CN115386432A - System for producing biodiesel by using double enzymes and production method thereof - Google Patents

System for producing biodiesel by using double enzymes and production method thereof Download PDF

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Publication number
CN115386432A
CN115386432A CN202210907754.XA CN202210907754A CN115386432A CN 115386432 A CN115386432 A CN 115386432A CN 202210907754 A CN202210907754 A CN 202210907754A CN 115386432 A CN115386432 A CN 115386432A
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water
pipe
tank
distillation
liquid
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陈鹏
陈好睿
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Hunan Nuoreixin Biotechnology Co ltd
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Hunan Nuoreixin Biotechnology Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
    • C11C1/02—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils
    • C11C1/04—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils by hydrolysis
    • C11C1/045—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils by hydrolysis using enzymes or microorganisms, living or dead
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Abstract

The invention discloses a system for producing biodiesel by utilizing double enzymes and a production method thereof, belonging to the technical field of biodiesel. The immobilized lipase immobilized device has the advantages of simple structure, scientific and reasonable design, convenient use, capability of greatly reducing the use cost of the immobilized lipase in production, stable indexes after the enzyme immobilization reaction and capability of reaching the national standard, safety, environmental protection, high yield and the like.

Description

System for producing biodiesel by using double enzymes and production method thereof
Technical Field
The invention belongs to the technical field of biodiesel, and particularly relates to a system for producing biodiesel by using double enzymes and a production method thereof.
Background
At present, the domestic biodiesel technology basically comprises the following steps: an acid-base two-step catalysis method, a glycerin pre-esterification and then base catalysis transesterification method, a hydrolyzed oil and fat after acid catalysis esterification method, a refining deacidification and then base catalysis transesterification method, a one-step liquid lipase and base saponification deacidification method, a one-step liquid lipase and critical method, a liquid lipase and immobilized lipase double-enzyme method and the like.
The acid-base two-step catalysis method has the advantages that the acid-base corrosion action requires the equipment to have the corrosion prevention effect, so that the equipment investment is large, the acid-base neutralization is realized due to the use of the acid-base, a large amount of salt and grease are saponified, the sewage treatment difficulty is increased, the environmental protection pressure is increased, the yield of the grease with high saponification loss is difficult to guarantee, and the yield of the biodiesel finished product which is the common kitchen waste oil raw material is about 85%.
In the process of glycerin esterification, because high-temperature reaction is easy to cause polymerization reaction to lose grease and glycerin, and simultaneously, a large amount of grease is saponified in the alkali-catalyzed esterification reaction at the later stage, the yield of the method is difficult to guarantee and is basically between 88 and 90 percent.
The acid catalysis esterification method after grease hydrolysis has large environmental protection pressure due to a large amount of sewage generated in the hydrolysis process, and the hydrolysis tower and the acid catalysis reaction kettle both need to have an anti-corrosion effect, so the equipment investment is relatively high.
The refining deacidification method adopts distillation deacidification in the refining deacidification process with higher cost, the process cannot produce waste grease with higher content of free fatty acid, the raw material selection range is too narrow, more grease is saponified in the alkali-catalyzed transesterification at the later stage, and the yield is also lower.
The one-step liquid lipase alkali-adding saponification deacidification method saponifies a large amount of grease along with unesterified and thorough free fatty acid during alkali addition, and the yield is seriously discounted.
As the critical method of the one-step liquid lipase and the critical method belongs to high temperature and high pressure and is difficult to ensure, the explosion accidents of factories using the process often occur.
The two-enzyme method for reinforcing the immobilized lipase by using the liquid lipase is the safest, most environment-friendly and highest yield (generally 4-5% higher than any process) process at present, but the use cost of the biological lipase is extremely high due to the fact that the price of the biological lipase, particularly the price of the immobilized lipase, is too high, and the immobilized lipase is extremely easy to inactivate and lose efficacy in the actual production process, so that the biological lipase is used in few factories at home at present.
Meanwhile, the processes adopt final reduced pressure distillation to obtain a finished product, and the reacted materials are cracked under high temperature in the distillation process so that the acid value of the materials exceeds the standard again.
Therefore, it is a technical problem to be solved by those skilled in the art that immobilized lipase can be stably maintained in a use batch for more than 300 times without inactivation or invalidation due to material reasons, or the acid value index of the product can meet the national standard.
Therefore, the invention provides a system for producing biodiesel by utilizing double enzymes and a production method thereof, which can greatly reduce the use cost of immobilized lipase in production, simultaneously, various indexes after the immobilized lipase reaction can be stable and reach the national standard, and the system has the advantages of safety, environmental protection, high yield and the like.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: provides a system for producing biodiesel by using double enzymes and a production method thereof, which at least solve the partial technical problems.
In order to realize the purpose, the technical scheme adopted by the invention is as follows:
the utility model provides a system for utilize two enzyme production biodiesel, including the liquid enzyme retort that is used for liquid lipase catalytic reaction, connect out the separating mechanism who is used for the reaction product separation from the liquid enzyme retort, connect out the drying mechanism who is used for the dry dewatering of separation product from the separating mechanism, connect out the distillation mechanism who is used for the distillation edulcoration of separation product from the drying mechanism, respectively from the vacuum circulation cooling body that drying mechanism and distillation mechanism connect out, and connect out the solid enzyme retort that is used for immobilized lipase catalytic reaction from the distillation mechanism, be equipped with the continuous settling mechanism who is used for liquid enzyme to retrieve to recycle between separating mechanism and the liquid enzyme retort, be connected with the liquid enzyme circulating pipe between continuous settling mechanism and the liquid lipase retort, vacuum circulation cooling mechanism is connected with tail gas treatment mechanism.
Further, the separation mechanism comprises a decanter centrifuge which is connected out from the liquid enzyme reaction tank and is used for separating oil phase, water phase and solid phase of reaction products, and a buffer tank which is connected out from the decanter centrifuge and is used for storing fatty acid methyl ester of the oil phase; a centrifugal liquid inlet pipe is connected between the liquid enzyme reaction tank and the sedimentation centrifuge, a liquid inlet pump is arranged on the centrifugal liquid inlet pipe, an oil outlet pipe is arranged between an oil port of the sedimentation centrifuge and the buffer tank, and an oil outlet valve is arranged on the oil outlet pipe.
Further, the continuous sedimentation mechanism comprises a first sedimentation tank connected with a water phase outlet of the sedimentation centrifuge, the upper part of the first sedimentation tank is connected with a first recovery pipe, and the first recovery pipe is connected with a liquid enzyme circulating pipe;
the continuous sedimentation mechanism also comprises a second sedimentation tank connected from the first sedimentation tank, the upper part of the second sedimentation tank is connected with a second recovery pipe, and the second recovery pipe is connected with the liquid enzyme circulating pipe;
the continuous sedimentation mechanism also comprises a third sedimentation tank connected from the second sedimentation tank, the upper part of the third sedimentation tank is connected with a third recovery pipe, and the third recovery pipe is connected with the liquid enzyme circulating pipe;
a first material discharge pipe is connected between the first settling tank and the second settling tank, a second material discharge pipe is connected between the second settling tank and the third settling tank, and the third settling tank is connected with a third material discharge pipe;
the first recovery pipe, the second recovery pipe and the third recovery pipe are respectively provided with a first recovery valve, a second recovery valve and a third recovery valve, and the liquid enzyme circulating pipe is provided with a recovery pump;
the liquid lipase reaction tank is provided with a grease input port, a methanol input port, a liquid enzyme input port and a liquid enzyme recovery port, the liquid enzyme circulating pipe is connected with the liquid enzyme recovery port, a water outlet pipe is arranged between the water phase outlet of the decanter centrifuge and the first settling tank, and the water outlet pipe is provided with a water outlet valve.
Furthermore, the drying mechanism comprises a drying condensing tower connected out of the cache tank, a drying packed bed is arranged in the middle of the drying condensing tower, a drying condenser is arranged at the upper part of the drying condensing tower, drying packing is arranged in the drying packed bed, a first drying condensate flow guide plate and a second drying condensate flow guide plate are arranged below the drying condenser, and a drying condensate collecting tank is arranged below the second drying condensate flow guide plate;
a drying and heating feeding pipe is connected between the buffer tank and the drying and condensing tower, and a drying and feeding pump and a drying and feeding heater are arranged on the drying and heating feeding pipe.
Further, the distillation mechanism comprises a distillation tower connected out of the drying condensation tower and a condensed material cache tank connected out of the distillation tower and connected into the immobilized enzyme reaction tank, a distillation circulating pipe connected out of the bottom of the distillation tower and connected into the middle of the distillation tower is arranged on the distillation tower, a distillation circulating pump and a distillation circulating heater are arranged on the distillation circulating pipe, a distillation packed bed is arranged in the middle of the distillation tower, a distillation condenser is arranged at the upper part of the distillation tower, a distilled heavy oil discharge pipe connected into a distilled heavy oil treatment working section is connected to the bottom of the distillation tower, distillation packing is arranged in the distillation packed bed, a first distillation condensate flow guide plate and a second distillation condensate flow guide plate are arranged below the distillation condenser, a distillation condensate collecting tank is arranged below the second distillation condensate flow guide plate, a distillation heavy oil discharge pump is arranged on the distillation heavy oil discharge pipe, a distillation condensate discharge port is formed in the distillation condensate collecting tank, a condensed material discharge pipe is connected between the distillation condensate collecting tank and the condensed material cache tank, and a condensate cooling heat exchanger is arranged on the condensed material discharge pipe;
a distillation feed pipe is connected between the drying condensation tower and the distillation tower, and a drying discharge pump and a distillation feed heater are arranged on the distillation feed pipe.
