CN106866476A - A kind of feather produces the device of several amino acids - Google Patents
A kind of feather produces the device of several amino acids Download PDFInfo
- Publication number
- CN106866476A CN106866476A CN201510911531.0A CN201510911531A CN106866476A CN 106866476 A CN106866476 A CN 106866476A CN 201510911531 A CN201510911531 A CN 201510911531A CN 106866476 A CN106866476 A CN 106866476A
- Authority
- CN
- China
- Prior art keywords
- female
- plate
- filter press
- frame filter
- reaction kettle
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
-
- 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses the device that a kind of feather produces several amino acids, belong to technical field of amino acid production.Device coproduction cystine, leucine and the tyrosine.Wherein, cystine workshop section include hydrolysis, concentration, alkali neutralize, a mother stock from, acid neutralize, once decolourings, secondary decolourization, ammonia neutralize and cystine refine；Wherein, leucine workshop section decolourizes including two female concentrations, condensation, two female ammonolysis, two mothers, two female ammonia are neutralized and leucine is refined；Wherein, tyrosine workshop section includes that alkali soluble, three mother's alkali neutralizations, secondary alkali soluble, three female sour neutralizations, three female decolourings, three female ammonolysis and a tyrosine are refined.The device has carried out many places adjustment on the basis of existing production technology, with the yield for reducing cost and improving product, meanwhile, the technique that the present invention is provided is more smooth, is adapted to industrialized production.
Description
Technical field
The present invention relates to technical field of amino acid production, more particularly to a kind of feather produces the device of several amino acids, more particularly to a kind of use drake feather or goose feather produce the device of cystine, tryptophan and tyrosine.
Background technology
Because world market is to the great demand of poultry meat product, butchering for birds produce substantial amounts of feather in process so that annual feather waste reaches millions of tons, and these feathers are as directly discarded, the degradation time that rots under field conditions (factors) is long, and rots smelly to pollute environment；As burning and burying needs substantial amounts of man power and material, it is also possible to cause secondary pollution, waste the resource of preciousness.Because feather contains substantial amounts of protein, amino acid is such as degraded to by the method for chemistry, has both been avoided the pollution of feather waste generation, but with good economic benefit, it is the best method for processing feather at present that can yet be regarded as.
The conventional method of amino-acids that is degraded to feather is acid hydrolyzation at present, acid hydrolyzation sends into acid hydrolysis tank feather after physical treatment, after repeatedly neutralizing and decolourizing, produce mother liquor, secondary mother liquid, three mother liquors and a Cystine Product, mother liquor, secondary mother liquid, three mother liquors send compound amino acid workshop section, leucine workshop section the amino acid different with tyrosine workshop section production respectively.Technological process to different workshop sections below is illustrated：
First, the technological process of cystine workshop section is：
1.1 hydrolysis sections
Raw material：Hair；Auxiliary material：Hydrochloric acid, steam；Hair is put into hydrolytic decomposition pot interior sealing, 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 caustic soda）；Hydrolyzate enters a neutralizing tank, is passed through liquefied ammonia（Or liquid caustic soda）；80 DEG C of temperature, neutralizes time 20h, terminal pH=5.0, filtering；Terminal product：1, filtrate（I.e. one time mother liquor, send L-arginine workshop to do raw material）2, filter residue（Go section of once decolourizing）.
1.3 once decolourize section
Auxiliary material：Hydrochloric acid, steam, pure water, activated carbon；Filter residue enters bleacher, throws（It is logical）Enter hydrochloric acid, steam, pure water, activated carbon；80 DEG C of temperature, bleaching time 2h, terminal pH=0.5, filtering；Terminal product：1, filter residue（Burning）2, filtrate（Remove secondary neutralizing zone）.
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, neutralizes time 12h, terminal pH=5.0, filtering；Terminal product：1, filtrate（I.e. secondary mother liquid, send L-Leu workshop to do raw material）2, filter residue（Go secondary decolourization section）.
