CN213506814U - Device for producing biological base oil - Google Patents
Device for producing biological base oil Download PDFInfo
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- CN213506814U CN213506814U CN202022077427.5U CN202022077427U CN213506814U CN 213506814 U CN213506814 U CN 213506814U CN 202022077427 U CN202022077427 U CN 202022077427U CN 213506814 U CN213506814 U CN 213506814U
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Abstract
The utility model discloses a device for producing biological base oil, which comprises a methyl oleate storage tank, an ester exchange reaction kettle, a flash evaporation device, an oleic acid polyol ester storage tank, an epoxidation static mixer, an epoxidation reaction kettle, an epoxy flash evaporation device and a filtering device; the methyl oleate storage tank is connected with the top end of the ester exchange reaction kettle; a raw material inlet is arranged on the ester exchange reaction kettle; the bottom end of the ester exchange reaction kettle is connected with a flash evaporation device; one end of the oleic acid polyol ester storage tank is connected with the flash evaporation device, and the other end of the oleic acid polyol ester storage tank is connected with a first input end of the epoxidation reactor; the second input end of the epoxidation reaction kettle is connected with the epoxidation static mixer, and the output end of the epoxidation reaction kettle is connected with the epoxidation flash evaporation device and the filtering device at one time. The utility model discloses well device is simple, easy operation, and can obtain the biological base oil of production that has excellent performance and high yield.
Description
Technical Field
The utility model relates to a biological base oil technical field, more specifically the device that relates to a production biological base oil that says so.
Background
The production of lubricant base oil and biodiesel or biological solvent oil by using various animal and vegetable oils is the mainstream direction of novel energy, the biological lubricant base oil has excellent physical properties including higher flash point, lower melting point and proper viscosity performance, and complex refining processes such as sulfonation, alkali washing, dewaxing, pour point depression and the like of mineral base oil are not needed when various types of lubricants are prepared, and the environmental pollution caused by a large amount of waste water and waste residues is avoided. Similarly, the biodiesel oil has high ignition performance and complete combustion because of its pure quality and much lower content of sulfide and other impurities than mineral oil, and is an excellent fuel with SO in the exhausted tail gas2The content of He, CO and the like is very low, and the method is greatly beneficial to environmental protection.
The production process of biological lubricating oil is mainly characterized by that under the action of catalyst the animal and plant oil and fat and alcohol chemicals (such as methyl alcohol and ethyl alcohol) are retained at required temperature to make ester exchange reaction so as to produce correspondent fatty acid ester material. Vegetable oils (e.g., rapeseed oil, soybean oil, peanut oil, corn oil, cottonseed oil, etc.), animal oils (e.g., fish oil, lard, tallow, sheep oil, etc.), waste oils, or microbial oils are all sources of fatty acids. The inexhaustible natural entitlements have good biodegradability, are safe and nontoxic, and are clean and environment-friendly raw materials for producing synthetic ester.
However, the existing device for preparing the esters is complex, and a series of problems of high raw material unit consumption, high loss, high energy consumption, long reaction time, unstable reaction zone, low product quality, low yield and the like also occur. Therefore, it is an urgent need to solve the problems of the art to provide an apparatus and a method for producing bio-base oil, which is simple in apparatus and operation, and can provide excellent performance and high yield.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides an apparatus and a preparation method for producing biological base oil, which are simple in apparatus and operation and can obtain excellent performance and high yield.
In order to achieve the above purpose, the utility model adopts the following technical scheme: a device for producing biological base oil comprises a methyl oleate storage tank, an ester exchange reaction kettle, a flash evaporation device, an oleic acid polyol ester storage tank, an epoxidation static mixer, an epoxidation reaction kettle, an epoxy flash evaporation device and a filtering device;
the methyl oleate storage tank is connected with the top end of the ester exchange reaction kettle;
a raw material inlet is arranged on the ester exchange reaction kettle; the bottom end of the ester exchange reaction kettle is connected with the flash evaporation device;
one end of the oleic acid polyol ester storage tank is connected with the flash evaporation device, and the other end of the oleic acid polyol ester storage tank is connected with a first input end of the epoxidation reactor;
and the second input end of the epoxidation reaction kettle is connected with the epoxidation static mixer, and the output end of the epoxidation reaction kettle is connected with the epoxidation flash evaporation device and the filtering device at one time.