Furthermore, a solid enzyme reaction circulating pipe which is connected out of the bottom of the solid enzyme reaction tank and is connected into the top of the solid enzyme reaction tank is arranged on the solid enzyme reaction tank, a solid enzyme reaction circulating pump is arranged on the solid enzyme reaction circulating pipe, a solid enzyme reaction discharging pipe which is connected to a finished product drying section is arranged on the lower middle portion of the solid enzyme reaction tank, a solid enzyme reaction discharging pump is arranged on the solid enzyme reaction discharging pipe, an immobilized lipase bed is arranged in a condensed material cache tank, immobilized lipase is arranged in the immobilized lipase bed, a solid enzyme feeding pipe is connected in front of the condensed material cache tank and the solid enzyme reaction tank, and a solid enzyme feeding pump is arranged on the solid enzyme feeding pipe.
Furthermore, the vacuum circulating cooling mechanism comprises a water ring vacuum pump, a water storage tank and a condensing mechanism, wherein the water ring vacuum pump is connected with the top of the drying condensing tower and the top of the distillation tower through pipelines respectively;
the water ring vacuum pump is provided with an air suction port and an air exhaust port, the water storage tank is provided with a first water inlet, a first water outlet and an exhaust gas outlet, the water ring vacuum pump is provided with a water inlet communicated with a water ring of the water ring vacuum pump, the first water inlet is connected with the air exhaust port of the water ring vacuum pump through a pipeline, and the first water outlet is connected with the water inlet of the water ring vacuum pump.
Furthermore, the condensing mechanism comprises a spiral plate type heat exchanger connected with the water storage tank, a first circulating water pump connected between the water storage tank and the spiral plate type heat exchanger, and a cold water tank connected with the spiral plate type heat exchanger;
the spiral plate type heat exchanger comprises a heat exchanger main body, a first spiral heat exchange channel and a second spiral heat exchange channel, wherein the first spiral heat exchange channel and the second spiral heat exchange channel are arranged in the heat exchanger main body;
the water storage tank is provided with a second water inlet and a second water outlet, the second water inlet is connected with the water outlet of the first spiral heat exchange channel through a first pipeline, and the second water outlet is connected with the water inlet of the first spiral heat exchange channel through a second pipeline;
the first circulating water pump is arranged on the second pipeline, the second pipeline is connected with a drain pipe, the drain pipe is connected between the first circulating water pump and the first spiral heat exchange channel, a drain valve is arranged on the drain pipe, the drain pipe is connected to a sewage treatment workshop section, the first pipeline is connected with a water inlet pipe, the water inlet pipe is connected out from the inner bottom of the cold water tank, a water inlet valve and a water pump are arranged on the water inlet pipe, the water inlet and the water outlet of the second spiral heat exchange channel are respectively connected with the inner bottom and the inner top of the cold water tank through pipelines, and the second circulating water pump is arranged on a pipeline connecting the water inlet of the second spiral heat exchange channel and the inner bottom of the cold water tank.
Furthermore, the tail gas treatment mechanism comprises an alkali liquor spray tower which is connected out from a waste gas outlet of the water storage tank through a pipeline and used for tail gas purification, a gas-liquid separation tower which is connected out from the alkali liquor spray tower and used for purified tail gas separation, and a boiler which is arranged beside the gas-liquid separation tower and used for performing harmless treatment on purified gas, wherein a circulating spray device used for recycling alkali liquor is arranged on the alkali liquor spray tower, and a blower used for pumping purified tail gas into the boiler;
the circulating spraying device comprises an alkali liquor circulating pipe connected out of the alkali liquor spraying tower and circulating spraying mechanisms connected with the alkali liquor circulating pipe and extending into the alkali liquor spraying tower for spraying alkali liquor on the distillation tail gas, wherein the alkali liquor circulating pipe is provided with an alkali liquor circulating pump and valves, and the circulating spraying mechanisms are at least two and comprise spraying pipes connected out of the alkali liquor circulating pipe and spiral spraying nozzles arranged on the spraying pipes;
an upper observation sight glass for observing the accumulation condition of the reaction soap is arranged at the middle lower part of the alkali liquor spray tower, a lower observation sight glass for observing alkali liquor in the alkali liquor spray tower is arranged at the lower part of the alkali liquor spray tower, a gas pipe is connected between the alkali liquor spray tower and the gas-liquid separation tower, the gas pipe is connected out of the top of the alkali liquor spray tower and is connected to the lower part of the gas-liquid separation tower, the diameter of the gas pipe is at least 15cm, an observation sight glass for observing separation liquid is arranged at the middle lower part of the gas-liquid separation tower, and a liquid outlet is formed at the bottom of the gas-liquid separation tower;
the top of the gas-liquid separation tower is connected with an exhaust pipe, the gas outlet of the exhaust pipe is opposite to the gas inlet of the blower and the distance between the gas outlet of the exhaust pipe and the gas inlet of the blower is at least 2 m;
the upper part of the alkali liquor spray tower is provided with an alkali liquor inlet for supplementing alkali liquor, the bottom of the alkali liquor spray tower is provided with an alkali liquor outlet for discharging waste alkali liquor, and the alkali liquor outlet is provided with a liquid discharge valve.
A production method of a system for producing biodiesel by using double enzymes comprises the following steps:
s1, feeding the waste animal and vegetable oil into a liquid enzyme reaction tank, and hydrolyzing the waste animal and vegetable oil with methanol and water in the tank under the catalysis of liquid lipase to generate fatty acid methyl ester;
s2, separating solid-phase residues, a water-phase liquid enzyme aqueous solution and oil-phase mixed fatty acid from a mixture consisting of the product and the raw material in the step S1 in a separation mechanism;
s3, separating the aqueous phase liquid enzyme solution by a continuous settling mechanism to obtain liquid lipase, introducing the liquid lipase into a liquid enzyme reaction tank for recycling, and removing water and waste gas from the oil-phase mixed fatty acid in a drying mechanism;
s4, removing waste gas and heavy oil from the mixed fatty acid with water and gas removed in a distillation mechanism to obtain primary methyl ester;
s5, allowing the primary methyl ester to enter a solid enzyme reaction tank for secondary hydrolysis under the catalysis of immobilized lipase, so that residual free fatty acid in the primary methyl ester completely reacts with triglyceride to generate fatty acid methyl ester;
s6, filtering and purifying the waste gas removed in the steps S3 and S4 in a vacuum circulating cooling mechanism to obtain primary purified tail gas;
and S7, allowing the primary purified tail gas to enter a tail gas treatment mechanism for saponification purification, and finally entering a boiler for combustion.
Compared with the prior art, the invention has the following beneficial effects:
the invention has simple structure, scientific and reasonable design and convenient use, and solves the technical problems that the unreasonable arrangement of the existing double-enzyme production system causes the inactivation and invalidation of the immobilized lipase easily and the acid value of the product does not reach the standard. According to the invention, the existing process system is adjusted, the distillation working section which is traditionally placed at the tail end is adjusted to the middle section, on one hand, the reaction mixture enters the distillation working section after the liquid lipase reacts, the substances harmful to the immobilized lipase are removed, and then the immobilized lipase catalytic reaction is carried out, so that the damage of the materials to the immobilized lipase is reduced to the lowest, the use batch of the immobilized lipase is greatly improved, and the cost of the immobilized lipase is reduced; on the other hand, the distillation section is preposed, so that the phenomenon that the acid value of the material rises again and exceeds the standard due to the cracking of the material caused by high temperature in the last distillation is effectively avoided, and the stability of the acid value of the product is ensured. The invention also optimizes the prior process system, wherein the continuous sedimentation mechanism separates and recovers the liquid enzyme, and the recovered liquid enzyme can be put into the liquid lipase reaction tank for recycling, so as to achieve the purpose of greatly reducing the cost of the liquid lipase; the vacuum circulating cooling mechanism adopts circulating water cooling to cool the vacuum pump, so that a large amount of water resources are saved; the tail gas treatment mechanism adopts targeted liquid to spray according to tail gas components, then the spray is subjected to gas-liquid separation, and the sprayed liquid is introduced into the boiler for high-temperature incineration so as to meet the emission requirement, save a large amount of investment and operation cost, and more effectively achieve the purposes of environmental protection and energy saving.
Drawings
FIG. 1 is a system diagram of the present invention.
FIG. 2 is a diagram showing the connection of the liquid enzyme reaction tank with the separation mechanism and the continuous sedimentation mechanism according to the present invention.
