CN108795749A - A kind of devices and methods therefor of immobilized tannase production gallic acid - Google Patents
A kind of devices and methods therefor of immobilized tannase production gallic acid Download PDFInfo
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- CN108795749A CN108795749A CN201810967054.3A CN201810967054A CN108795749A CN 108795749 A CN108795749 A CN 108795749A CN 201810967054 A CN201810967054 A CN 201810967054A CN 108795749 A CN108795749 A CN 108795749A
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- gallic acid
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- enzyme
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- tannase
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/18—Apparatus specially designed for the use of free, immobilized or carrier-bound enzymes
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/22—Preparation of oxygen-containing organic compounds containing a hydroxy group aromatic
Abstract
The present invention relates to the devices and methods therefors that a kind of immobilized tannase produces gallic acid.Device includes：Feedstock pre-processing system, hydrolysis system and piece-rate system.The working condition on the one hand solving tank reactor using the device can not change in real time, and not for the moment, product quality can not ensure material quality, the problem of flexibility difference；On the other hand it solves the problems, such as that stirring and bubbling destroy the strong mechanism of enzyme the structure of immobilized enzyme, so that enzyme is recycled number and maximize.Collocation continuous production processes, and inhibiting effect of the raising to enzymatic activity of gallic acid concentration in production process is relieved, the service life of immobilised enzymes is greatly improved while improving transformation efficiency.Using device and method of the present invention produce gallic acid, have the advantages that equipment is simple, technique flexibly, high income, superior product quality, production pollution it is small, easily realize industrialization, for gallic acid clean and effective produce provide strong technical support.
Description
Technical field
The present invention relates to the devices and methods therefors that a kind of immobilized tannase produces gallic acid, specifically with fixed tannin
It is research object, a kind of quantity-produced column reactor without mixing of research and design and production method that enzyme, which produces gallic acid, is belonged to
In biological chemical field.
Background technology
Gallic acid also known as gallic acid, chemical name are Gallic Acid, are white or light brown needle-shaped
Or flat crystal, it is widely present in the plants such as Chinese gall, tower drawing, grape.It is a kind of important fine chemical product, uses extensively
In fields such as chemical industry, medicine, food and electronics industries.
Hydrolysis Chinese tannin production gallic acid is the main source of gallic acid product in the world, and technology is main
Have：Acid-hydrolysis method, alkali hydrolysis method, fermentation method and enzyme process.Acid, alkali hydrolysis method are due to tannin high conversion rate, simple for process forming
For industry universal method, but its one side severe corrosion to equipment, on the other hand produce that waste liquid amount is big and COD high, coloration are big, contains
Salt amount is high and causes processing difficult, of high cost, can cause huge pollution to environment if it cannot handle completely.With biological skill
The continuous development of art, is reached its maturity using fermentation method and preparation of gallic acid by using enzyme.But fermentation method length reaction time, tannin hydrolysis
Not exclusively, process is difficult to control and causes gallic acid yield low, larger to Natural Resources of Gallnuts waste, is not eaten using Production by Enzymes
Sub- acid becomes the mainstream of research.And immobilised enzymes obtains extensive as a kind of recyclable, efficient, segregative enzyme preparation
Using.