The utility model has the advantages that: the ester exchange reaction kettle and the flash evaporation device are arranged in the utility model for preparing the oleic acid polyol ester, and no residue of low-boiling-point substances exists, thereby ensuring that the synthesized polyol fatty acid ester can be used at high temperature; the utility model discloses in still set up epoxidation reaction kettle and epoxy flash distillation device and be for epoxidation preparation biological base oil, adopt the device can guarantee the yield and the performance of final product.
Preferably, the method further comprises the following steps: and the methyl oleate recovery system is connected with the upper part of the ester exchange reaction kettle.
Adopt above-mentioned technical scheme's beneficial effect: the system is arranged to recycle methyl oleate and compound green chemistry.
Preferably, the flash device comprises a flash tank and a flash heater, the input end of the flash heater is respectively connected with the bottom end of the transesterification reaction kettle and the output end of the flash tank, and the output end of the flash heater is connected with the input end of the flash tank; the output end of the flash tank is also connected with the oleic acid polyol ester storage tank.
Adopt above-mentioned technical scheme's beneficial effect: the device is arranged to ensure that the methyl oleate can be completely steamed out, so that the methyl oleate is completely removed, the purity and yield of the oleic acid polyol ester are ensured, and subsequent steps are prevented from being influenced.
Preferably, the method further comprises the following steps: the device comprises a formic acid storage tank and a hydrogen peroxide storage tank, wherein the epoxidation static mixer is respectively connected with the formic acid storage tank and the hydrogen peroxide storage tank.
Adopt above-mentioned technical scheme's beneficial effect: the use amounts of formic acid and hydrogen peroxide are controlled to ensure that the raw materials in the epoxidation static mixer can be supplied to the subsequent reaction steps.
Preferably, the epoxy flash device comprises an epoxy flash tank and an epoxy flash heater, wherein the input end of the epoxy flash heater is connected with the output end of the epoxidation reactor, and the output end of the epoxy flash heater is connected with the input end of the epoxidation flash tank; and the output end of the epoxy flash tank is connected with the filtering device.
Adopt above-mentioned technical scheme's beneficial effect: the device is used for promoting the reaction of the oleic acid polyol ester and the hydrogen peroxide.
Preferably, the filtering device comprises a filtering and mixing tank, a filtering machine, a filtrate temporary storage tank and a biological base oil storage tank; the top end of the filtering and mixing tank is provided with a filtering agent inlet; the input end of the filtering and mixing tank is connected with the output end of the epoxy flash tank, and the output end of the filtering and mixing tank is sequentially connected with the filtering machine, the filtrate temporary storage tank and the biological base oil storage tank.
Adopt above-mentioned technical scheme's beneficial effect: the filtering device is arranged to filter impurities and obtain colorless, tasteless and low freezing point biological base oil.
Preferably, the method further comprises the following steps: and circulating pumps are arranged between the ester exchange reaction kettle and the flash evaporation heater, between the flash evaporation tank and the flash evaporation heater, between the epoxidation reaction kettle and the epoxidation flash evaporation heater, between the epoxidation flash evaporation tank and the epoxidation flash evaporation heater, between the filtering mixing tank and the filter, and between the filtrate temporary storage tank and the biological base oil storage 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.