Fig. 3 is a structural view of the continuous sedimentation mechanism of the present invention.
FIG. 4 is a view showing the structure of a distillation mechanism according to the present invention.
Fig. 5 is a structural view of the drying mechanism of the present invention.
FIG. 6 is an enlarged view of a immobilized enzyme reaction tank of the present invention.
FIG. 7 is a view showing the structure of the vacuum circulation cooling mechanism of the present invention.
Fig. 8 is a cross-sectional view of a spiral plate heat exchanger of the present invention.
FIG. 9 is a structural view of an exhaust gas treating means according to the present invention.
Wherein, the names corresponding to the reference numbers are:
1-liquid enzyme reaction tank, 2-separation mechanism, 3-drying mechanism, 4-distillation mechanism, 5-vacuum circulating cooling mechanism, 6-solid enzyme reaction tank, 7-continuous sedimentation mechanism, 8-tail gas treatment mechanism, 101-grease input port, 102-methanol input port, 103-liquid enzyme input port, 104-liquid enzyme recovery port, 105-liquid enzyme circulation pipe, 106-first recovery pipe, 107-second recovery pipe, 108-third recovery pipe, 109-first recovery valve, 110-second recovery valve, 111-third recovery valve, 112-recovery pump, 201-sedimentation centrifuge, 202-buffer tank, 203-centrifugal liquid inlet pipe, 204-liquid inlet pump, 205-oil outlet pipe, 206-oil outlet valve, 301-drying condensing tower, 302-a dry packed bed, 303-a dry condenser, 304-a dry packing, 305-a first dry condensate guide plate, 306-a second dry condensate guide plate, 307-a dry condensate collection tank, 308-a dry heating feed pipe, 309-a dry feed pump, 310-a dry feed heater, 401-a distillation column, 402-a condensate buffer tank, 403-a distillation circulation pipe, 404-a distillation circulation pump, 405-a distillation circulation heater, 406-a distillation packed bed, 407-a distillation condenser, 408-a distilled heavy oil discharge pipe, 409-a distillation packing, 410-a first distillation condensate guide plate, 411-a second distillation condensate guide plate, 412-a distillation condensate collection tank, 413-a distilled heavy oil discharge pump, 414-distillation condensate discharge port, 415-condensed material discharge pipe, 416-condensate cooling heat exchanger, 417-distillation feed pipe, 418-drying discharge pump, 419-distillation feed heater, 501-water ring vacuum pump, 502-water storage tank, 503-spiral plate heat exchanger, 504-cold water tank, 505-first circulating water pump, 506-water inlet, 507-exhaust port, 509-first water inlet, 510-first water outlet, 511-suction port, 512-second water inlet, 513-second water outlet, 514-second circulating water pump, 515-first pipeline, 516-second pipeline, 517-drain pipe, 518-drain valve, 519-water inlet pipe, 520-water inlet valve, 521-water pump, 522-waste gas discharge port, 531-heat exchanger body, 532-first spiral heat exchange channel, 533-second spiral heat exchange channel, 601-immobilized enzyme reaction circulating pipe, 602-immobilized enzyme reaction circulating pump, 603-immobilized enzyme reaction discharging pipe, 604-immobilized enzyme reaction discharging pump, 605-immobilized lipase bed, 606-immobilized lipase, 607-immobilized enzyme feeding pipe, 608-immobilized enzyme feeding pump, 701-first settling tank, 702-second settling tank, 703-third settling tank, 704-first discharging pipe, 705-second discharging pipe, 706-third discharging pipe, 801-alkali liquor spray tower, 802-gas-liquid separation tower, 803-boiler, 804-blower, 805-alkali liquor circulating pipe, 806-alkali liquor circulating pump, 807-valve, 808-spray pipe, 809-spiral spray nozzle, 811-upper observation sight glass, 812-lower observation sight glass, 813-gas pipe, 814-observation sight glass, 815-liquid outlet, 816-gas exhaust pipe, 817-alkali liquor inlet, 818-alkali liquor outlet and 819-liquid discharge valve.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. 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 the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation or be constructed and operated in a particular orientation, and thus, it should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; of course, mechanical connection and electrical connection are also possible; in addition, they may be directly connected, indirectly connected through an intermediary, or may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
As shown in fig. 1-9, the system for producing biodiesel by using double enzymes provided by the present invention comprises a liquid enzyme reaction tank 1 for liquid lipase catalysis reaction, a separation mechanism 2 connected from the liquid enzyme reaction tank 1 for separating reaction products, a drying mechanism 3 connected from the separation mechanism 2 for drying and removing water from the separation product, a distillation mechanism 4 connected from the drying mechanism 3 for distillation and impurity removal of the separation product, a vacuum circulation cooling mechanism 5 respectively connected from the drying mechanism 3 and the distillation mechanism 4, and a solid enzyme reaction tank 6 connected from the distillation mechanism 4 for immobilized lipase catalysis reaction, wherein a continuous settling mechanism 7 for recycling liquid enzymes is arranged between the separation mechanism and the liquid enzyme reaction tank 1, a liquid enzyme circulation pipe 105 is connected between the continuous settling mechanism 7 and the liquid lipase reaction tank 1, and the vacuum circulation cooling mechanism 5 is connected with a tail gas treatment mechanism 8.
The invention provides a production method of a system for producing biodiesel by using double enzymes, which comprises the following steps:
s1, enabling waste gas animal and vegetable oil to enter a liquid enzyme reaction tank and hydrolyzing the waste gas animal and vegetable oil and methanol and water in the tank under the catalysis of liquid lipase to generate fatty acid methyl ester;
s2, separating solid-phase residues, a water-phase liquid enzyme aqueous solution and oil-phase mixed fatty acid from a mixture consisting of the product and the raw material in the step S1 in a separation mechanism;
s3, separating the aqueous phase liquid enzyme solution by a continuous settling mechanism to obtain liquid lipase, introducing the liquid lipase into a liquid enzyme reaction tank for recycling, and removing water and waste gas from the oil-phase mixed fatty acid in a drying mechanism;
s4, removing waste gas and heavy oil from the mixed fatty acid with water and gas removed in a distillation mechanism to obtain primary methyl ester;
s5, allowing the primary methyl ester to enter a solid enzyme reaction tank for secondary hydrolysis under the catalysis of immobilized lipase, so that residual free fatty acid in the primary methyl ester completely reacts with triglyceride to generate fatty acid methyl ester;
step S6, the waste gas removed in the step S3 and the step S4 enters a vacuum circulating cooling mechanism for water filtration and purification to obtain primary purified tail gas;
and S7, allowing the primarily purified tail gas to enter a tail gas treatment mechanism for saponification and purification, and finally using the primarily purified tail gas as fuel.
The production system is a double-enzyme (liquid lipase and immobilized lipase) double-hydrolysis system, so that the hydrolysis sufficiency of the waste animal and vegetable oil is ensured, and the conversion rate of the biodiesel is greatly improved; the production method is reasonably arranged according to a production system, and comprises liquid lipase catalytic reaction, solid, water and oil separation, oil phase drying, oil phase distillation and immobilized lipase catalytic reaction in sequence, so that the production of the biodiesel is more reasonable.
The waste animal and vegetable oil is hydrolyzed in the liquid enzyme reaction tank 1 by the catalysis of liquid lipase; separating solid-phase slag, a water-phase liquid enzyme water solution and oil-phase mixed fatty acid from the hydrolysis mixture in a decanter centrifuge 201 of a separation mechanism 2, wherein the oil-phase mixed fatty acid is subjected to dehydration and degassing by a drying mechanism 3 and reduced pressure degassing and impurity removal by a distillation mechanism 4 in sequence, reaches an immobilized lipase reaction tank 6, is hydrolyzed again under the catalysis of immobilized lipase in the immobilized lipase to obtain fatty acid methyl ester with extremely high content, namely biodiesel, and the biodiesel is dried to obtain a finished product; separating the liquid lipase which is not inactivated from the aqueous phase liquid enzyme solution by a continuous settling mechanism 7 and recycling the liquid lipase in the liquid enzyme reaction tank 1; the solid-phase residues (oil sludge and a small amount of grease) are adsorbed in the decanter centrifuge 201, the solid-phase residues are periodically cleaned, the solid-phase residues are extruded into blocks to manufacture fertilizers, and the extruded grease can also be used as fuels for producing boilers, so that the maximum utilization rate of byproducts is realized. In addition, the exhaust gas removed by the drying means 3 and the distillation means 4 is subjected to a harmless treatment by the exhaust gas treatment means 8.
The long-term production practice shows that the main reasons of inactivation failure of the immobilized lipase are that the quality of raw material oil is unstable, and the immobilized lipase is damaged by inorganic acid radical ions in waste oil and oil sludge and wrapped in the reaction process, so that the inactivation failure of the immobilized lipase is caused. And the analysis and detection of the material after the liquid lipase catalytic reaction show that the sum of the contents of the fatty acid methyl ester and the free fatty acid in the mixed product reaches or exceeds the national standard.