CN106978451A discloses a kind of method that immobilized glucose oxidase prepares sodium gluconate.This method will
The glucose oxidase prepared is mixed with glucose solution, is stirred to react obtained sodium gluconate.CN106957883A is disclosed
A kind of method of immobilization allinase synthesis 4,5,9-trithiadodeca-1,6,11-triene 9-oxide.The allinase prepared and allicin are mixed this method, after filtering
Dry obtained 4,5,9-trithiadodeca-1,6,11-triene 9-oxide.CN102321681B discloses a kind of method of immobilized tannase production gallic acid.This method will
Gallnut extract, training pollen or tower after crushing draw powder raw material to be placed in raw material pot for solvent extraction, obtain leaching liquor.In the water equipped with leaching liquor
It solves and the static hydrolysis of immobilized tannase progress is added in tank, gallic acid is made.Wherein, enzyme reactor is anti-for completing enzymatic
The core apparatus answered provides suitable place and best reaction condition for enzymic catalytic reaction.Enzyme reactor is with bubble type at present
Based on stirring pot type, mostly to stir based on pot type enzyme reactor.Bubble type utilizes the gas being passed through from reactor bottom to generate
A large amount of bubbles, the immixture of substrate and enzyme is played in uphill process, and stir pot type utilize from using stirring by substrate
It is mixed with enzyme.Both methods needs equipment simple, and operation is easy, but Shortcomings.On the one hand, the production item of tank reactor
Part can not change in real time, and not for the moment, product quality can not ensure that flexibility is poor to material quality.On the other hand, stirring and bubbling pair
Enzyme has strong mechanism, destroys the structure of immobilized enzyme, influences the service life of enzyme.
Therefore, a kind of device and method producing gallic acid using immobilised enzymes continuous high-efficient of design have critically important
Realistic meaning.
Invention content
The present invention relates to the devices and methods therefors that a kind of immobilized tannase produces gallic acid.Device includes：Raw material is pre-
Processing system, hydrolysis system and piece-rate system.Method is end toper under the reacted device of tannic acid solution in tannic acid fluid reservoir
Enter reactor shell after absorbent cotton coarse filtration in end socket, enters crystallisation by cooling after the fixed tannin enzyme hydrolysis in tube body
Tank opens valve after the precipitation of gallic acid crystal, flows into centrifuge, product dry packing after centrifugation, and centrifuge mother liquor returns single
Continue to hydrolyze as raw material in peaceful fluid reservoir.
The feedstock pre-processing system includes tannic acid fluid reservoir and pure water fluid reservoir；The hydrolysis system is served as reasons
The column reactor of cylindrical tube and top and the bottom conical head composition；The piece-rate system includes crystallisation by cooling tank and centrifugation
Machine；Tannic acid fluid reservoir and pure water liquid storage pot bottom are connect through pipeline with reactor bottom；Reactor top by pipeline with
Crystallisation by cooling tank top connects；Crystallisation by cooling tank lower part is connect with centrifuge by pipeline.
Tannic acid fluid reservoir and pure water fluid reservoir in the feedstock pre-processing system all have chuck, can be in tank
Material is heated or cooled.
The reactor shell has chuck, and material in reactor can be heated or cooled.
The reactor conical head, the one end to connect with cylinder are the load-bearing stainless steel sieve with uniform circular hole
Plate.
By flanged joint between the reactor conical head and cylinder, can be freely disassembled.
200 mesh stainless steel filtering nets are accompanied between the reactor conical head and cylinder.
Immobilized tannase is housed in the reactor shell；The reactor lower part conical head is equipped with filling
Object, the filler are absorbent cotton or gauze；
The crystallisation by cooling tank has stirring by least three, the retort of refrigerating function is formed and is formed by connecting, between each tank
It is connected with centrifuge by pipeline.
The reactor shell ratio of height to diameter is 12:1~7:1；Preferred reactor cylinder ratio of height to diameter is 10:1.
The method that immobilized tannase produces gallic acid, the tannin liquid mass concentration in the tannic acid fluid reservoir are
6~13%, pH are 7 ± 0.5, and temperature is 40-50 DEG C.
Immobilized tannase is filled in the reactor shell, it is 40- to be heated by chuck and keep reactor temperature
50 DEG C, the flow velocity of control tannin liquid in the reactor is no more than 0.6VEnzyme/h(VEnzymeIndicate the accumulation of immobilized tannase in reactor
Volume).