According to the technical scheme, compared with the prior art, the utility model discloses a device for producing biological base oil, the appearance of the oleic acid polyol ester prepared by the device of the utility model is light yellow, the acid value is about 0.1-0.3mgKOH/g, and the content of the oleic acid polyol ester is more than 98%; and the finally obtained finished product of the biological base oil has the properties of no color, no smell, high flash point and low condensation point.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be 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 preparation of oleic acid polyol ester according to the present invention;
FIG. 2 is a schematic diagram of the epoxidation reaction provided by the present invention;
FIG. 3 is a schematic structural diagram of a filtering apparatus according to the present invention;
wherein, the device comprises a 1-methyl oleate storage tank, a 2-ester exchange reaction kettle, a 3-flash evaporation device, a 4-oleic acid polyol ester storage tank, a 5-epoxidation static mixer, a 6-epoxidation reaction kettle, a 7-epoxy flash evaporation device, an 8-filtering device, a 9-methyl oleate recovery system, a 10-formic acid storage tank, an 11-hydrogen peroxide storage tank, a 12-filtering device, a 13-circulating pump I, a 14-circulating pump II, a 15-circulating pump III, a 16-circulating pump IV, a 17-circulating pump V and an 18-circulating pump VI,
21-a raw material inlet, 31-a flash tank, 32-a flash heater, 61-a sewage system, 71-an epoxy flash tank, 72-an epoxy flash heater, 81-a filtering and mixing tank, 82-a filter, 83-a filtrate temporary storage tank, 84-a biological base oil storage tank and 85-a filter agent inlet.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Referring to the attached drawings 1-3, the embodiment of the utility model discloses a device for producing biological base oil, which comprises a methyl oleate storage tank 1, an ester exchange reaction kettle 2, a flash evaporation device 3, an oleic acid polyol ester storage tank 4, an epoxidation static mixer 5, an epoxidation reaction kettle 6, an epoxidation flash evaporation device 73 and a filtering device 128;
the methyl oleate storage tank 1 is connected with the top end of the ester exchange reaction kettle 2;
the ester exchange reaction kettle 2 is provided with a raw material inlet 21; the bottom end of the ester exchange reaction kettle 2 is connected with a flash evaporation device 3;
one end of the oleic acid polyol ester storage tank 4 is connected with the flash evaporation device 3, and the other end of the oleic acid polyol ester storage tank is connected with a first input end of the epoxidation reactor 6;
the second input end of the epoxidation reactor 6 is connected with the epoxidation static mixer 5, and the output end is connected with the epoxidation flash evaporation device 3 and the filtering device 12 at one time.
In one embodiment, further comprising: a methyl oleate recovery system 9, wherein the methyl oleate recovery system 9 is connected with the upper part of the ester exchange reaction kettle 2.
In one embodiment, the flash evaporation device 3 comprises a flash evaporation tank 31 and a flash evaporation heater 32, wherein the input end of the flash evaporation heater 32 is connected with the bottom end of the transesterification reaction kettle 2 and the output end of the flash evaporation tank 31, and the output end is connected with the input end of the flash evaporation tank 31; the output end of the flash tank 31 is also connected with the oleic acid polyol ester storage tank 4. The device is arranged to ensure that the methyl oleate can be completely steamed out, so that the methyl oleate is completely removed, the purity and yield of the oleic acid polyol ester are ensured, and subsequent steps are prevented from being influenced.
In one embodiment, further comprising: the formic acid storage tank 10, the hydrogen peroxide storage tank 11 and the epoxidation static mixer 5 are respectively connected with the formic acid storage tank 10 and the hydrogen peroxide storage tank 11. The formic acid storage tank 10 and the hydrogen peroxide storage tank 11 are arranged to control the use amounts of formic acid and hydrogen peroxide, so that the raw materials in the epoxidation static mixer 5 can be supplied to the subsequent reaction steps.
In one embodiment, the epoxy flash apparatus 73 includes an epoxy flash tank 71 and an epoxy flash heater 72, an input terminal of the epoxy flash heater 72 is connected to an output terminal of the epoxidation reactor 6, and an output terminal thereof is connected to an input terminal of the epoxidation flash tank 31; the output of the epoxy flash tank 71 is connected to the filtration device 12. The device is used for promoting the reaction of the oleic acid polyol ester and the hydrogen peroxide. The bottom of the epoxidation reaction kettle 6 is also provided with a sewage system 61 for discharging the sewage of the epoxidation reaction kettle 6 into the sewage system 61 for treatment, so that the environment pollution is avoided.
In one embodiment, the filtering apparatus 12 comprises a filtering mixing tank 81, a filtering machine 82, a filtrate temporary storage tank 83 and a bio-base oil storage tank 84; the top end of the filtering and mixing tank 81 is provided with a filtering agent inlet 85; the input end of the filtering and mixing tank 81 is connected with the output end of the epoxy flash tank 71, and the output end is sequentially connected with the filter 82, the filtrate temporary storage tank 83 and the biological base oil storage tank 84. The filtering device 12 is provided in order to filter impurities and obtain a biological base oil that is colorless, odorless and has a low freezing point.
In one embodiment, further comprising: and circulating pumps are arranged between the ester exchange reaction kettle 2 and the flash heater 32, between the flash tank 31 and the flash heater 32, between the epoxidation reaction kettle 6 and the epoxidation flash heater 72, between the epoxidation flash tank 31 and the epoxidation flash heater 72, between the filtering mixing tank 81 and the filtering machine 82, and between the filtrate temporary storage tank 83 and the biological base oil storage tank 84. The purpose of the circulation pump is to generate power to drive the material into the required equipment.