Therefore, the invention adjusts the prior process system, adjusts the distillation section which is traditionally arranged at the tail end to the middle section, and distills the liquid lipase reaction product before entering the immobilized lipase reaction. On one hand, the reaction mixture enters a distillation section after the liquid lipase reacts, substances harmful to the immobilized lipase are removed, and then the immobilized lipase catalytic reaction is carried out. Thus, the obtained distillation condensate only contains a small amount of triglyceride without affecting the quality except for the vast majority of fatty acid methyl ester and a small portion of free fatty acid, and the fatty acid methyl ester, the free fatty acid and the triglyceride carried out by distillation have no obvious harmful effect on the immobilized lipase and have relatively stable composition. The activity of the immobilized lipase can reach normal attenuation speed in the material after pre-distillation, the use batch completely meets the requirements, the risk of accidental inactivation and invalidation of the immobilized lipase is almost negligible, and the use batch of the immobilized lipase is greatly improved (the immobilized lipase can be stabilized for more than 300 batches through the distillation material, and generally only about 70 batches are used without distillation before, and the risk of accidental inactivation and invalidation is often generated), so that the cost of the immobilized lipase of the biological enzyme method process is reduced by about 25 percent of the original cost. On the other hand, the distillation working section is arranged in front, so that the phenomenon that the acid value of the material is increased again and exceeds the standard due to cracking caused by high temperature generated by the final distillation of the material is effectively avoided, and the stability of the acid value of the product is ensured.
The distillation section is the distillation mechanism 4 and comprises a distillation tower 401 connected from a drying condensation tower 301 and a condensed material buffer tank 402 connected from the distillation tower 401 and connected into a immobilized enzyme reaction tank 6, the distillation tower 401 is provided with a distillation circulating pipe 403 connected from the bottom of the distillation tower 401 and connected into the middle of the distillation tower 401, the distillation circulating pipe 403 is provided with a distillation circulating pump 404 and a distillation circulating heater 405, the middle of the distillation tower 401 is provided with a distillation packing bed 406, the upper part of the distillation tower 401 is provided with a distillation condenser 407, the bottom of the distillation tower is connected with a distilled heavy oil discharge pipe 408 connected into the distilled heavy oil treatment section, the distillation packing bed 406 is internally provided with distillation packing 409, the distillation condenser 407 is provided with a first distillation condensate guide plate 410 and a second distillation condensate guide plate 411, the second distillation condensate guide plate 411 is provided with a distillation condensate collecting tank 412, the distillation heavy oil discharge pipe 408 is provided with a distillation heavy oil discharge pump 413, the distillation condensate collecting tank 412 is provided with a distillation discharge outlet 414, a condensed material discharge pipe 415 is connected between the distillation condensate discharging outlet 414 and the condensed material buffer tank 402, and the condensed material discharge pipe 415 is provided with a condensate cooling heat exchanger 416; a distillation feed pipe 417 is connected between the drying condensation tower 301 and the distillation tower 401, and a drying discharge pump 418 and a distillation feed heater 419 are arranged on the distillation feed pipe 417.
The desired oil-phase fatty acid mixture separated in the separation means 2 is dehydrated and degassed in the drying means 3, heated to steam by the distillation feed heater 419 and supplied to the distillation column 401, and the components of the fatty acid mixture are separated in the distillation column 401 due to the difference in boiling point and specific gravity. Wherein heavy oil (plant pitch or black foot) having toxicity to immobilized lipase is condensed first and falls into the bottom of the distillation tower 401 when the specific gravity is high; whereas the desired fatty acid methyl esters, free fatty acids and triglycerides are slowly condensed and finally condensed in the top distillation condenser 407. In order to effectively separate the two, the first distillation condensate guide plate 410 and the second distillation condensate guide plate 411 guide the condensed required fatty acid methyl ester to the distillation condensate collecting tank 412, and the condensed fatty acid methyl ester enters the re-condensation through the distillation condensate discharging port 414 to be buffered in the condensed material buffer tank 402 for the next working condition, and the heavy oil and the like are discharged through the distillation heavy oil discharging pipe 408. In order to achieve sufficient distillation and increase the distillation rate of fatty acid methyl ester and the like, the distillation circulation pipe 403 may circulate and distill the condensate until all or most of the desired fatty acid methyl ester and the like are separated.
The fatty acid methyl ester and the like, i.e. the primary methyl ester, from which the substances such as heavy oil and the like are removed enter the solid enzyme reaction tank 6 to carry out the re-hydrolysis reaction of the immobilized lipase, in order to ensure the complete hydrolysis, a solid enzyme reaction circulating pipe 601 which is connected out from the bottom of the solid enzyme reaction tank 6 and is connected to the top of the solid enzyme reaction tank 6 is arranged on the enzyme reaction tank 6, and a solid enzyme reaction circulating pump 602 is arranged on the solid enzyme reaction circulating pipe 601. The reaction mixture may be repeatedly hydrolyzed by the immobilized enzyme reaction circulation tube 601 to increase the conversion rate of fatty acid methyl ester.
Before distillation, the drying mechanism 3 is needed to remove the gas and water from the oil phase mixed fatty acid after the liquid enzyme reaction. The drying mechanism 3 comprises a drying condensing tower 301 connected out of the cache tank 202, a drying packed bed 302 is arranged in the middle of the drying condensing tower 301, a drying condenser 303 is arranged on the upper portion of the drying condensing tower 301, a drying packing 304 is arranged in the drying packed bed 302, a first drying condensate guide plate 305 and a second drying condensate guide plate 306 are arranged below the drying condenser 303, and a drying condensate collecting tank 307 is arranged below the second drying condensate guide plate 306. A drying and heating feed pipe 308 is connected between the buffer tank 202 and the drying and condensing tower 301, and a drying and feeding pump 309 and a drying and feeding heater 310 are arranged on the drying and heating feed pipe 308. The oil phase mixed fatty acid is heated by the dry feed heater 310 to a mixed vapor, separation is achieved due to the difference in boiling points of the oil and water, and the waste gas is mostly separated at this stage.
In the production of biological enzyme, especially lipase, the consumption of liquid lipase (or liquid enzyme for short) is large, generally more than 0.3%, and the recovery and utilization rate of liquid enzyme is low, which results in high cost of liquid enzyme. Therefore, the invention adopts the continuous sedimentation mechanism to separate and recycle the liquid enzyme, and the recycled liquid enzyme can be put into the liquid lipase reaction tank for recycling, so as to achieve the purpose of greatly reducing the cost of the liquid lipase. In the practice of producing biodiesel by using an enzymatic process for a long time, it is found that most of the reacted liquid lipase floats on the surface of the water phase separated by the decanter centrifuge 201 in an emulsified state, and therefore, the continuous sedimentation mechanism adopts a method of high liquid level maintenance and bottom drainage to separate the liquid lipase which is not inactivated for multiple times for recycling, thereby achieving the purpose of reducing the newly added liquid lipase. Therefore, the use amount of the liquid lipase in the process of producing the biodiesel by the biological enzyme method is reduced, so that the aim of greatly reducing the cost of producing the liquid lipase by the biological enzyme method is fulfilled.
The liquid enzyme reaction mixture is separated by a decanter centrifuge 201 to obtain a water phase, i.e. a heavy phase liquid, which contains glycerol, methanol, water and a small amount of liquid enzyme. Because most of the liquid lipase floats on the surface of the heavy phase liquid in an emulsified state, if the bottom liquid and the middle-upper liquid of the heavy phase liquid are continuously separated, liquid containing a large amount of liquid lipase can be obtained, and pure liquid lipase liquid can be obtained after multiple times of separation.
The continuous sedimentation mechanism comprises a first sedimentation tank 701 connected with the sedimentation centrifuge 201 in water phase, the upper part of the first sedimentation tank 701 is connected with a first recovery pipe 106, and the first recovery pipe 106 is connected with a liquid enzyme circulating pipe 105. According to the method, liquid lipase floats on the surface of heavy phase liquid in an emulsified state, most of the liquid lipase exists at the upper part of the first settling tank 701, so that the liquid at the upper part of the first settling tank 701 is recycled to the liquid lipase reaction tank 1, and the reuse of the liquid lipase which is not inactivated is realized. As the liquid at the lower part of the first settling tank 701 also contains a small amount of liquid enzyme, in order to ensure that the recovery rate of the liquid enzyme is improved, the continuous settling mechanism also comprises a second settling tank 702 connected from the first settling tank 701, the upper part of the second settling tank 702 is connected with a second recovery pipe 107, and the second recovery pipe 107 is connected with the liquid enzyme circulating pipe 105. In this manner, the second settling tank 702 can achieve secondary recovery of liquid enzyme. Similarly, the liquid at the lower part of the second settling tank 702 also contains a small amount of liquid enzyme, the continuous settling mechanism also comprises a third settling tank 703 connected from the second settling tank 702, the upper part of the third settling tank 703 is connected with a third recovery pipe 108, and the third recovery pipe 108 is connected with the liquid enzyme circulating pipe 105. In this way, the third settling tank 703 can achieve three recoveries of liquid enzyme. Each settling tank is beneficial to the timely participation of the liquid enzyme recovered from each section in the subsequent catalytic reaction, thereby greatly reducing the amount of newly added liquid lipase and lowering the production cost. Wherein, the number of the settling tanks is set according to the actual situation.