It is when the quality for the immobilized tannase that the quality for being converted to dry matter with the tannic acid solution of entrance is equal to filling
A batch, often primary with tannase in 40-50 DEG C of pure water flushing reactor before production next group, the volume of flushing liquor is 1VEnzyme,
It rinses speed and is no more than 0.6VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
Produce gallic acid using device and method of the present invention, have equipment is simple, technique flexibly, high income,
Small advantage is polluted in superior product quality, production, is in particular in：
(1) non-stirring reactor of autonomous Design is simple in structure, and operation is flexible, solves stirring and is bubbled the strong machine to enzyme
The problem of tool acts on and destroys the structure of immobilized enzyme makes enzyme recycle number and maximizes.
(2) it is digested by reactor, adjusting flow velocity and jacket temperature of the tannin mother liquor in reactor can be effective
Control hydrolysis rate and degree, the working condition for solving tank reactor can not change in real time, material quality not for the moment,
Product quality can not ensure, the problem of flexibility difference.
(3) unicity of biological enzyme is utilized to produce gallic acid, product is single, and product impurity is few, and quality is high.
(4) continuous production processes, but the inhibition of enzymatic activity is made in the raising for relieving gallic acid concentration in production process
With greatly improving the service life of immobilised enzymes while improving transformation efficiency.
(5) complete tannin do not hydrolyzed be returned in mother liquor after follow-up centrifugation and applied mechanically, both can guarantee the conversion ratio of tannic acid,
It is generated again without the waste water of with high salt, high COD, environmental protection has been taken into account while realizing economic benefit.
Description of the drawings
Fig. 1 is the apparatus structure schematic diagram that immobilized tannase produces gallic acid, wherein 1. tannic acid fluid reservoirs, 2.
Pure water fluid reservoir, 3. column reactors, 4. flanges, 5. strainers, 6. sieve plates, 7. spinner flowmeters, 8. crystallisation by cooling tanks, 9. points
It disembarks, 10. mother liquor recovering devices.
Specific implementation mode
To explain the technical content, the achieved purpose and the effect of the present invention in detail, below in conjunction with embodiment and coordinate attached
Figure is explained.
Embodiment 1：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 6%, pH, and temperature is 45 DEG C.Pure water temperature is adjusted to 45 in pure water fluid reservoir
℃。
(2) primary with tannase in 45 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.6VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 0.6V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters
Reactor shell, it is 45 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through
Ice water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, filter cake is products obtained therefrom, filtrate
It is recycled to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, a batch production
Time is 28 hours, yield 71.3%, content 99.5%.
Embodiment 2：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 10%, pH, and temperature is 48 DEG C.Pure water temperature is adjusted to 48 in pure water fluid reservoir
℃。
(2) primary with tannase in 48 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.5VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 0.5V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters
Reactor shell, it is 48 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through
Ice water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, filter cake is products obtained therefrom, filtrate
It is recycled to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, a batch production
Time is 16.7 hours, yield 71.2%, content 99.6%.
Embodiment 3：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 13%, pH, and temperature is 46 DEG C.Pure water temperature is adjusted to 46 in pure water fluid reservoir
℃。
(2) primary with tannase in 46 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.45VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 0.45V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters
Reactor shell, it is 46 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through
Ice water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, filter cake is products obtained therefrom, filtrate
It is recycled to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, a batch production
Time is 12.8 hours, yield 63.5%, content 96.8%.
Embodiment 4：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 6%, pH, and temperature is 42 DEG C.Pure water temperature is adjusted to 42 in pure water fluid reservoir
℃。
(2) primary with tannase in 42 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.42VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 0.42V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters
Reactor shell, it is 42 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through
Ice water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, filter cake is products obtained therefrom, filtrate
It is recycled to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, a batch production
Time is 83.3 hours, yield 71.8%, content 99.6%.
Embodiment 5：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 10%, pH, and temperature is 45 DEG C.Pure water temperature is adjusted to 45 in pure water fluid reservoir
℃。
(2) primary with tannase in 45 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.35VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 0.2V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters
Reactor shell, it is 45 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through
Ice water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, filter cake is products obtained therefrom, filtrate
It is recycled to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, a batch production
Time is 50 hours, yield 71.1%, content 99.5%.