1.5 secondary decolourizations section
Auxiliary material：Hydrochloric acid, steam, pure water, activated carbon；Filter residue enters bleacher, throws（It is logical）Enter hydrochloric acid, steam, pure water, activated carbon, 80 DEG C of temperature, bleaching time 2h, terminal pH=0.5, filtering；Terminal product：1, filter residue（Recycle）2, filtrate（Remove three neutralizing zones）.
1.6 3 neutralizing zones
Auxiliary material：Ammoniacal liquor；Filtrate enters three neutralizing tanks, is passed through ammoniacal liquor, and temperature 80 neutralizes time 3h, terminal pH=4.0, filtering；Terminal product：1, filtrate（I.e. three times mother liquors, send TYR workshop to do raw material）2, filter residue（I.e. CYSTINE crude product, removes refining stage）.
1.7 refining stages
Auxiliary material：Distilled water, steam；With distilled water flushing epimere process product and centrifuge dripping, dryer is sent into, be passed through steam drying, packed, storage, 100 DEG C of drying temperature, drying time 3h；Terminal product：CYSTINE finished product.
2nd, the technological process of leucine workshop section is：
2.1 enriching sections
Raw material：Steam；Secondary mother liquid is passed through in concentration tank, steam, 120 DEG C of temperature, air pressure -0.09MPa, concentration time 6h, crystallization is passed through；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, 80 DEG C of temperature neutralizes time 4h, filtering；Terminal product：1, filtrate（Recycle）2, filter residue（Go ammonolysis section）
2.3 ammonolysis section
Auxiliary material：Ammoniacal liquor, pure water, steam；Filter residue enters ammonolysis tank, is passed through ammoniacal liquor, pure water, steam, 80 DEG C of temperature, ammonolysis time 3h, filtering；Terminal product, 1, filtrate（Recycle）2, filter residue（Go decolouring section）(cystine).
2.4 decolouring sections
Auxiliary material：Steam, pure water, activated carbon；Filter residue enters bleacher, leads to（Throw）Enter steam, pure water, activated carbon, 80 DEG C of temperature, bleaching time 2h, filtering；Terminal product：1, filter residue（Recycle）2, filtrate（Remove secondary neutralizing zone）
2.5 2 neutralizing zones
Auxiliary material：Ammoniacal liquor, steam；Filtrate enters secondary neutralizing tank, is passed through ammoniacal liquor, and steam, 80 DEG C of temperature neutralizes time 4h, filtering；Terminal product, 1, filtrate（Recycle）2, filter residue（I.e. L-Leu crude product, removes refining stage）
2.6 refining stages
Auxiliary material：Distilled water, steam (histidine hydrochloride)；With distilled water flushing epimere process product and centrifuge dripping, dryer is sent into, be passed through steam drying, packed, storage, 100 DEG C of drying temperature, drying time 3h；Terminal product：L-Leu finished product.
The technological process of tyrosine workshop section is：
3.1 alkali solubles section
Raw material：Three mother liquors（Three neutralizing zone products in CYSTINE production）；Auxiliary material：Liquid caustic soda, pure water, activated carbon；Three mother liquors are passed through in alkali soluble tank, are led to（Throw）Enter liquid caustic soda, pure water, activated carbon, 90 DEG C of temperature, alkali soluble time 6h, filtering；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, and 80 DEG C of temperature neutralizes time 6h, terminal pH=8.5, filtering；Terminal product：1, filtrate（Recycle）2, filter residue（Go decolouring section）.
3.3 decolouring sections
Auxiliary material：Hydrochloric acid, steam, pure water, activated carbon；Filter residue enters bleacher, leads to（Throw）Enter hydrochloric acid, steam, pure water, activated carbon, 80 DEG C of temperature, bleaching time 2h, terminal pH=0.5, filtering；Terminal product：1, filter residue（Recycle）2, filtrate（Remove secondary neutralizing zone）.
3.4 2 neutralizing zones
Auxiliary material：Ammoniacal liquor；Filtrate enters secondary neutralizing tank, is passed through ammoniacal liquor, and 80 DEG C of temperature neutralizes time 4h, terminal pH=4.0, crystallization, filtering；Terminal product：1, filtrate（Recycle）2, filter residue（I.e. TYR crude product, removes refining stage）.