A first discharge pipe 704 is connected between the first settling tank 701 and the second settling tank 702, a second discharge pipe 705 is connected between the second settling tank 702 and the third settling tank 703, and a third discharge pipe 706 is connected to the third settling tank 703. Preferably, a first discharge pipe 704 extends from the bottom of the first settling tank 701 to the middle upper part of the second settling tank 702, and a second discharge pipe 705 extends from the bottom of the second settling tank 702 to the middle upper part of the third settling tank 703. According to the siphon drainage principle, the heavy phase liquid continuously enters each settling tank, the liquid level of the heavy phase liquid continuously rises, and at the moment, the mixture of glycerol, methanol, water and the like at the bottom of the heavy phase liquid overflows into the next settling tank through each discharge pipe, so that separation is realized.
The lower liquids of the first settling tank 701, the second settling tank 702 and the third settling tank 703 are separated again through a first discharge pipe 704, a second discharge pipe 705 and a third discharge pipe 706, respectively. Preferably, the first discharging pipe 704 extends from the bottom of the first settling tank 701 to the middle upper part of the second settling tank 702, the second discharging pipe 705 extends from the bottom of the second settling tank 702 to the middle upper part of the third settling tank 703, and most of the glycerol, methanol and water which are separated for many times are discharged to a wastewater treatment section through the third discharging pipe 706 for subsequent treatment. Preferably, the nozzle of each discharge pipe is about 15 to 20cm from the bottom of each settling tank. A first recovery valve 109 is arranged on the first recovery pipe 106, a second recovery valve 110 is arranged on the second recovery pipe 107, a third recovery valve 111 is arranged on the third recovery pipe 108, and the first recovery valve 109, the second recovery valve 110 and the third recovery valve 111 are preferably one-way throttle valves. The liquid enzyme circulating pipe 105 is provided with a recovery pump 112, and the recovery pump 112 is convenient for pumping out liquid containing liquid enzyme at the upper part of each settling tank.
A centrifugal liquid inlet pipe 203 is connected between the liquid lipase reaction tank 1 and the sedimentation type centrifuge 201, and a liquid inlet pump 204 is arranged on the centrifugal liquid inlet pipe 203. A water outlet pipe 707 is arranged between the water port of the decanter centrifuge 201 and the first settling tank 701, and a water outlet valve 708 is arranged on the water outlet pipe 707. An oil outlet pipe 205 is arranged between the oil port of the decanter centrifuge 201 and the buffer tank 202, and an oil outlet valve 206 is arranged on the oil outlet pipe 205. Decanter centrifuge 201 is preferably a horizontal decanter centrifuge, and outlet valve 708 and outlet valve 206 are preferably solenoid valves. Solid-phase slag substances centrifuged in the decanter centrifuge 201 by the mixture after the catalytic reaction are attached to the decanter centrifuge 201, the solid-phase slag substances are periodically cleaned, and the solid-phase slag substances are extruded into blocks to be made into fertilizer; because a small amount of grease is adsorbed in the solid-phase slag, the solid-phase slag can also be used as fuel for producing boilers, and the maximum utilization rate of byproducts is realized.
In the existing preparation process of the biodiesel by the enzyme method, a water ring vacuum pump is usually used for pumping out waste gas in a drying tower and a distillation tower so as to carry out vacuum drying on the biodiesel inside. Because the exhaust gas temperature that takes out is high, and the water ring vacuum pump is when the extraction, and the temperature constantly risees, and too high temperature can make water ring vacuum pump air exhaust ability decline and can't reach the production demand, consequently need constantly change water for water ring vacuum pump, and the water consumption is huge. Therefore, the vacuum circulating cooling mechanism 5 is adopted to condense and cool the circulating water, the working water temperature of the water ring vacuum pump is ensured to be at the proper working temperature in real time, the use of the water ring vacuum pump caused by overhigh water temperature in the water ring of the water ring vacuum pump can be effectively avoided, and the water in the water storage tank can be effectively used for providing the circulating water for the water ring vacuum pump.
The vacuum circulating cooling mechanism 5 comprises a water ring vacuum pump 501 respectively connected with the tops of the drying and condensing tower 302 and the distillation tower 402 through pipelines, a water storage tank 502 connected with the water ring vacuum pump 501 and used for providing circulating water for the water storage tank, and a condensing mechanism connected with the water storage tank 502 and used for cooling the circulating water in the water storage tank. The water storage tank 502 is added on the basis of the use of the water ring vacuum pump 501, so that the water in the water ring vacuum pump 501 can be recycled. And a circulating water condensing mechanism is added on the basis of the use of the water storage tank 502 to cool the water in the water storage tank 502, reduce the temperature of the working water of the water ring vacuum pump 501 and ensure the normal air pumping capacity of the water ring vacuum pump 501. The volume of the water storage tank 502 is preferably 1 cubic, the water storage tank can be recycled for one week, the water consumption which needs 200 tons every week is reduced to 1 ton, a large amount of water resources are saved, meanwhile, the sewage discharge treatment which needs 200 tons every week is reduced to 1 ton every week, and the sewage treatment cost is effectively saved.
The water ring vacuum pump 501 is provided with an air suction port 511 and an air exhaust port 507, the water storage tank 502 is provided with a first water inlet 509, a first water outlet 510 and an exhaust gas outlet 522, the water ring vacuum pump 501 is provided with a water inlet 506 communicated with a water ring of the water ring vacuum pump 501, the first water inlet 509 is connected with the air exhaust port 507 of the water ring vacuum pump 501 through a pipeline, and the first water outlet 510 is connected with a water inlet of the water ring vacuum pump 501. In this way, water is circulated between the water storage tank 502 and the water ring vacuum pump 501. The exhaust gas pumped out from the drying condensing tower 301 or the distillation tower 401 by the water ring vacuum pump 501 is discharged from an exhaust port 507 of the water ring vacuum pump and is discharged into the water storage tank 502 through a first water inlet 509 connected to the exhaust port 507. The exhaust gas entering the water storage tank 502, including the water carried by it, is separated from the gas and liquid within the water storage tank 502. The separated water is directly left in the water storage tank 502 for recycling by the water ring vacuum pump 501. And the gas is discharged from the water storage tank 502 and enters the next waste gas harmless treatment section. When the water storage tank 502 supplies water to the water ring vacuum pump, the water is discharged from the first water outlet 510 and enters the water ring vacuum pump 501 through the water inlet 506 connected to the first water outlet 510. The volume of the water storage tank is 1m 3 The water demand of the water ring vacuum pump 501 is met, and meanwhile, the cost and the waste water resource caused by the selection of the water storage tank 502 with the overlarge model are reduced. The waste gas outlet 522 is connected with a waste gas outlet pipe, and waste gas pumped by the water ring vacuum pump passes through wasteThe exhaust outlet 522 and the exhaust gas outlet are externally discharged to the tail gas treatment mechanism 8 for the harmless treatment of the exhaust gas.
The condensing mechanism comprises a spiral plate type heat exchanger 503 connected with a water storage tank 502, a first circulating water pump 505 connected between the water storage tank 502 and the spiral plate type heat exchanger 503, and a cold water tank 504 connected with the spiral plate type heat exchanger 503. In this way, when the water in the water storage tank 502 is cooled, the water in the water storage tank 502 is discharged into the spiral plate heat exchanger 503 by the first circulating water pump 505, and exchanges heat with the cold water provided by the cold water tank 504 in the spiral plate heat exchanger 503, thereby achieving the purpose of reducing the temperature of the water in the water storage tank 502. The water in the water storage tank 502 is cooled and then is supplied to the water ring vacuum pump 501 for use, so that the normal air extraction capacity of the water ring vacuum pump 501 is ensured.
The spiral plate type heat exchanger 503 comprises a heat exchanger main body 531, and a first spiral heat exchange channel 532 and a second spiral heat exchange channel 533 which are arranged in the heat exchanger main body 531, wherein the water storage tank 502 is connected with the first spiral heat exchange channel 532, and the cold water tank 504 is connected with the second spiral heat exchange channel 533. Therefore, when the water in the water storage tank 502 and the water in the cold water tank 504 exchange heat in the spiral plate type heat exchanger 503, the water respectively flows in two spiral channels formed by rolling two parallel steel plates, and the heat exchange can be carried out without mutual interference. The first spiral heat exchange channel 532 and the second spiral heat exchange channel 533 are separated by the heat exchange plates, the two channels are distributed at intervals, the water inlet and outlet of the first spiral heat exchange channel 532 are distributed at two ends of the heat exchanger body 531, each flow channel in the first spiral heat exchange channel 532 is communicated through the water inlet and outlet of the first spiral heat exchange channel 532, the water inlet and outlet of the second spiral heat exchange channel 533 is distributed at two ends of the heat exchanger body 531, and each flow channel in the second spiral heat exchange channel 533 is communicated through the water inlet and outlet of the second spiral heat exchange channel 533.