Embodiment 6：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 13%, pH, and temperature is 44 DEG C.Pure water temperature is adjusted to 44 in pure water fluid reservoir
℃。
(2) primary with tannase in 44 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.36VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 0.2V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters
Reactor shell, it is 44 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through
Ice water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, filter cake is products obtained therefrom, filtrate
It is recycled to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, a batch production
Time is 38.4 hours, yield 68.3%, content 98.4%.
Embodiment 7：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 6%, pH, and temperature is 40 DEG C.Pure water temperature is adjusted to 46 in pure water fluid reservoir
℃。
(2) primary with tannase in 46 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.6VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 1V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters anti-
Device cylinder is answered, it is 46 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through ice
Water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, and filter cake is products obtained therefrom, and filtrate is returned
It receives to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, when a batch produces
Between be 16.7 hours, yield 70.2%, content 99.1%.
Embodiment 8：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 8%, pH, and temperature is 43 DEG C.Pure water temperature is adjusted to 40 in pure water fluid reservoir
℃。
(2) primary with tannase in 40 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.5VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 1V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters anti-
Device cylinder is answered, it is 40 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through ice
Water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, and filter cake is products obtained therefrom, and filtrate is returned
It receives to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, when a batch produces
Between be 10 hours, yield 68.7%, content 99.3%.
Embodiment 9：
(1) it is 10 by ratio of height to diameter:Immobilized tannase is filled in 1 reactor shell；It will be in tank by tannic acid fluid reservoir
It is 7 ± 0.5 that tannic acid solution mass concentration, which is adjusted to 13%, pH, and temperature is 46 DEG C.Pure water temperature is adjusted to 46 in pure water fluid reservoir
℃。
(2) primary with tannase in 46 DEG C of pure water flushing reactor respectively before producing, the volume of flushing liquor is 1VEnzyme,
Flushing speed is 0.6VEnzyme/ h, flushing liquor are merged into tannin fluid reservoir.
(3) with 1V after the absorbent cotton coarse filtration in the reacted device lower end conical head of tannic acid solutionEnzymeThe flow velocity of/h enters anti-
Device cylinder is answered, it is 46 DEG C to keep reactor temperature, and tannin liquid enters crystallisation by cooling tank after being hydrolyzed by enzyme layer, and chuck is passed through ice
Water cools down, and waits in tank that temperature is down to 20 DEG C and is dehydrated hereinafter, coolant liquid is put into centrifuge, and filter cake is products obtained therefrom, and filtrate is returned
It receives to tannic acid fluid reservoir, continuous feed liquor to a batch production terminates.The gallic acid produced through the above steps, when a batch produces
Between be 7.7 hours, yield 60.9%, content 95.3%.
Embodiment 10
A kind of device of immobilized tannase production gallic acid, including feedstock pre-processing system, hydrolysis system and separation
System；The feedstock pre-processing system includes tannic acid fluid reservoir 1 and pure water fluid reservoir 2；The hydrolysis system is tool
The column reactor 3 being made of the chromatographic column of constant temperature jacket and the conical head of lower part；The piece-rate system includes cooling ties
Brilliant tank 7 and centrifuge 8；Tannic acid fluid reservoir 1 and 2 bottom of pure water fluid reservoir are connect through pipeline with 3 bottom of column reactor；Column
3 top of formula reactor is connect by pipeline with 7 top of crystallisation by cooling tank；7 lower part of crystallisation by cooling tank is connected with centrifuge 8 by pipeline
It connects.
One end that the conical head of 7 bottom of column reactor connects with cylinder is provided with the load-bearing of uniform circular hole not
Become rusty steel sieve plate 5, and 200 mesh stainless steel filtering nets 5 are accompanied between the conical head and cylinder of the column reactor.
The 3 lower taper end socket of column reactor is equipped with filler, and the filler is absorbent cotton or gauze；Column
It is filled with tannase in the cylinder of formula reactor 3.
