CN108863868A - A kind of feather produces the device of a variety of amino acid - Google Patents
A kind of feather produces the device of a variety of amino acid Download PDFInfo
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- CN108863868A CN108863868A CN201710337485.7A CN201710337485A CN108863868A CN 108863868 A CN108863868 A CN 108863868A CN 201710337485 A CN201710337485 A CN 201710337485A CN 108863868 A CN108863868 A CN 108863868A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
- C07C227/38—Separation; Purification; Stabilisation; Use of additives
- C07C227/40—Separation; Purification
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C277/00—Preparation of guanidine or its derivatives, i.e. compounds containing the group, the singly-bound nitrogen atoms not being part of nitro or nitroso groups
- C07C277/08—Preparation of guanidine or its derivatives, i.e. compounds containing the group, the singly-bound nitrogen atoms not being part of nitro or nitroso groups of substituted guanidines
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C319/00—Preparation of thiols, sulfides, hydropolysulfides or polysulfides
- C07C319/26—Separation; Purification; Stabilisation; Use of additives
- C07C319/28—Separation; Purification
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Abstract
The invention discloses the devices that a kind of feather produces a variety of amino acid, belong to technical field of amino acid production.Device coproduction cystine, leucine and the tyrosine.Wherein, cystine workshop section includes that hydrolysis, concentration, alkali neutralization, a mother stock are neutralized from, acid, primary decoloration, secondary decolourization, ammonia neutralization and cystine refine；Wherein, leucine workshop section includes two female concentrations, condensation, two female ammonolysis, two female decolorations, two female ammonia neutralize and leucine purification；Wherein, tyrosine workshop section includes an alkali soluble, three female alkali neutralizations, secondary alkali soluble, three female acid neutralizations, three female decolorations, three female ammonolysis and tyrosine purification.The device has carried out many places adjustment on the basis of existing production technology, to reduce cost and improve the yield of product, meanwhile, technique provided by the invention is more smooth, is suitble to industrialized production.
Description
Technical field
The present invention relates to technical field of amino acid production, in particular to a kind of feather produces the device of a variety of amino acid, especially
It is related to a kind of device that cystine, tryptophan and tyrosine are produced using drake feather or goose feather.
Background technique
Since world market is to the great demand of poultry meat product, butchering for birds generates a large amount of plumage in process
Hair, so that annual feather waste reaches millions of tons, these feathers are as directly discarded, and rot degradation time under field conditions (factors)
It is long, and smelly pollute the environment of rotting；As burning and burying needs a large amount of man power and material, it is also possible to secondary pollution is caused,
Waste valuable resource.Since feather contains a large amount of protein, amino acid is such as degraded to by the method for chemistry,
Not only the pollution of feather waste generation had been avoided, but also with good economic efficiency, can yet be regarded as is the best of current processing feather
Method.
The conventional method of amino-acids that is degraded to feather is acid hydrolyzation at present, and feather is sent by acid hydrolyzation after physical treatment
In acid hydrolysis tank, after repeatedly being neutralized and decolourized, a mother liquor, secondary mother liquid, three times mother liquor and Cystine Product are generated, it is primary female
Liquid, secondary mother liquid, mother liquor send compound amino acid workshop section, leucine workshop section and tyrosine workshop section to produce different amino respectively three times
Acid.The process flow of different workshop sections is illustrated below：
One, the process flow of cystine workshop section is：1.1 hydrolysis section
Raw material：Hair；Auxiliary material：Hydrochloric acid, steam；Hair is put into hydrolytic decomposition pot and is sealed, hydrochloric acid is passed through（Concentration ﹥ 30%）, steam；
120 DEG C of temperature, acidolysis time 7h；Terminal product：Hydrolyzate（Remove a neutralizing zone）.
1.2 neutralizing zones
Auxiliary material：Liquefied ammonia（Or liquid alkaline）；Hydrolyzate enters a neutralizing tank, is passed through liquefied ammonia（Or liquid alkaline）；80 DEG C of temperature, neutralize the time
20h, terminal pH=5.0, filtering；Terminal product：1, filtrate（That is a mother liquor, send L-arginine workshop to do raw material）2, filter residue（It goes
Primary decoloration section）.
1.3 primary decoloration sections
Auxiliary material：Hydrochloric acid, steam, pure water, active carbon；Filter residue enters bleacher, throws（It is logical）Enter hydrochloric acid, steam, pure water, active carbon；
80 DEG C of temperature, bleaching time 2h, terminal pH=0.5, filtering；Terminal product：1, filter residue（Burning）2, filtrate（Go secondary neutralization
Section）.
1.4 2 neutralizing zones
Auxiliary material：Ammonium hydrogen carbonate；Filtrate enters secondary neutralizing tank, puts into ammonium hydrogen carbonate；80 DEG C of temperature, neutralize time 12h, terminal pH
=5.0, filtering；Terminal product：1, filtrate（That is secondary mother liquid send L-Leu workshop to do raw material）2, filter residue（Remove secondary decolourization
Section）.
1.5 secondary decolourization sections
Auxiliary material：Hydrochloric acid, steam, pure water, active carbon；Filter residue enters bleacher, throws（It is logical）Enter hydrochloric acid, steam, pure water, active carbon,
80 DEG C of temperature, bleaching time 2h, terminal pH=0.5, filtering；Terminal product：1, filter residue（It recycles）2, filtrate（It goes in three times
And section）.
