashing out a trace amount of ethanol gas, and storing the obtained methyl oleate into a methyl oleate storage tank 63;
(4) pumping the filtrate into a flash evaporation heater I51 through a circulating pump II 8 and a circulating pump V11, heating to the temperature of 87 ℃, continuously entering a normal-pressure flash evaporation tank 52 for flash evaporation, cooling the flash evaporated ethanol, recovering the cooled flash evaporated ethanol into an ethanol recovery system 14, pumping the flash evaporated methyl linoleate into a flash evaporation heater II 53 through a circulating pump VI 12 for heating, performing flash evaporation in a vacuum flash evaporation tank 54 at the temperature of 90 ℃, flashing off a trace amount of ethanol gas, and storing the obtained methyl linoleate into a methyl linoleate storage tank 55.
The performance data for methyl linoleate and methyl oleate determined in examples 1-3 are as follows, table 1:
| inspection item | Conditional unit | Oleic acid methyl ester | Linoleic acid methyl ester |
| Density of | ﹙20℃﹚g/cm3 | 0.88 | 0.88 |
| Color (appearance) | ---- | Light yellow liquid | Light yellow liquid |
| Freezing point | ℃ | -26 | -34 |
| Full acid number | mgKOH/g | 0.23 | 0.17 |
| Moisture content | mg/kg | ＜50 | ＜50 |
| Content (wt.) | (％) | 79 | 76 |
| Iodine number | gI/100g | 98 | 151 |
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other. The device disclosed by the embodiment corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (5)
1. A device for separating methyl oleate and methyl linoleate from biodiesel is characterized by comprising a biodiesel storage tank, an ethanol storage tank, a fractionation kettle, a filter, a methyl linoleate flash evaporation device and a methyl oleate flash evaporation device;
the biodiesel storage tank is sequentially connected with the ethanol storage tank, the fractionation kettle and the filter; the filter is respectively connected with the methyl linoleate flash evaporation device and the methyl oleate flash evaporation device;
the methyl oleate flash evaporation device comprises a methyl oleate flash evaporation heater, a vacuum methyl oleate flash evaporation tank and a methyl oleate storage tank; the filter is sequentially connected with the methyl oleate flash evaporation heater, the vacuum methyl oleate flash tank and the methyl oleate storage tank.
2. The device for separating the methyl oleate and the methyl linoleate according to the biodiesel of claim 1, wherein the methyl linoleate flash evaporation device comprises a flash heater I, an atmospheric flash evaporation tank, a flash heater II, a vacuum flash evaporation tank and a methyl linoleate storage tank;
the filter is sequentially connected with the flash heater I, the normal-pressure flash tank, the flash heater II, the vacuum flash tank and the methyl linoleate storage tank.
3. The device for separating the methyl oleate and the methyl linoleate by using the biodiesel according to claim 2, wherein the device further comprises a filtrate temporary storage tank, a methyl oleate temporary storage tank and a solid methyl oleate storage tank;
the filter is respectively connected with the filtrate temporary storage tank and the solid methyl oleate storage tank;
the solid methyl oleate storage tank is sequentially connected with the methyl oleate temporary storage tank and the methyl oleate flash evaporation heater;
the filtrate temporary storage tank is connected with the flash evaporation heater I.
4. The device for separating the methyl oleate and the methyl linoleate according to the biodiesel of claim 1, further comprising a freezing chamber, wherein the filter is installed in the freezing chamber.
5. The device for separating the methyl oleate and the methyl linoleate according to claim 3, further comprising a plurality of circulating pumps, wherein the circulating pumps are arranged between the fractionation kettle and the filter, between the filtrate temporary storage tank and the flash heater I, between the vacuum flash tank and the flash heater, and between the flash heater II and the atmospheric flash tank.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113061489A (en) * | 2021-03-26 | 2021-07-02 | 河北金谷再生资源开发有限公司 | Device and method for separating methyl oleate and methyl linoleate from biodiesel |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113061489A (en) * | 2021-03-26 | 2021-07-02 | 河北金谷再生资源开发有限公司 | Device and method for separating methyl oleate and methyl linoleate from biodiesel |
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