Example 1
The method for producing the biological base oil by adopting the device comprises the following steps:
(1) under the protection of nitrogen, adding polyol into a transesterification reaction kettle 2 through a raw material inlet 21, and heating to 60 ℃; after the polyhydric alcohol is dissolved, adding a formic acid catalyst and methyl oleate into the ester exchange reaction kettle 2, controlling the speed of the ester exchange reaction kettle 2 at 60r/min and the temperature at 160 ℃, and reacting for 3 hours; then, adding phosphoric acid into the transesterification reaction kettle 2 and controlling the pH value of the transesterification reaction kettle 2 to be 7; obtaining a mixture A; wherein the mass of the formic acid catalyst accounts for 0.1% of the mass of the methyl oleate, and the mass of the phosphoric acid accounts for 0.05% of the mass of the methyl oleate;
(2) pumping the mixture A into a flash tank 31 through a circulating pump I13, heating for 2 hours at the temperature of 180 ℃, stopping heating, cooling to 80 ℃ to obtain oleic acid polyol ester, and pumping the oleic acid polyol ester into an oleic acid polyol ester storage tank 4 through a circulating pump II 14 for later use; the content of the oleic acid polyol ester is 99.2 percent;
(3) pumping oleic acid polyol ester into an epoxidation reaction kettle 6, starting stirring and controlling the temperature to 60 ℃; pumping formic acid in a formic acid storage tank 10 and hydrogen peroxide in a hydrogen peroxide storage tank 11 into an epoxidation reaction kettle 6 through an epoxidation static mixer 5, controlling the temperature of the epoxidation reaction kettle 6 at 60 ℃ by using cooling water, stirring at the speed of 60r/min, and preserving heat for 5 hours to obtain a mixture B; standing for 2h, pumping the hydrogen peroxide and formic acid left in the reaction into a sewage system 61 for treatment and discharging; wherein, the mass of the hydrogen peroxide accounts for 25 percent of that of the oleic acid polyol ester, and the mass of the formic acid accounts for 2.5 percent of that of the oleic acid polyol ester.
(4) Controlling the vacuum degree of the epoxidation reaction kettle 6 to be (-0.1) MPa, heating the mixture B in the epoxidation reaction kettle 6 to 100 ℃, pumping the mixture B into an epoxy flash tank 71 through a circulating pump III 15, and removing moisture in epoxy flash through an epoxy flash heater 72 to obtain a mixture C; (5) pumping the mixture C into a filtering and mixing tank 81 through a circulating pump IV 16, stirring at the speed of 60r/min, adding argil and diatomite into the filtering and mixing tank 81 through a filtering agent inlet 85, stirring at the temperature of 95 ℃ and at the speed of 60r/min for carrying out adsorption reaction for 0.5h, pumping the material into a filter 82 through a circulating pump V17, feeding the obtained product into a filtrate temporary storage tank 83, and pumping into a biological base oil storage tank 84 through a circulating pump VI 18; wherein, the mass of the argil is 0.01 percent of the mass of the mixture C, and the mass of the diatomite is 0.01 percent of the mass of the mixture C.
Example 2
The method for producing the biological base oil by adopting the device comprises the following steps:
(1) under the protection of nitrogen, adding polyol into a transesterification reaction kettle 2 through a raw material inlet 21, and heating to 100 ℃; after the polyhydric alcohol is dissolved, adding a formic acid catalyst and methyl oleate into the ester exchange reaction kettle 2, and controlling the speed of the ester exchange reaction kettle 2 at 80r/min and the temperature at 200 ℃ for reaction for 10 hours; then, adding phosphoric acid into the transesterification reaction kettle 2 and controlling the pH value of the transesterification reaction kettle 2 to be 7; obtaining a mixture A; wherein the mass of the formic acid catalyst accounts for 0.3% of the mass of the methyl oleate, and the mass of the phosphoric acid accounts for 0.1% of the mass of the methyl oleate;
(2) pumping the mixture A into a flash tank 31 through a circulating pump I13, heating for 3 hours at the temperature of 200 ℃, stopping heating, cooling to 80 ℃, and pumping the obtained oleic acid polyol ester into an oleic acid polyol ester storage tank 4 through a circulating pump II 14 for later use; the content of the oleic acid polyol ester is 99.6 percent;
(3) pumping oleic acid polyol ester into an epoxidation reaction kettle 6, starting stirring and controlling the temperature to 65 ℃; pumping formic acid in a formic acid storage tank 10 and hydrogen peroxide in a hydrogen peroxide storage tank 11 into an epoxidation reaction kettle 6 through an epoxidation static mixer 5, controlling the temperature of the epoxidation reaction kettle 6 at 65 ℃ by using cooling water, stirring at the speed of 80r/min, and preserving heat for 8 hours to obtain a mixture B; standing for 2h, pumping the hydrogen peroxide and formic acid left in the reaction into a sewage system 61 for treatment and discharging; wherein, the mass of the hydrogen peroxide accounts for 30 percent of that of the oleic acid polyol ester, and the mass of the formic acid accounts for 3 percent of that of the oleic acid polyol ester.