1.6 neutralizing zones three times
Auxiliary material：Ammonium hydroxide；Filtrate enters neutralizing tank three times, is passed through ammonium hydroxide, and temperature 80 neutralizes time 3h, terminal pH=4.0, filtering；
Terminal product：1, filtrate（That is mother liquor three times, send l-tyrosine workshop to do raw material）2, filter residue（That is l-cysteine crude product goes to refine
Section）.
1.7 refining stage
Auxiliary material：Distilled water, steam；With distilled water flushing upper section process product and centrifuge dripping, it is sent into dryer, is passed through steam baking
It is dry, it packs, storage, 100 DEG C of drying temperature, drying time 3h；Terminal product：L-cysteine finished product.
Two, the process flow of leucine workshop section is：
2.1 enriching section
Raw material：Steam；Secondary mother liquid is passed through in concentration tank, is passed through steam, 120 DEG C of temperature, air pressure -0.09MPa, concentration time
6h, crystallization；Terminal product：Crystal solution（Remove a neutralizing zone）.
2.2 neutralizing zones
Auxiliary material：Sulfuric acid, pure water；Crystal solution enters a neutralizing tank, is passed through sulfuric acid, and pure water, neutralizes time 4h, mistake by 80 DEG C of temperature
Filter；Terminal product：1, filtrate（It recycles）2, filter residue（Go ammonolysis section）
2.3 ammonolysis sections
Auxiliary material：Ammonium hydroxide, pure water, steam；Filter residue enters ammonolysis tank, is passed through ammonium hydroxide, pure water, steam, and 80 DEG C of temperature, the ammonolysis time
3h, filtering；Terminal product, 1, filtrate（It recycles）2, filter residue（Go decoloration section）(cystine).
2.4 decoloration sections
Auxiliary material：Steam, pure water, active carbon；Filter residue enters bleacher, leads to（It throws）Enter steam, pure water, active carbon, takes off by 80 DEG C of temperature
Color time 2h, filtering；Terminal product：1, filter residue（It recycles）2, filtrate（Remove secondary neutralizing zone）
2.5 2 neutralizing zones
Auxiliary material：Ammonium hydroxide, steam；Filtrate enters secondary neutralizing tank, is passed through ammonium hydroxide, and steam, neutralizes time 4h, filtering by 80 DEG C of temperature；
Terminal product, 1, filtrate（It recycles）2, filter residue（That is L-Leu crude product, removes refining stage）
2.6 refining stage
Auxiliary material：Distilled water, steam (histidine hydrochloride)；With distilled water flushing upper section process product and centrifuge dripping, it is sent into and dries
Dry machine is passed through steam drying, packs, storage, and 100 DEG C of drying temperature, drying time 3h；Terminal product：L-Leu finished product.
The process flow of tyrosine workshop section is：
3.1 alkali soluble sections
Raw material：Mother liquor three times（Neutralizing zone product three times in l-cysteine production）；Auxiliary material：Liquid alkaline, pure water, active carbon；It will three times
Mother liquor is passed through in alkali soluble tank, is led to（It throws）Enter liquid alkaline, pure water, active carbon, filters by 90 DEG C of temperature, alkali soluble time 6h；Terminal product：
1, filter residue (recycling) 2, filtrate（Remove a neutralizing zone）.
3.2 neutralizing zones
Auxiliary material：Hydrochloric acid；Filtrate enters a neutralizing tank, is passed through hydrochloric acid, 80 DEG C of temperature, neutralizes time 6h, terminal pH=8.5, mistake
Filter；Terminal product：1, filtrate（It recycles）2, filter residue（Go decoloration section）.
3.3 decoloration sections
Auxiliary material：Hydrochloric acid, steam, pure water, active carbon；Filter residue enters bleacher, leads to（It throws）Enter hydrochloric acid, steam, pure water, active carbon,
80 DEG C of temperature, bleaching time 2h, terminal pH=0.5, filtering；Terminal product：1, filter residue（It recycles）2, filtrate（It goes in secondary
And section）.
3.4 2 neutralizing zones
Auxiliary material：Ammonium hydroxide；Filtrate enters secondary neutralizing tank, is passed through ammonium hydroxide, 80 DEG C of temperature, neutralizes time 4h, terminal pH=4.0, knot
Crystalline substance, filtering；Terminal product：1, filtrate（It recycles）2, filter residue（That is l-tyrosine crude product, removes refining stage）.
3.5 refining stage
Auxiliary material：Distilled water, steam；With distilled water flushing upper section process product and centrifuge dripping, it is sent into dryer, is passed through steam baking
It is dry, it packs, storage, 100 DEG C of drying temperature, air pressure -0.09Mpa, drying time 5h.
When applicant states process in realization, the dosage of discovery acid, alkali and active carbon is big, causes production cost higher；Together
When, produce a large amount of waste water；In addition, the yield of cystine, leucine and tyrosine is lower.
Summary of the invention
To solve the above-mentioned problems, the purpose of the present invention is to provide the devices that a kind of feather produces a variety of amino acid, use
In reducing cost and improving yield, to obtain bigger economic benefit.The technical solution is as follows：
The embodiment of the invention also provides the device that a kind of feather produces a variety of amino acid, which includes cystine workshop section, bright
Propylhomoserin workshop section and tyrosine workshop section etc..