The water storage tank 502 is provided with a second water inlet 512 and a second water outlet 513, the second water inlet 512 is connected with the water outlet of the first spiral heat exchange channel 532 through a first pipeline 515, and the second water outlet 513 is connected with the water inlet of the first spiral heat exchange channel 532 through a second pipeline 516. The design is such that water in the water storage tank 502 can enter the spiral plate type heat exchanger 503 for heat exchange. The water is discharged from the second water outlet 513, is conveyed by the second pipe 516, enters the first spiral heat exchange channel 532 from the water inlet of the first spiral heat exchange channel 532, and exchanges heat with the cooling water in the second spiral heat exchange channel 533 in the spiral plate type heat exchanger 503.
The first circulating water pump 505 is arranged on the second pipeline 516. Therefore, the water in the water storage tank 522 can smoothly enter the first spiral channel 532 of the spiral plate heat exchanger 503 to achieve the purpose of exchanging heat with the cooling water in the second spiral heat exchange channel 533. Under the action of the first water circulating pump 505, the water in the water storage tank is conveyed by the second pipe 516, and enters the first spiral heat exchange channel 532 to exchange heat with the cooling water in the second spiral heat exchange channel 533, so that the temperature of the water in the water storage tank 502 is reduced.
And a drain pipe 517 is connected to the second pipeline 516, the drain pipe 517 is connected between the first circulating water pump 505 and the first spiral heat exchange channel 532, a drain valve 518 is arranged on the drain pipe 517, and the drain pipe 517 is connected to a sewage treatment section. When the water in the water storage tank 502 is polluted seriously and needs to be replaced due to repeated use, the sewage in the water storage tank can be smoothly drained. And opening a drain valve 518 on the drain pipe 517 to discharge the sewage in the water storage tank from the second water outlet 513, and discharging the sewage from the drain pipe 517 after conveying the sewage to the joint of the second pipeline 516 and the drain pipe 517 under the action of the first circulating water pump 505, thereby achieving the purpose of draining the sewage in the water storage tank.
The first pipeline 515 is connected with a water inlet pipe 519, the water inlet pipe 519 is connected out from the bottom in the cold water tank 504, and a water inlet valve 520 and a water pump 521 are arranged on the water inlet pipe 519. Therefore, the water storage tank 502 can be used for smoothly supplementing water when sewage in the water storage tank is emptied and water needs to be supplemented. The water inlet valve 520 on the water inlet pipe 519 is opened, water flows out from the bottom of the cold water tank 504 under the action of the water pump 521, flows to the joint of the water inlet pipe 519 and the first pipeline 515, is conveyed to the second water inlet 512 through the first pipeline 515, and enters the water storage tank 502 from the second water inlet 512, so that the purpose of supplementing enough water to the water storage tank 502 is achieved. The cold water tank 504 is connected with a water replenishing pipe, and the water replenishing pipe is directly connected with a tap water pipe and used for replenishing water to the cold water tank 504.
The water inlet and the water outlet of the second spiral heat exchange channel 533 are respectively connected with the inner bottom and the inner top of the cold water tank 504 through pipes. Therefore, cold water in the cold water tank 504 can enter the second spiral heat exchange channel 533, which is beneficial for the water in the water storage tank 502 to exchange heat with the cold water in the second spiral heat exchange channel 533 after entering the first spiral heat exchange channel 532. Cold water flows out from the bottom in the cold water tank 5044, enters the second spiral heat exchange channel 533 through the water inlet of the second spiral heat exchange channel 533, and therefore the purpose that water entering the water storage tank 502 of the first spiral heat exchange channel 532 can exchange heat with the cold water in the second spiral heat exchange channel 533 is achieved.
A second circulating water pump 514 is arranged on a pipeline connecting the water inlet of the second spiral heat exchange channel 533 and the bottom in the cold water tank 504. In this way, the second circulating water pump 514 pumps the cold water in the cold water tank 504 into the second spiral heat exchange channel 533. The cold water in the cold water tank 504 flows out from the bottom in the cold water tank under the action of the second circulating water pump 514, smoothly enters the second spiral heat exchange channel 533 through the water inlet of the second spiral heat exchange channel 533 and then returns to the cold water tank 504, the volume of the cold water tank 504 is more than twenty times of the volume of the water storage tank 502, and thus the circulating water in the water storage tank 502 can be effectively cooled.
The tail gas condensed and removed by the vacuum circulating cooling mechanism 5 to remove water-soluble harmful substances still has strong irritating malodorous gas, and is generally treated by a biological deodorization method, but the treatment effect often does not meet the emission requirement. Therefore, the tail gas treatment mechanism 8 is adopted, the targeted liquid is adopted to spray based on tail gas components, and then the sprayed liquid is subjected to gas-liquid separation and introduced into the boiler for high-temperature incineration to meet the emission requirement, a smell treatment device is not required to be built, a large amount of investment and operation cost are saved, and the purposes of environmental protection and energy saving can be effectively achieved.
The tail gas treatment mechanism 8 comprises an alkali liquor spray tower 801 connected out from a waste gas outer discharge port 522 of the water storage tank 502 through a pipeline and used for tail gas purification, a gas-liquid separation tower 802 connected out from the alkali liquor spray tower 801 and used for purified tail gas separation, and a boiler 803 arranged beside the gas-liquid separation tower 802 and used for performing harmless treatment on purified gas, wherein a circulating spray device used for recycling alkali liquor is arranged on the alkali liquor spray tower 801, and a blower 804 used for pumping purified tail gas is arranged on the boiler 803.
Since the distillate of the biodiesel distillation is basically fatty acid or fatty acid methyl ester with different carbon chains, the main components which are required and can be condensed in the distillation tower or a condenser arranged in front of a vacuum pump are 18-carbon methyl ester, 16-carbon methyl ester and part of 14-carbon methyl ester, and the part of 14-carbon methyl ester and lower carbon chain fatty acid or fatty acid methyl ester are pumped by the vacuum pump of the vacuum cooling device, so that the gas odor components pumped out in vacuum are basically fatty acid and fatty acid methyl ester. According to the principle that fatty acid and fatty acid methyl ester can be saponified with alkali and can be combusted to generate heat energy, tail gas after vacuum cooling treatment is introduced into an alkali liquor spray tower 801 to carry out saponification acid-base neutralization reaction, so that tail gas purification is realized, and purified gas is separated by a gas-liquid separation tower 802 and is finally introduced into a boiler 803 to be used as fuel for burning. The distillation tail gas can completely reach the tail gas emission standard through double treatment of saponification and combustion, so that the environment is protected, and the treated tail gas is used as fuel for secondary production, so that the energy conservation and emission reduction are realized.
The circulating spray device comprises an alkali liquor circulating pipe 805 connected from the alkali liquor spray tower 801 and a circulating spray mechanism connected with the alkali liquor circulating pipe 805 and extending into the alkali liquor spray tower 801 for spraying alkali liquor on the distillation tail gas, wherein an alkali liquor circulating pump 806 and a valve 807 are arranged on the alkali liquor circulating pipe 805. The exhaust port at the top of the distillation tower is connected to the middle lower part of the alkali liquor spray tower 801 through a pipeline, a proper amount of prepared alkali water is injected into the alkali liquor spray tower 801, the alkali water is preferably sodium hydroxide aqueous solution with the concentration of about 5%, so that tail gas entering the alkali liquor spray tower 801 from the middle lower part can be sprayed by the alkali water to remove acidic harmful substances in the tail gas, little malodorous gas is discharged after spraying, and the exhaust port effectively reaches the emission standard. The circulating spraying mechanisms are at least two, and comprise a spraying pipe 808 connected from the alkali liquor circulating pipe 805 and a spiral spraying nozzle 809 arranged on the spraying pipe 808. The alkaline water is sprayed out through the spiral spray nozzle 809 and is in a large-area water mist shape, so that the contact area between the waste gas and the alkaline liquid is increased. When the circulating spraying mechanism is provided with a plurality of circulating spraying mechanisms, the spiral spraying nozzles 809 of the circulating spraying mechanisms are distributed in an up-and-down opposite mode. The size and the height of the alkali liquor spray tower 801, the number of the spray pipes 808 and the spiral spray nozzles 809 are determined according to the exhaust gas volume. The sprayed alkaline water falls into the bottom of the alkaline liquid spray tower 801 and is pumped into the spiral spray nozzle 809 at the upper part of the alkaline liquid spray tower 801 again through the alkaline liquid circulating pipe 805 and the alkaline liquid circulating pump 806, and the alkaline water can be recycled for multiple times, so that the usage amount of the alkaline water is greatly reduced, and the full effect of the alkaline water is ensured.