(4) Controlling the vacuum degree of the epoxidation reaction kettle 6 to be (-0.1) MPa, heating the mixture B in the epoxidation reaction kettle 6 to 105 ℃, pumping the mixture B into an epoxy flash tank 71 through a circulating pump III 15, and removing moisture in epoxy flash through an epoxy flash heater 72 to obtain a mixture C; (5) pumping the mixture C into a filtering and mixing tank 81 through a circulating pump IV 16, stirring at the speed of 80r/min, adding argil and diatomite into the filtering and mixing tank 81 through a filtering agent inlet 85, stirring at 105 ℃ and 80r/min for carrying out adsorption reaction for 2 hours, pumping the material into a filter 82 through a circulating pump V17, feeding the obtained product into a filtrate temporary storage tank 83, and pumping into a biological base oil storage tank 84 through a circulating pump VI 18; wherein, the mass of the argil is 0.05 percent of the mass of the mixture C, and the mass of the diatomite is 0.05 percent of the mass of the mixture C.
Example 3
The method for producing the biological base oil by adopting the device comprises the following steps:
(1) under the protection of nitrogen, adding polyol into a transesterification reaction kettle 2 through a raw material inlet 21, and heating to 80 ℃; after the polyhydric alcohol is dissolved, adding a formic acid catalyst and methyl oleate into the ester exchange reaction kettle 2, and controlling the speed of the ester exchange reaction kettle 2 at 70r/min and the temperature at 180 ℃ for reaction for 6 hours; then, adding phosphoric acid into the transesterification reaction kettle 2 and controlling the pH value of the transesterification reaction kettle 2 to be 7; obtaining a mixture A; wherein the mass of the formic acid catalyst accounts for 0.2% of the mass of the methyl oleate, and the mass of the phosphoric acid accounts for 0.08% of the mass of the methyl oleate;
(2) pumping the mixture A into a flash tank 31 through a circulating pump I13, heating for 2.5 hours at the temperature of 190 ℃, stopping heating, cooling to 80 ℃, and pumping the obtained oleic acid polyol ester into an oleic acid polyol ester storage tank 4 through a circulating pump II 14 for later use; the content of the oleic acid polyol ester is 99.5 percent;
(3) pumping oleic acid polyol ester into an epoxidation reaction kettle 6, starting stirring and controlling the temperature to 60 ℃; pumping formic acid in a formic acid storage tank 10 and hydrogen peroxide in a hydrogen peroxide storage tank 11 into an epoxidation reaction kettle 6 through an epoxidation static mixer 5, controlling the temperature of the epoxidation reaction kettle 6 at 60-65 ℃ by using cooling water, stirring at the speed of 70r/min, and preserving heat for 7 hours to obtain a mixture B; standing for 2h, pumping the hydrogen peroxide and formic acid left in the reaction into a sewage system 61 for treatment and discharging; wherein, the mass of the hydrogen peroxide accounts for 28 percent of that of the oleic acid polyol ester, and the mass of the formic acid accounts for 2.5 percent of that of the oleic acid polyol ester.
(4) Controlling the vacuum degree of the epoxidation reaction kettle 6 to be (-0.1) MPa, heating the mixture B in the epoxidation reaction kettle 6 to 102 ℃, pumping the mixture B into an epoxy flash tank 71 through a circulating pump III 15, and removing moisture in epoxy flash through an epoxy flash heater 72 to obtain a mixture C; (5) pumping the mixture C into a filtering and mixing tank 81 through a circulating pump IV 16, stirring at the speed of 60r/min, adding argil and diatomite into the filtering and mixing tank 81 through a filtering agent inlet 85, stirring at the temperature of 100 ℃ and at the speed of 60r/min for carrying out adsorption reaction for 1.2h, pumping the material into a filter 82 through a circulating pump V17, feeding the obtained product into a filtrate temporary storage tank 83, and pumping into a biological base oil storage tank 84 through a circulating pump VI 18; wherein, the mass of the argil is 0.03 percent of the mass of the mixture C, and the mass of the diatomite is 0.03 percent of the mass of the mixture C.