Wherein, cystine workshop section includes HCl recovery structure and the hydrolytic reaction pot set gradually, the first inspissator, in alkali
It is anti-with reaction kettle, sedimentation basin, the first plate and frame filter press, dissolving tank, sour neutralization reaction kettle, the second plate and frame filter press, the first decoloration
Answer kettle, third plate and frame filter press, the second decoloring reaction kettle, the 4th plate and frame filter press, ammonia neutralization reaction kettle and first centrifuge etc..
Wherein, HCl recovery structure is connect for recycling hydrolysis with hydrolytic reaction pot, the first inspissator, alkali neutralization reaction kettle and dissolving tank
The dilute hydrochloric acid of reaction kettle, the first inspissator and the discharge of alkali neutralization reaction kettle, the sludge outlet of the 4th plate and frame filter press pass through conveying
Structure is connect with the feed inlet of the first decoloring reaction kettle for recycling waste active carbon.
Liquid is realized by pipeline and is transported in pre-structure, and filter residue is transported by structure for conveying.
Wherein, leucine workshop section includes material-compound tank and the two female inspissators set gradually, condensation reaction kettle, cooling reactor, the
Five plate and frame filter press, two female ammonolysis reaction kettles, the 6th plate and frame filter press, two female decoloring reaction kettles, the 7th plate and frame filter press, two mothers
Ammonia neutralization reaction kettle and two female centrifuges etc..Wherein, material-compound tank connect with the feed inlet of condensation reaction kettle for deploy sulfuric acid with
To obtain ortho-xylene -4- sulfonic acid, the liquid feeding end of two female inspissators and the filtrate (liquid of the second plate and frame filter press connect ortho-xylene
It connects.Preferably, the filtrate (liquid of the 5th plate and frame filter press connect the production for improving leucine with the feed inlet of condensation reaction kettle
Rate.
Liquid is realized by pipeline and is transported in pre-structure, and filter residue is transported by structure for conveying.
Wherein, tyrosine workshop section includes the first alkali soluble reaction kettle set gradually, three female alkali neutralization reaction kettles, the 8th sheet frame
Filter press, the second alkali soluble reaction kettle, the 9th plate and frame filter press, three female sour neutralization reaction kettles, the tenth plate and frame filter press, three female decolorations
Reaction kettle, the 11st plate and frame filter press, three female ammonolysis reaction kettles and three female centrifuges etc., the feed inlet of the first alkali soluble reaction kettle with
The centrifugate of first centrifuge exports connection, and the sludge outlet of the 11st plate and frame filter press is anti-by structure for conveying and the second alkali soluble
The feed inlet of kettle is answered to connect for recycling waste active carbon.
Preferably, the sludge outlet of the 9th plate and frame filter press is connected by the feed inlet of structure for conveying and two female decoloring reaction kettles
It connects for recycling waste active carbon（Certainly, it directly can also manually be transported by cart here）.8th plate and frame filter press
Filtrate (liquid connect the yield for improving leucine with the feed inlet of two female ammonolysis reaction kettles.
Liquid is realized by pipeline and is transported in pre-structure, and filter residue is transported by structure for conveying.
In aforementioned structure, each structure is sequentially connected with essentially by pipeline（Wherein the conveying of filter residue is carried out by structure for conveying
Transport）, the structures such as kinetic pump, valve and flow valve are set as needed on pipeline.Meanwhile aforementioned each structure be all it is acidproof or
Caustic corrosion structure, reaction kettle are enamel reaction still or glass reaction kettle（Capacity uses 10 cubes, 15 cubes or 20 vertical as needed
Side）, each reaction kettle be set as needed stirring, thermometer, barometer, insulation jacket, cooling water jecket etc. or at tail gas
The connection of reason system.Further, two layers of the setting in each workshop point, each reaction kettle or sedimentation basin or dissolving tank etc. are set to one layer, sheet frame
Filter press is set to two layers.Structure for conveying includes that detachable inclined plate and one side are arranged below the slag-drip opening of plate and frame filter press（Row
Cinder notch side）Filter residue is sent into collecting tank by collecting tank disposed in parallel, inclined plate, and collecting tank will by conveyer belt or delivery chute
Filter residue is sent into corresponding reaction kettle.
Wherein, the first inspissator is an effect inspissator, and two female inspissators are Three-effect concentration device.
Wherein, dilute hydrochloric acid, ammonium hydroxide and liquefied ammonia are unified provides, and NaOH solution is to deploy when using, then the in above structure
One decoloring reaction kettle, the second decoloring reaction kettle, two female decoloring reaction kettles, three female sour neutralization reaction kettles and three female decoloring reaction kettles etc.
It provides device with dilute hydrochloric acid to connect for providing dilute hydrochloric acid, ammonia neutralization reaction kettle and two female neutralization reaction kettles etc. are mentioned with ammonium hydroxide
It connect and is used for liquefied ammonia offer device for providing ammonium hydroxide, two female ammonolysis reaction kettles and three female ammonolysis reaction kettles for device connection
Liquefied ammonia is provided.