The crystallisation by cooling tank 7 is formed by connecting by least three retort, is connected with centrifuge 8 by pipeline between each tank.
The 3 cylinder ratio of height to diameter of column reactor is 10:1.
Example the above is only the implementation of the present invention is not intended to limit the scope of the invention, every to utilize this hair
Equivalents made by bright specification and accompanying drawing content are applied directly or indirectly in relevant technical field, include similarly
In the scope of patent protection of the present invention.
Claims (9)
1. a kind of device of immobilized tannase production gallic acid, which is characterized in that including feedstock pre-processing system, hydrolysis system
System and piece-rate system；The feedstock pre-processing system includes tannic acid fluid reservoir（1）With pure water fluid reservoir（2）；Described
Hydrolysis system is the column reactor that the conical head of chromatographic column and lower part with constant temperature jacket forms（3）；The separation
System includes crystallisation by cooling tank（7）And centrifuge（8）；Tannic acid fluid reservoir（1）With pure water fluid reservoir（2）Bottom through pipeline with
Column reactor（3）Bottom connects；Column reactor（3）Top passes through pipeline and crystallisation by cooling tank（7）Top connects；Cooling knot
Brilliant tank（7）Lower part and centrifuge（8）It is connected by pipeline.
2. the device of immobilized tannase production gallic acid described in claim 1, which is characterized in that the pillar reaction
Device（7）One end that the conical head of bottom connects with cylinder is provided with the load-bearing stainless steel sieve of uniform circular hole（5）, the column
200 mesh stainless steel filtering nets are accompanied between the conical head and cylinder of formula reactor（5）.
3. the device of immobilized tannase production gallic acid described in claim 1, which is characterized in that the pillar reaction
Device（3）Lower taper end socket is equipped with filler, and the filler is absorbent cotton or gauze；
Column reactor（3）Cylinder in be filled with tannase.
4. the device of immobilized tannase production gallic acid described in claim 1, which is characterized in that the crystallisation by cooling
Tank（7）It is formed by connecting by least three retort, passes through pipeline and centrifuge between each tank（8）It is connected.
5. the device of immobilized tannase production gallic acid described in claim 1, which is characterized in that the pillar reaction
Device（3）Cylinder ratio of height to diameter is 12:1~7:1；It is preferred that column reactor（3）Cylinder ratio of height to diameter is 10:1.
6. producing gallic acid using the device of claim 1-5 any one of them immobilized tannases production gallic acid
Method, which is characterized in that the tannic acid solution in the tannic acid fluid reservoir is through de- in the conical head of column reactor lower end
Enter reactor shell after fat cotton coarse filtration, enters crystallisation by cooling tank after the fixed tannin enzyme hydrolysis in tube body, wait for nutgall
After acid crystal is precipitated, valve is opened, flows into centrifuge, product dry packing after centrifugation, centrifuge mother liquor returns in tannin fluid reservoir
Continue to hydrolyze as raw material.
7. the method for the production gallic acid described in claim 6, which is characterized in that the tannin in the tannic acid fluid reservoir
Liquid mass concentration is that 6 ~ 13%, pH is 7 ± 0.5, and temperature is 40-50 DEG C.
8. the method for the production gallic acid described in claim 6, which is characterized in that fill fixation in the reactor shell
Change tannase, it is 40-50 DEG C to heat and keep reactor temperature, and the flow velocity of control tannin liquid in the reactor is no more than
0.6VEnzyme/ h, VEnzymeIndicate the stacking volume of immobilized tannase in reactor.
9. the method for the production gallic acid described in claim 6, which is characterized in that use 40-50 respectively before often producing next group
DEG C pure water rinse that tannase in reactor is primary, and the volume of flushing liquor is 1VEnzyme, rinse speed and be no more than 0.6VEnzyme/ h is rinsed
Liquid is merged into tannin fluid reservoir.
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5952023A (en) * | 1996-02-05 | 1999-09-14 | Lipton, Division Of Conopco, Inc. | Enzyme extraction process for tea |
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