Performance testing
The performance of the bio-base oil obtained in examples 1-3 of the present invention was determined according to the national standard GB/T20828-:
performance results data for the biological base oils of examples 1-3
As can be seen from the table 1, the biological base oil obtained by the device has the characteristics of high flash point, low condensation point, degradability and the like, so that the comprehensive performance is outstanding. The bio-based base oil has very wide application in the industries of aviation, wind power, automobiles, machining, transportation, metallurgy, coal, building, light industry and the like. Bio-based base oils are becoming more popular and have incomparable characteristics with mineral base oils, namely biodegradability to rapidly reduce environmental pollution.
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 invention. 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 (7)
1. The device for producing the biological base oil is characterized by comprising a methyl oleate storage tank, an ester exchange reaction kettle, a flash evaporation device, an oleic acid polyol ester storage tank, an epoxidation static mixer, an epoxidation reaction kettle, an epoxy flash evaporation device and a filtering device;
the methyl oleate storage tank is connected with the top end of the ester exchange reaction kettle;
a raw material inlet is arranged on the ester exchange reaction kettle; the bottom end of the ester exchange reaction kettle is connected with the flash evaporation device;
one end of the oleic acid polyol ester storage tank is connected with the flash evaporation device, and the other end of the oleic acid polyol ester storage tank is connected with a first input end of the epoxidation reactor;
and a second input end of the epoxidation reaction kettle is connected with the epoxidation static mixer, and an output end of the epoxidation reaction kettle is sequentially connected with the epoxidation flash evaporation device and the filtering device.
2. The apparatus for manufacturing bio-base oil according to claim 1, further comprising: and the methyl oleate recovery system is connected with the upper part of the ester exchange reaction kettle.
3. The apparatus for producing bio-base oil according to claim 2, wherein the flash apparatus comprises a flash tank and a flash heater, the input end of the flash heater is connected to the bottom end of the transesterification reaction vessel and the output end of the flash tank, respectively, and the output end is connected to the input end of the flash tank; the output end of the flash tank is also connected with the oleic acid polyol ester storage tank.
4. An apparatus for producing bio base oil according to claim 3, further comprising: the device comprises a formic acid storage tank and a hydrogen peroxide storage tank, wherein the epoxidation static mixer is respectively connected with the formic acid storage tank and the hydrogen peroxide storage tank.
5. The apparatus for producing bio-base oil according to claim 4, wherein the epoxy flash apparatus comprises an epoxy flash tank and an epoxy flash heater, an input end of the epoxy flash heater is connected to an output end of the epoxidation reactor, and an output end of the epoxy flash heater is connected to an input end of the epoxidation flash tank; and the output end of the epoxy flash tank is connected with the filtering device.
6. The apparatus for producing bio-base oil according to claim 5, wherein said filtering apparatus comprises a filtering mixing tank, a filtering machine, a filtrate temporary storage tank and a bio-base oil storage tank;
the top end of the filtering and mixing tank is provided with a filtering agent inlet;
the input end of the filtering and mixing tank is connected with the output end of the epoxy flash tank, and the output end of the filtering and mixing tank is sequentially connected with the filtering machine, the filtrate temporary storage tank and the biological base oil storage tank.
7. An apparatus for producing bio base oil according to claim 6, further comprising: and circulating pumps are arranged between the ester exchange reaction kettle and the flash evaporation heater, between the flash evaporation tank and the flash evaporation heater, between the epoxidation reaction kettle and the epoxidation flash evaporation heater, between the epoxidation flash evaporation tank and the epoxidation flash evaporation heater, between the filtering mixing tank and the filter, and between the filtrate temporary storage tank and the biological base oil storage tank.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112094701A (en) * | 2020-09-21 | 2020-12-18 | 河北金谷再生资源开发有限公司 | Device for producing biological base oil and preparation method thereof |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112094701A (en) * | 2020-09-21 | 2020-12-18 | 河北金谷再生资源开发有限公司 | Device for producing biological base oil and preparation method thereof |
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