Further, which further includes arginine workshop section or compound amino acid workshop section, the filtrate of the first plate and frame filter press
Outlet is connect with arginine workshop section or compound amino acid workshop section for producing arginine or compound amino acid.
Wherein, HCl recovery structure includes reflux condensing tube, Vacuuming structure, condenser, diluted acid storage tank and water scrubber etc..
Wherein, reflux condensing tube is set to the top of hydrolytic reaction pot and the import connection of its gas outlet and condenser, the outlet of condenser
Mouth is connect with Vacuuming structure, and the exhaust outlet of Vacuuming structure and water scrubber is connect with exhaust treatment system, the exhaust gas of water scrubber
The gas outlet of import neutralization with alkali reaction kettle connects, the diluted acid outlet of water scrubber, the first inspissator condensation-water drain（Condensed water
In contain a small amount of dilute hydrochloric acid）It is connect with the import of diluted acid storage tank with the liquid outlet of condenser, the outlet and dissolution of diluted acid storage tank
The feed inlet of tank connects.Wherein, reflux condensing tube is used for cooling steam, specifically can be with by hydrochloric acid reflux into hydrolytic reaction pot
For spherical, snakelike or straight configuration, preferably dimroth's condensing tube.Wherein, condenser is the condensation for being commonly used in recycling
Device.Wherein, Vacuuming structure is vacuum pump, wherein water scrubber is circulating water wash structure, is internally provided with spray head and concentration
Washing acid is sent into diluted acid storage tank when its concentration reaches certain value by meter.Further, condenser and Vacuuming structure it
Between be equipped with alkali cleaning structure.
Wherein, a plate and frame filter press can be shared in above structure, in each step or shares a reaction kettle, such as third
Plate and frame filter press and the 4th plate and frame filter press can be realized that such as the first decoloring reaction kettle and second takes off by the same plate and frame filter press
Colour response kettle can be realized that is, above-mentioned connection relationship is mainly functionally defined by same reaction kettle, be not intended as this
The restriction of invention.But in actual production process, in order to produce smooth progress, aforementioned each structure is all real by individual structure
It is existing.
Wherein, " first " in foregoing description, " second " ... wait descriptions to be served only for distinguishing, to facilitate description, without
Other Special Significances.
Technical solution provided in an embodiment of the present invention has the beneficial effect that：The embodiment of the invention provides a kind of feathers to produce
The device of a variety of amino acid, the device have carried out many places adjustment on the basis of existing production technology, to reduce cost and mention
The yield of high product, meanwhile, technique provided by the invention is more smooth, is suitble to industrialized production.
Detailed description of the invention
To describe the technical solutions in the embodiments of the present invention more clearly, make required in being described below to embodiment
Attached drawing is briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for
For those of ordinary skill in the art, without creative efforts, it can also be obtained according to these attached drawings other
Attached drawing.
Fig. 1 is the structural block diagram for the device that feather provided in an embodiment of the present invention produces a variety of amino acid；
Fig. 2 is the structural block diagram of HCl recovery structure provided in an embodiment of the present invention；
Fig. 3 is the process flow chart of cystine workshop section provided in an embodiment of the present invention；
Fig. 4 is the process flow chart of leucine workshop section provided in an embodiment of the present invention；
Fig. 5 is the process flow chart of tyrosine workshop section provided in an embodiment of the present invention.
Specific embodiment
To make the object, technical solutions and advantages of the present invention clearer, below in conjunction with attached drawing to embodiment party of the present invention
Formula is described in further detail.
Referring to Fig. 1, the embodiment of the invention provides the device that a kind of feather produces a variety of amino acid, which includes Guang ammonia
Sour workshop section, leucine workshop section and tyrosine workshop section etc..
Wherein, referring to Fig. 1, cystine workshop section includes HCl recovery structure 1 and the hydrolytic reaction pot 2, first that sets gradually
Inspissator 3, alkali neutralization reaction kettle 4, sedimentation basin 5, the first plate and frame filter press 6, dissolving tank 7, sour neutralization reaction kettle 8, the second sheet frame
Filter press 9, the first decoloring reaction kettle 10, third plate and frame filter press 11, the second decoloring reaction kettle 12, the 4th plate and frame filter press 13,
Ammonia neutralization reaction kettle 14 and the first centrifuge 15 etc..Wherein, HCl recovery structure 1 and hydrolytic reaction pot 2, the first inspissator 3, alkali
Neutralization reaction kettle 4 and dissolving tank 7 connect, and the sludge outlet of the 4th plate and frame filter press 13 passes through structure for conveying and the first decoloring reaction
The feed inlet of kettle 10 connects.
Wherein, referring to Fig. 1, leucine workshop section includes material-compound tank 37 and the two female inspissators 16, condensation reaction set gradually
The female ammonolysis reaction kettle 20 of kettle 17, cooling reactor 18, the 5th plate and frame filter press 19, two, the female decoloring reaction of the 6th plate and frame filter press 21, two
The female ammonia neutralization reaction kettle 24 of kettle 22, the 7th plate and frame filter press 23, two and two female centrifuges 25 etc..Wherein, material-compound tank 37 and condensation
The feed inlet of reaction kettle 17 connects, and the liquid feeding end of two female inspissators 16 is connect with the filtrate (liquid of the second plate and frame filter press 9.