The soap liquid produced after saponification reaction is located at the upper part of the alkali liquor, and if the alkali liquor is completely reacted, the soap liquid is turbid. In order to add alkali liquor in time, the middle lower part of the alkali liquor spray tower 801 is provided with an upper observation sight glass 811 for observing reaction soap liquor, and the lower part of the alkali liquor spray tower 801 is provided with a lower observation sight glass 812 for observing alkali liquor, so that the condition of the liquid in the alkali liquor can be observed in time. The upper part of the alkali liquor spray tower 801 is provided with an alkali liquor inlet 817, the bottom part is provided with an alkali liquor outlet 818, and the alkali liquor outlet 812 is provided with a liquid discharge valve 819. The added alkali liquor is supplemented by an alkali liquor inlet 817, and the liquid completely reacted is discharged by an alkali liquor outlet 818. The bottom of the alkali liquor spray tower 801 is preferably provided with a bucket-mounted structure, so that the alkali liquor can be recycled and discharged.
An air pipe 813 is connected between the alkali liquor spray tower 801 and the gas-liquid separation tower 802, and the air pipe 813 is connected from the top of the alkali liquor spray tower 801 and is connected to the lower part of the gas-liquid separation tower 802. The gas after saponification reaction carries a large amount of liquid, and therefore, the moisture in the gas needs to be removed, so that the purified gas enters the gas-liquid separation tower 2 from the alkali liquor spray tower 801, and the purified gas completes the water removal in the gas-liquid separation tower 802 from bottom to top. The liquid separated from the gas and the liquid is stored at the bottom of the gas-liquid separation tower 802, an observation sight glass 814 for observing the separated liquid is arranged at the middle lower part of the gas-liquid separation tower 802, a liquid discharge port 815 is arranged at the bottom of the gas-liquid separation tower 802, the observation sight glass 814 is convenient for observing the liquid level of the waste lye at the bottom, and the liquid discharge port 815 is convenient for discharging the waste lye. The liquid outlet 815 is connected with the waste liquid treatment section through a pipeline, so that the waste alkali liquid is guided into the waste liquid treatment section for harmless treatment.
The distillation waste gas is neutralized by the saponification acid-base to remove most harmful foul gas in the distillation waste gas, reaches the emission standard, and can be directly discharged from an exhaust pipe 816 connected to the top of the gas-liquid separation tower 802. In order to avoid the condition of incomplete acid-base neutralization when a large amount of distillation tail gas is discharged, the purified tail gas is finally used as boiler fuel, so that the absolute green is realized, and the energy consumption is greatly saved. The top of the gas-liquid separation tower 802 is connected with an exhaust pipe 816, the gas outlet of the exhaust pipe 816 is opposite to the gas inlet of the blower 804, purified tail gas is introduced into the boiler 803 to be incinerated under the negative pressure condition of the gas inlet of the blower 804, and the distance between the gas outlet of the exhaust pipe 816 and the gas inlet of the blower 804 is at least 2 meters. The boiler 803 is the existing boiler of the biodiesel production system, and the boiler 803 can also be replaced by the existing boiler heat-conducting oil furnace of the biodiesel production system, and the purified tail gas is introduced into the heat-conducting oil furnace for incineration.
The decanter centrifuge 201, the drying condenser 303, the drying feed pump 309, the drying feed heater 310, the drying feed heater 404, the distillation circulation heater 405, the distillation condenser 407, the distilled heavy oil discharge pump 413, the condensate cooling heat exchanger 416, the drying discharge pump 418, the distillation feed heater 419, the water ring vacuum pump 501, the drying discharge pump 505, the second circulation water pump 514, the immobilized enzyme reaction circulation pump 602, the immobilized enzyme reaction discharge pump 604, the gas-liquid separation tower 802, the blower 804, the alkali liquor circulation pump 806, the first spiral spray nozzle 809 and the second spiral spray nozzle 810 used in the present invention are all known electrical equipment, and can be purchased and used directly in the market, and the structure, the circuit and the control principle thereof are known technologies, therefore, the structure, the circuit and the control principle of the above devices are not described herein again.
Finally, it should be noted that: the above embodiments are only preferred embodiments of the present invention to illustrate the technical solutions of the present invention, but not to limit the technical solutions, and certainly not to limit the patent scope of the present invention; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention; that is, the technical problems to be solved by the present invention are still consistent with the present invention, and all the modifications or changes made without substantial meaning in the spirit and scope of the present invention should be included in the protection scope of the present invention; in addition, the technical scheme of the invention is directly or indirectly applied to other related technical fields, and the technical scheme is included in the patent protection scope of the invention.

Claims (10)

1. The system for producing the biodiesel by using the double enzymes is characterized by comprising a liquid enzyme reaction tank (1) for liquid lipase catalytic reaction, a separation mechanism (2) for separating reaction products is connected out from the liquid enzyme reaction tank (1), a drying mechanism (3) for drying and removing water from the separation mechanism (2) is connected out, a distillation mechanism (4) for distilling and removing impurities from the separation products is connected out from the drying mechanism (3), a vacuum circulating cooling mechanism (5) is respectively connected out from the drying mechanism (3) and the distillation mechanism (4), and a solid enzyme reaction tank (6) for immobilized lipase catalytic reaction is connected out from the distillation mechanism (4), a continuous settling mechanism (7) for recycling the liquid enzymes is arranged between the separation mechanism and the liquid enzyme reaction tank (1), a liquid enzyme circulating pipe (105) is connected between the continuous settling mechanism (7) and the liquid lipase reaction tank (1), and a tail gas treatment mechanism (8) is connected to the vacuum circulating cooling mechanism (5).
2. The system for producing biodiesel by using double enzymes according to claim 1, wherein the separation mechanism (2) comprises a decanter centrifuge (201) for separating oil phase, water phase and solid phase of the reaction product which is connected out of the liquid enzyme reaction tank (1), and a buffer tank (202) for storing fatty acid methyl ester of the oil phase which is connected out of the decanter centrifuge (201); a centrifugal liquid inlet pipe (203) is connected between the liquid enzyme reaction tank (1) and the decanter centrifuge (201), a liquid inlet pump (204) is arranged on the centrifugal liquid inlet pipe (203), an oil outlet pipe (205) is arranged between an oil port of the decanter centrifuge (201) and the buffer tank (202), and an oil outlet valve (206) is arranged on the oil outlet pipe (205).
3. The system for producing biodiesel by using double enzymes according to claim 2, wherein the continuous settling mechanism (7) comprises a first settling tank (701) connected with a water phase outlet of the decanter centrifuge (201), a first recovery pipe (106) is connected to the upper part of the first settling tank (701), and the first recovery pipe (106) is connected with the liquid enzyme circulating pipe (105);
the continuous sedimentation mechanism also comprises a second sedimentation tank (702) connected from the first sedimentation tank (701), the upper part of the second sedimentation tank (702) is connected with a second recovery pipe (107), and the second recovery pipe (107) is connected with the liquid enzyme circulating pipe (105);
the continuous sedimentation mechanism also comprises a third sedimentation tank (703) connected from the second sedimentation tank (702), the upper part of the third sedimentation tank (703) is connected with a third recovery pipe (108), and the third recovery pipe (108) is connected with the liquid enzyme circulating pipe (105);
a first material discharge pipe (704) is connected between the first settling tank (701) and the second settling tank (702), a second material discharge pipe (705) is connected between the second settling tank (702) and the third settling tank (703), and the third settling tank (703) is connected with a third material discharge pipe (706);
a first recovery valve (109), a second recovery valve (110) and a third recovery valve (111) are respectively arranged on the first recovery pipe (106), the second recovery pipe (107) and the third recovery pipe (108), and a recovery pump (112) is arranged on the liquid enzyme circulating pipe (105);
the liquid lipase reaction tank (1) is provided with a grease input port (101), a methanol input port (102), a liquid enzyme input port (103) and a liquid enzyme recovery port (104), a liquid enzyme circulating pipe (105) is connected with the liquid enzyme recovery port (104), a water outlet pipe (707) is arranged between a water phase outlet of the decanter centrifuge (201) and the first settling tank (701), and a water outlet valve (708) is arranged on the water outlet pipe (707).
4. The system for producing biodiesel by using double enzymes according to claim 2, wherein the drying mechanism (3) comprises a drying condensing tower (301) connected from the buffer tank (202), a drying packed bed (302) is arranged in the middle of the drying condensing tower (301), a drying condenser (303) is arranged at the upper part of the drying condensing tower (301), a drying filler (304) is arranged in the drying packed bed (302), a first drying condensate guide plate (305) and a second drying condensate guide plate (306) are arranged below the drying condenser (303), and a drying condensate collecting tank (307) is arranged below the second drying condensate guide plate (306);
a drying and heating feeding pipe (308) is connected between the buffer tank (202) and the drying and condensing tower (301), and a drying and feeding pump (309) and a drying and feeding heater (310) are arranged on the drying and heating feeding pipe (308).