Preferably, the filtrate (liquid of the 5th plate and frame filter press 19 is connect bright for improving with the feed inlet of condensation reaction kettle 17
The yield of propylhomoserin.
Wherein, referring to Fig. 1, tyrosine workshop section includes the female alkali neutralization reaction of the first alkali soluble reaction kettle 26, three set gradually
The female sour neutralization reaction kettle 31 of kettle 27, the 8th plate and frame filter press 28, the second alkali soluble reaction kettle 29, the 9th plate and frame filter press 30, three, the
The female ammonolysis reaction kettle 35 of the female decoloring reaction kettle 33 of ten plate and frame filter press 32, three, the 11st plate and frame filter press 34, three and three female centrifugations
The centrifugate of machine 36 etc., the feed inlet of the first alkali soluble reaction kettle 26 and the first centrifuge 15 exports connection, the 11st plate compression
The sludge outlet of machine 34 is connect by structure for conveying with the feed inlet of the second alkali soluble reaction kettle 29.
Preferably, the charging that the sludge outlet of the 9th plate and frame filter press 30 passes through structure for conveying and two female decoloring reaction kettles 22
Mouth connection is for recycling waste active carbon（Certainly, it directly can also be manually transported through by cart here）.8th sheet frame pressure
The filtrate (liquid of filter 28 connect the yield for improving leucine with the feed inlet of two female ammonolysis reaction kettles 20.
Aforementioned structure is sequentially connected with essentially by pipeline, and kinetic pump, valve and flow valve are set as needed on pipeline.Together
When, aforementioned each structure is all acidproof or caustic corrosion structure, and reaction kettle is enamel reaction still or glass reaction kettle.Further,
Two layers of the setting in each workshop point, reaction kettle are set to one layer, and plate and frame filter press is set to two layers.Wherein, for conveying the conveying knot of filter residue
Structure includes that detachable inclined plate and one side collecting tank disposed in parallel are arranged below the slag-drip opening of plate and frame filter press, and inclined plate will be filtered
Slag is sent into collecting tank, and filter residue is sent into reaction kettle by collecting tank by conveyer belt or delivery chute.
Further, which further includes arginine workshop section or compound amino acid workshop section, the filtrate of the first plate and frame filter press 6
Outlet is connect with arginine workshop section or compound amino acid workshop section for producing arginine or compound amino acid.
Wherein, referring to fig. 2, HCl recovery structure 1 includes reflux condensing tube 38, Vacuuming structure 39, condenser 40, diluted acid
Storage tank 41 and water scrubber 42 etc..Wherein, reflux condensing tube 38 is set to top and its gas outlet and the condenser 40 of hydrolytic reaction pot 2
Import connection, the gas outlet of condenser 40 connect with Vacuuming structure 39, the exhaust outlet and water scrubber 42 of Vacuuming structure 39
Exhaust outlet connect with exhaust treatment system, the connection of the gas outlet of the exhaust gas inlet neutralization with alkali reaction kettle 4 of water scrubber 42, water
The liquid outlet of the diluted acid outlet, the condensation-water drain of the first inspissator 3 and condenser 40 of washing tower 42 with diluted acid storage tank 41 into
Mouth connection, the outlet of diluted acid storage tank 41 and dissolving tank 7 connect.
Referring to Fig. 3-5, the process flow of above-mentioned apparatus is illustrated below, is included the following steps：
Wherein, referring to Fig. 3, cystine workshop section includes the following steps：
101 hydrolysis：4 tons of drake feathers after selecting hair machine to select hair are sent into 15 cubes of hydrolytic reaction pot 2 and use the hydrochloric acid of 30wt%
It is hydrolyzed, hydrolysis temperature is 115 DEG C, hydrolysis time 5h, drake feather（Dry weight）Mass ratio with hydrochloric acid is 1:1.8, while hydrochloric acid
It is spare that recovery structure 1 recycles hydrochloric acid.
102 concentrations：The first inspissator 3 of hydrolyzate that step 101 obtains is concentrated into the 1/3 of original weight amount, thickening temperature
It is 90 DEG C, while the recycling hydrochloric acid of HCl recovery structure 1 is spare, obtains about 3 tons of concentrates.
103 alkali neutralizations：The concentrate that 10 tons of steps 102 are obtained is sent into alkali neutralization reaction kettle 4, and is added
500KgNa2CO3The NaOH solution of solid and 3 tons of 30wt% are reacted, and 70 DEG C of reaction temperature, reaction time 8h, while hydrochloric acid returns
It is spare to receive the recycling hydrochloric acid of structure 1.
104 1 mother stocks from：The neutralizer that step 103 is obtained is sent into sedimentation basin 5 natural subsidence 30 hours, is re-fed into the
Filters pressing is carried out in one plate and frame filter press 6, a mother liquor is obtained and send arginine workshop section or compound amino acid workshop section for producing arginine
Or compound fertilizer, filter residue send dissolving tank 7 by structure for conveying.
105 acid neutralize；The step of filter residue that step 104 is obtained is sent into dissolving tank 7, is recycled using HCl recovery structure 1
101, whole hydrochloric acid of 102 and 103 recycling are dissolved（Ratio be about filter residue and recycling hydrochloric acid mass ratio be 1:2.5 left
It is right）, adjustment pH is 0.85, after being completely dissolved, and is sent into sour neutralization reaction kettle 8,30wt% hydrochloric acid or HCl recovery structure 1 is added
The hydrochloric acid of recycling carries out sour neutralization, and adjustment pH is 0.55, reacts at room temperature the time 25 minutes, is sent into the second sheet frame pressure after the reaction was completed
Filter 9 carries out filters pressing, obtains secondary mother liquid and is sent into two female inspissators 16 for producing leucine, filter residue send first by structure for conveying
Decoloring reaction kettle 10.
106 primary decolorations：The filter residue that step 105 is obtained is sent into the first decoloring reaction kettle 10, and appropriate pure water, work is added
Property charcoal and 30wt% hydrochloric acid decolourize, and decolorization condition is：65 DEG C of temperature, pH 0.5, active carbon is the whole that step 107 generates
Waste active carbon the reaction time 30 minutes, is sent into third plate and frame filter press 11 after the completion of decoloration and carries out filters pressing, filtrate send the second decoloration
Reaction kettle 12, filter residue send Solid Waste Treatment.
107 secondary decolourizations：The filtrate that step 106 is obtained is sent into the second decoloring reaction kettle 12, and appropriate pure water, work is added
Property charcoal and 30wt% hydrochloric acid decolourize, and decolorization condition is：65 DEG C of temperature, pH 0.5, the usage amount of active carbon is fresh activity
20Kg/ tons of hairs of charcoal the reaction time 30 minutes, are sent into the 4th plate and frame filter press 13 after the completion of decoloration and carry out filters pressing, filter residue is returned
Receive active carbon send step 106 by structure for conveying（First decoloring reaction kettle 10）It uses, filtrate send ammonia neutralization reaction kettle 14.
108 ammonia neutralize：The filtrate that step 107 is obtained is sent into ammonia neutralization reaction kettle 14, and the ammonium hydroxide that 20wt% is added carries out
It neutralizes, neutrality condition is：75 DEG C of temperature, the usage amount of ammonium hydroxide is 200Kg/ tons of hairs, is sent into the first centrifuge 15 after the reaction was completed
It is centrifugated to obtain cystine crude product and mother liquor three times, mother liquor is sent into the first alkali soluble reaction kettle 26 for producing tyrosine, Guang three times
Propylhomoserin crude product send step 109.
The purification of 109 cystines：The cystine crude product that step 108 obtains is washed, dries and obtain after crushing cystine essence
Product, the chromatography detection through national regulations, the purity of cystine fine work is 95.4%, and yield is 47.1Kg hair per ton.
Wherein, referring to fig. 4, leucine workshop section includes the following steps：
201 2 female concentrations：The secondary mother liquid that step 105 is obtained is sent into two female inspissators 16（Triple effect）In, in 100 DEG C of conditions
Under, 17 Baume degrees are concentrated into, the concentrate after concentration send condensation reaction kettle 17.
202 contracting and：By volume the 1 of the concentrated sulfuric acid and ortho-xylene in material-compound tank 37：1, which carries out allotment reaction, obtains mixed liquor
18 cubes of concentrates spare, that step 201 is obtained（While hot）, 500L allotment after mixed liquor and 200KgNaCl be sent into condensation
In reaction kettle 17, it is sent into cooling reactor 18 after the reaction was completed and is cooled to room temperature, is re-fed into the 5th plate and frame filter press 19 and carries out filters pressing, filter
Slag send two female ammonolysis reaction kettles 20 by structure for conveying, is condensed in the feed inlet of filtrate return condensation reaction kettle 17.
203 2 female ammonolysis：The filter residue that step 202 is obtained is sent into two female ammonolysis reaction kettles 20, dissolution（Appropriate pure water and
The filtrate that step 302 obtains）Liquid feeding ammonia carries out ammonolysis afterwards, and aminolysis conditions are：95 DEG C of temperature, terminal pH is 8.0, and the time is to react
Subject to completion, the 6th plate and frame filter press 21 is sent to carry out filters pressing after the reaction was completed, filter residue send two female decoloring reactions by structure for conveying
Kettle 22.
204 2 female decolorations：The filter residue that step 203 is obtained is sent into two female decoloring reaction kettles 22, and appropriate pure water, work is added
Property charcoal and 30wt% hydrochloric acid decolourize, and decolorization condition is：80 DEG C of temperature, active carbon is the useless activity of whole that step 305 recycles
Charcoal, pH 1 reaction time 2 hours, send the 7th plate and frame filter press 23 to carry out filters pressing after the completion of decoloration, filtrate send two female ammonia to neutralize
Reaction kettle 24, certainly, the step can also use 15Kg/8 tons of hairs of fresh activity charcoal.
205 2 female ammonia neutralize：The filtrate that step 204 is obtained is sent in two female ammonia neutralization reaction kettles 24, and 30wt% ammonium hydroxide is added
Ammonolysis is carried out, aminolysis conditions are：Temperature 70 C, terminal pH are 4.6, the reaction time 20 minutes, send two female centrifugations after the reaction was completed
The centrifugation of machine 25 obtains leucine crude product, and leucine crude product send step 206.