5. The system for producing biodiesel by using double enzymes according to claim 4, wherein the distillation mechanism (4) comprises a distillation tower (401) connected from the drying and condensing tower (301) and a condensed material buffer tank (402) connected from the distillation tower (401) and connected to the immobilized enzyme reaction tank (6), the distillation tower (401) is provided with a distillation circulating pipe (403) connected from the bottom of the distillation tower (401) and connected to the middle of the distillation tower (401), the distillation circulating pipe (403) is provided with a distillation circulating pump (404) and a distillation circulating heater (405), the distillation tower (401) is provided with a distillation packing bed (406) in the middle, the distillation condenser (407) is arranged at the upper part, the bottom is connected with a distilled heavy oil discharge pipe (408) connected to a distilled heavy oil treatment section, the distillation packing (406) is provided with distillation packing (406), a first distillation condensate guide plate (410) and a second distillation condensate guide plate (411) are arranged below the distillation condenser (407), a distillation condensate collection tank (411) is arranged below the second distillation condensate collection tank (411), the distillation heavy oil discharge pipe (408) is provided with a distillation condensate discharge outlet (413), the distillation condensate collection tank (412) is provided with a distillation condensate discharge outlet (415), and a condensate discharge tank (414) is connected between the distillation condensate discharge outlet (414), a condensate cooling heat exchanger (416) is arranged on the condensed material discharge pipe (415);
a distillation feed pipe (417) is connected between the drying condensation tower (301) and the distillation tower (401), and a drying discharge pump (418) and a distillation feed heater (419) are arranged on the distillation feed pipe (417).
6. The system for producing biodiesel by using double enzymes according to claim 5, wherein a solid enzyme reaction circulating pipe (601) which is connected out from the bottom of the solid enzyme reaction tank (6) and connected to the top of the solid enzyme reaction tank (6) is arranged on the solid enzyme reaction tank (6), a solid enzyme reaction circulating pump (602) is arranged on the solid enzyme reaction circulating pipe (601), a solid enzyme reaction discharging pipe (603) which is connected to a finished product drying section is arranged at the middle lower part of the solid enzyme reaction tank (6), a solid enzyme reaction discharging pump (604) is arranged on the solid enzyme reaction discharging pipe (603), an immobilized lipase bed (605) is arranged in the condensed material cache tank (403), an immobilized lipase (606) is arranged in the immobilized lipase bed (605), a solid enzyme feeding pipe (607) is connected in front of the condensed material cache tank (403) and the solid enzyme reaction tank (6), and a solid enzyme feeding pump (608) is arranged on the solid enzyme feeding pipe (607).
7. The system for producing biodiesel by using double enzymes according to claim 5, wherein the vacuum circulating cooling mechanism (5) comprises a water ring vacuum pump (501) connected with the tops of the drying and condensing tower (302) and the distillation tower (402) through pipelines, a water storage tank (502) connected with the water ring vacuum pump (501) for providing circulating water for the water storage tank, and a condensing mechanism connected with the water storage tank (502) for cooling the circulating water in the water storage tank;
the water ring vacuum pump (501) is provided with an air suction port (511) and an air exhaust port (507), the water storage tank (502) is provided with a first water inlet (509), a first water outlet (510) and a waste gas outer exhaust port (522), the water ring vacuum pump (501) is provided with a water inlet (506) communicated with a water ring of the water ring vacuum pump, the first water inlet (509) is connected with the air exhaust port (507) of the water ring vacuum pump (501) through a pipeline, and the first water outlet (510) is connected with a water inlet of the water ring vacuum pump (501).
8. The system for producing biodiesel by using double enzymes according to claim 7, wherein the condensing mechanism comprises a spiral plate type heat exchanger (503) connected with the water storage tank (502), a first circulating water pump (505) connected between the water storage tank (502) and the spiral plate type heat exchanger (503), and a cold water tank (504) connected with the spiral plate type heat exchanger (503);
the spiral plate type heat exchanger (503) comprises a heat exchanger main body (531), a first spiral heat exchange channel (532) and a second spiral heat exchange channel (533) which are arranged in the heat exchanger main body (531), the water storage tank (502) is connected with the first spiral heat exchange channel (532), and the cold water tank (504) is connected with the second spiral heat exchange channel (533);
the water storage tank (502) is provided with a second water inlet (512) and a second water outlet (513), the second water inlet (512) is connected with the water outlet of the first spiral heat exchange channel (532) through a first pipeline (515), and the second water outlet (513) is connected with the water inlet of the first spiral heat exchange channel (532) through a second pipeline (516);
first circulating water pump (505) is located on second pipeline (516), be connected with drain pipe (517) on second pipeline (516), drain pipe (517) insert between first circulating water pump (505) and first spiral heat transfer passageway (532), be equipped with drain valve (518) on drain pipe (517), drain pipe (517) insert to the sewage treatment workshop section, be connected with inlet tube (519) on first pipeline (515), inlet tube (519) connect out from cold water tank (504) bottom, be equipped with water intaking valve (520) and water pump (521) on inlet tube (519), the water inlet and the delivery port of second spiral heat transfer passageway (533) are connected through interior bottom and the interior top of pipeline with cold water tank (504) respectively, be equipped with second circulating water pump (514) on second spiral heat transfer passageway (533) water inlet and the cold water tank (504) bottom phase connection pipeline.
9. The system for producing biodiesel by using double enzymes according to claim 7, wherein the tail gas treatment mechanism (8) comprises an alkali liquor spray tower (801) which is connected out from an exhaust gas outlet (522) of the water storage tank (502) through a pipeline and used for tail gas purification, a gas-liquid separation tower (802) which is connected out from the alkali liquor spray tower (801) and used for purified tail gas separation, and a boiler (803) which is arranged beside the gas-liquid separation tower (802) and used for harmless treatment of purified gas, wherein a circulating spray device used for recycling alkali liquor is arranged on the alkali liquor spray tower (801), and a blower (804) used for purified tail gas suction is arranged on the boiler (803);
the circulating spraying device comprises an alkali liquor circulating pipe (805) connected out of the alkali liquor spraying tower (801) and a circulating spraying mechanism connected with the alkali liquor circulating pipe (805) and extending into the alkali liquor spraying tower (801) for spraying alkali liquor on the distillation tail gas, wherein the alkali liquor circulating pipe (805) is provided with an alkali liquor circulating pump (806) and a valve (807), and the circulating spraying mechanism comprises at least two spraying pipes (808) connected out of the alkali liquor circulating pipe (805) and spiral spraying nozzles (809) arranged on the spraying pipes (808);
an upper observation viewing mirror (811) for observing the accumulation condition of the reaction soap is arranged at the middle lower part of the alkali liquor spray tower (801), a lower observation viewing mirror (812) for observing the alkali liquor in the alkali liquor spray tower is arranged at the lower part of the alkali liquor spray tower, a gas pipe (813) is connected between the alkali liquor spray tower (801) and the gas-liquid separation tower (802), the gas pipe (813) is connected out from the top of the alkali liquor spray tower (801) and connected to the lower part of the gas-liquid separation tower (802), the pipe diameter of the gas pipe (813) is at least 15cm, an observation viewing mirror (814) for observing the separation liquid is arranged at the middle lower part of the gas-liquid separation tower (802), and a liquid discharge port (815) is arranged at the bottom of the gas-liquid separation tower (802);
the top of the gas-liquid separation tower (802) is connected with an exhaust pipe (816), the gas outlet of the exhaust pipe (816) is opposite to the gas inlet of the blower (804) and the distance between the gas outlet and the gas inlet is at least 2 m;
the upper part of the alkali liquor spray tower (801) is provided with an alkali liquor inlet (817) for replenishing alkali liquor, the bottom part of the alkali liquor spray tower is provided with an alkali liquor outlet (818) for discharging waste alkali liquor, and the alkali liquor outlet (818) is provided with a liquid discharge valve (819).
10. The method for producing a system for producing biodiesel using two enzymes according to any one of claims 1 to 9, characterized by comprising the steps of:
s1, enabling waste gas animal and vegetable oil to enter a liquid enzyme reaction tank and hydrolyzing the waste gas animal and vegetable oil and methanol and water in the tank under the catalysis of liquid lipase to generate fatty acid methyl ester;
s2, separating solid-phase slag substances, aqueous phase liquid enzyme aqueous solution and oil phase mixed fatty acid from the mixture consisting of the product and the raw materials in the step S1 in a separating mechanism;
s3, separating the aqueous phase liquid enzyme solution by a continuous settling mechanism to obtain liquid lipase, introducing the liquid lipase into a liquid enzyme reaction tank for recycling, and removing water and waste gas from the oil-phase mixed fatty acid in a drying mechanism;
s4, removing waste gas and heavy oil from the mixed fatty acid with water and gas removed in a distillation mechanism to obtain primary methyl ester;
s5, allowing the primary methyl ester to enter a solid enzyme reaction tank for secondary hydrolysis under the catalysis of immobilized lipase, so that residual free fatty acid in the primary methyl ester completely reacts with triglyceride to generate fatty acid methyl ester;
s6, filtering and purifying the waste gas removed in the steps S3 and S4 in a vacuum circulating cooling mechanism to obtain primary purified tail gas;
and S7, allowing the primary purified tail gas to enter a tail gas treatment mechanism for saponification purification, and finally entering a boiler for combustion.
CN202210907754.XA 2022-07-29 2022-07-29 System for producing biodiesel by using double enzymes and production method thereof Pending CN115386432A (en)

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US20140020282A1 (en) * 2012-07-23 2014-01-23 Paul Lavella, SR. Method and system for integrated biodiesel production
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