The purification of 206 leucines：The leucine crude product that step 205 obtains is washed, dries and obtain after crushing leucine essence
Product, the chromatography detection through national regulations, the purity of leucine fine work is 95.5%, and yield is 34.7Kg hair per ton.
Wherein, the filtrate obtained in above process and centrifugate, which can return, applies.
Wherein, referring to Fig. 5, tyrosine workshop section includes the following steps：
301 alkali solubles：It is sent in the first alkali soluble reaction kettle 26 in the mother liquor three times that step 108 obtains, 30wt%NaOH solution is added
Alkali soluble is carried out, condition is：Temperature 70 C, the reaction time 5 hours, terminal pH was 12, sent three female alkali neutralization reactions after the reaction was completed
Kettle 27.
302 3 female alkali neutralizations：The reaction solution that step 301 is obtained is sent in three female alkali neutralization reaction kettles 27, and (NH is added4)2CO3Neutralization reaction is carried out, reaction condition is：To room temperature after being reacted while hot, terminal pH is 4.7, the reaction time 1 hour, instead
It should send the 8th plate and frame filter press 28 filters pressing after the completion, filter residue send the second alkali soluble reaction kettle 29 by structure for conveying, and filtrate send step
203（Two female ammonolysis reaction kettles 20）In the filter residue that obtains for dissolving step 202.
303 2 alkali solubles：The filter residue that step 302 is obtained is sent into the second alkali soluble reaction kettle 29, be added appropriate pure water,
Whole waste active carbons that 30wt%NaOH solution and step 305 generate are reacted, and reaction condition is：Temperature 70 C, pH 12,
Reaction time 5 hours, send the 9th plate and frame filter press 30 filters pressing after the reaction was completed, filter residue recovered carbon, filtrate send three female neutralizations
The active carbon of reaction kettle 31, recycling send step 204（Two female decoloring reaction kettles 22）Middle carry out decoloring reaction.
304 3 female acid neutralize：The filtrate that step 303 is obtained send three female neutralization reaction kettles 31, add 30wt% hydrochloric acid into
Row neutralization reaction, reaction condition are：Terminal is pH8.5, reacts at room temperature time 2 h, send the tenth plate compression after the reaction was completed
32 filters pressing of machine, filter residue send three female decoloring reaction kettles 33 by structure for conveying.
305 3 female decolorations：The filter residue that step 304 is obtained send three female decoloring reaction kettles 33, be added 12 times of weight pure water,
30wt% hydrochloric acid and fresh activity charcoal, decolorization condition are：Temperature 60 C, 20Kg/ tons of hairs of fresh activity charcoal, pH 0.5, when reaction
Between hour, decoloration after the completion of send the 11st plate and frame filter press 34 filters pressing, filter residue recovered carbon send the second alkali by structure for conveying
Molten reaction kettle 29, filtrate send three female ammonolysis reaction kettles 35.
306 3 female ammonolysis：The filtrate that step 305 is obtained is sent in three female ammonolysis reaction kettles 35, and liquefied ammonia is added and is reacted,
Reaction condition is：Temperature 70 C, terminal pH2.4, the reaction time 2 hours, filter-cloth filtering after the reaction was completed, filter residue send three it is female from
The drying centrifugation of scheming 36 obtains tyrosine crude product.
The purification of 307 tyrosine：The tyrosine crude product that step 306 obtains is washed, dries and obtain after crushing tyrosine essence
Product, the chromatography detection through national regulations, the purity of tyrosine fine work is 93.9%, and yield is 25.2Kg hair per ton.
Wherein, the filtrate obtained in above process and centrifugate, which can return, applies.
Wherein, dilute hydrochloric acid, ammonium hydroxide and liquefied ammonia are unified provides, and NaOH solution is to deploy when using, then the in above structure
The female sour neutralization reaction kettle 31 of the female decoloring reaction kettle 22, three of one decoloring reaction kettle 10, the second decoloring reaction kettle 13, two and three female decolorations
Reaction kettles 33 etc. provide device with dilute hydrochloric acid and connect for providing dilute hydrochloric acid, ammonia neutralization reaction kettle 14 and two female neutralization reaction kettles
24 equal devices that provide with ammonium hydroxide connects for providing ammonium hydroxide, and two female ammonolysis reaction kettles 20 and three mother's ammonolysis reaction kettles 35 are and liquid
Ammonia provides device connection for providing liquefied ammonia.
The embodiment of the invention provides the device that a kind of feather produces a variety of amino acid, which includes HCl recovery knot
Structure, hydrolytic reaction pot, the first inspissator, alkali neutralization reaction kettle, sedimentation basin, the first plate and frame filter press, dissolving tank, sour neutralization reaction
Kettle, the second plate and frame filter press, the first decoloring reaction kettle, third plate and frame filter press, the second decoloring reaction kettle, the 4th plate compression
Machine, ammonia neutralization reaction kettle, the first centrifuge, two female inspissators, condensation reaction kettle, cooling reactor, the 5th plate and frame filter press, two female ammonia
Solution reaction kettle, the 6th plate and frame filter press, two female decoloring reaction kettles, the 7th plate and frame filter press, two female ammonia neutralization reaction kettles, two it is female from
Scheming, the first alkali soluble reaction kettle, three female alkali neutralization reaction kettles, the 8th plate and frame filter press, the second alkali soluble reaction kettle, the 9th sheet frame pressure
Filter, three female sour neutralization reaction kettles, the tenth plate and frame filter press, three female decoloring reaction kettles, the 11st plate and frame filter press, three female ammonolysis
Reaction kettle and three female centrifuges, the device have carried out many places adjustment on the basis of existing process units, with reduce cost and
The yield of product is improved, meanwhile, each structure is common structure in device provided by the invention and connection relationship is simple, is convenient for back
Active carbon is received, it is compact-sized, it is suitble to industrialized production.
The above described specific embodiments of the present invention are not intended to limit the scope of the present invention..Any basis
Any other various changes and modifications that technical concept of the invention is made should be included in the guarantor of the claims in the present invention
It protects in range.
Claims (7)
1. a kind of feather produces the device of a variety of amino acid, including cystine workshop section, leucine workshop section and tyrosine workshop section,
It is characterized in that,
The cystine workshop section includes that HCl recovery structure and the hydrolytic reaction pot set gradually, the first inspissator, alkali neutralization are anti-
Answer kettle, sedimentation basin, the first plate and frame filter press, dissolving tank, sour neutralization reaction kettle, the second plate and frame filter press, the first decoloring reaction kettle,
Third plate and frame filter press, the second decoloring reaction kettle, the 4th plate and frame filter press, ammonia neutralization reaction kettle and the first centrifuge, the salt
Acid recovery structure is connect with hydrolytic reaction pot, the first inspissator, alkali neutralization reaction kettle and dissolving tank, the 4th plate and frame filter press
Sludge outlet connect with the feed inlet of the first decoloring reaction kettle by structure for conveying；
The leucine workshop section includes material-compound tank and the two female inspissators, condensation reaction kettle, cooling reactor, the 5th sheet frame set gradually
Filter press, two female ammonolysis reaction kettles, the 6th plate and frame filter press, two female decoloring reaction kettles, the 7th plate and frame filter press, two female ammonia neutralize
Reaction kettle and two female centrifuges, the material-compound tank are connect with the feed inlet of condensation reaction kettle, the liquid feeding end of described two female inspissators
It is connect with the filtrate (liquid of the second plate and frame filter press；
The tyrosine workshop section includes the first alkali soluble reaction kettle set gradually, three female alkali neutralization reaction kettles, the 8th plate compression
Machine, the second alkali soluble reaction kettle, the 9th plate and frame filter press, three female sour neutralization reaction kettles, the tenth plate and frame filter press, three female decoloring reactions
Kettle, the 11st plate and frame filter press, three female ammonolysis reaction kettles and three female centrifuges, the feed inlet of the first alkali soluble reaction kettle and the
The centrifugate of one centrifuge exports connection, and the sludge outlet of the 11st plate and frame filter press passes through structure for conveying and the second alkali soluble
The feed inlet of reaction kettle connects.
2. the device that feather according to claim 1 produces a variety of amino acid, which is characterized in that described device further includes essence
Propylhomoserin workshop section or compound amino acid workshop section, the filtrate (liquid and arginine workshop section or compound amino acid of first plate and frame filter press
Workshop section's connection.
3. the device that feather according to claim 1 produces a variety of amino acid, which is characterized in that the 9th plate compression
The sludge outlet of machine is connect by structure for conveying with the feed inlet of two female decoloring reaction kettles.
4. the device that feather according to claim 1 produces a variety of amino acid, which is characterized in that the 5th plate compression
The filtrate (liquid of machine is connect with the feed inlet of condensation reaction kettle.
5. the device that feather according to claim 1 produces a variety of amino acid, which is characterized in that the 8th plate compression
The filtrate (liquid of machine is connect with the feed inlet of two female ammonolysis reaction kettles.
6. the device that feather according to claim 1 produces a variety of amino acid, which is characterized in that first inspissator is
One effect inspissator, described two female inspissators are Three-effect concentration device.
7. the device that feather according to claim 1-6 produces a variety of amino acid, which is characterized in that the hydrochloric acid
Recovery structure includes reflux condensing tube, Vacuuming structure, condenser, diluted acid storage tank and water scrubber, and the reflux condensing tube is set to
The import of the top of hydrolytic reaction pot and its gas outlet and condenser connects, and the gas outlet of the condenser and Vacuuming structure connect
It connects, the connection of the gas outlet of the exhaust gas inlet neutralization with alkali reaction kettle of the water scrubber, it is the diluted acid outlet of the water scrubber, first dense
The condensation-water drain of contracting device and the liquid outlet of condenser are connect with the import of diluted acid storage tank, the outlet of the diluted acid storage tank and molten
Solve the feed inlet connection of tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710337485.7A CN108863868A (en) | 2017-05-15 | 2017-05-15 | A kind of feather produces the device of a variety of amino acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710337485.7A CN108863868A (en) | 2017-05-15 | 2017-05-15 | A kind of feather produces the device of a variety of amino acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108863868A true CN108863868A (en) | 2018-11-23 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710337485.7A Pending CN108863868A (en) | 2017-05-15 | 2017-05-15 | A kind of feather produces the device of a variety of amino acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108863868A (en) |
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2017
- 2017-05-15 CN CN201710337485.7A patent/CN108863868A/en active Pending
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