3.5 refining stages
Auxiliary material：Distilled water, steam；With distilled water flushing epimere process product and centrifuge dripping, dryer is sent into, be passed through steam drying, packed, storage, 100 DEG C of drying temperature, air pressure -0.09Mpa, drying time 5h.
When applicant states process in realization, it is found that the consumption of acid, alkali and activated carbon is big, cause production cost higher；Meanwhile, generate substantial amounts of waste water；In addition, the yield of cystine, leucine and tyrosine is relatively low.
The content of the invention
In order to solve the above problems, it is an object of the invention to provide the device that a kind of feather produces several amino acids, for reduces cost and raising yield, to obtain bigger economic benefit.The technical scheme is as follows：
The embodiment of the present invention additionally provides the device that a kind of feather produces several amino acids, and the device is including cystine workshop section, leucine workshop section and tyrosine workshop section etc..
Wherein, cystine workshop section includes HCl recovery structure and the hydrolytic reaction pot for setting gradually, 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, the 3rd 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 etc..Wherein, HCl recovery structure is connected to reclaim the watery hydrochloric acid of hydrolytic reaction pot, the first inspissator and alkali neutralization reaction kettle discharge with hydrolytic reaction pot, the first inspissator, alkali neutralization reaction kettle and dissolving tank, and the sludge outlet of the 4th plate and frame filter press is connected to recycle waste active carbon by the charging aperture of structure for conveying and the first decoloring reaction kettle.
Liquid is realized transporting by pipeline 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 for setting gradually, condensation reaction kettle, cooling reactor, the 5th 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 female ammonia neutralization reaction kettles and two female centrifuges etc..Wherein, material-compound tank is connected to allotment sulfuric acid with ortho-xylene to obtain ortho-xylene -4- sulfonic acid with the charging aperture of condensation reaction kettle, and the liquid feeding end of two female inspissators is connected with the filtrate (liquid of the second plate and frame filter press.Preferably, the filtrate (liquid of the 5th plate and frame filter press is connected to improve the yield of leucine with the charging aperture of condensation reaction kettle.
Liquid is realized transporting by pipeline in pre-structure, and filter residue is transported by structure for conveying.
Wherein, tyrosine workshop section is including the first alkali soluble reactor, three female alkali neutralization reaction kettles, the 8th plate and frame filter press, the second alkali soluble reactor, the 9th plate and frame filter press, three female acid 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 kettles and the three female centrifuges for setting gradually etc., the charging aperture of the first alkali soluble reactor is connected with the centrifugate outlet of the first centrifuge, and the sludge outlet of the 11st plate and frame filter press is connected to recycle waste active carbon by the charging aperture of structure for conveying and the second alkali soluble reactor.
Preferably, the sludge outlet of the 9th plate and frame filter press is connected to recycle waste active carbon by the charging aperture of structure for conveying and two female decoloring reaction kettles（Certainly, directly can also manually be transported by go-cart here）.The charging aperture of the filtrate (liquid of the 8th plate and frame filter press and two female ammonolysis reaction kettles is connected to improve the yield of leucine.
Liquid is realized transporting by pipeline in pre-structure, and filter residue is transported by structure for conveying.
In aforementioned structure, each structure is sequentially connected with essentially by pipeline（The conveying of wherein filter residue is transported by structure for conveying）, the structures such as kinetic pump, valve and flow valve are arranged as required on pipeline.Meanwhile, foregoing each structure is all acidproof or caustic corrosion structure, and reactor is enamel reaction still or glass reaction kettle（Capacity uses 10 cubes, 15 cubes or 20 cubes as needed）, each reactor is arranged as required to stirring, thermometer, barometer, insulation jacket, cooling water jecket etc. or is connected with exhaust treatment system.Further, each workshop point two-layer is set, and each reactor or sedimentation basin or dissolving tank etc. are located at one layer, and plate and frame filter press is located at two layers.Structure for conveying includes that the slag-drip opening lower section of plate and frame filter press sets detachable swash plate and its side（Slag-drip opening side）The collecting tank be arrangeding in parallel, swash plate is sent into filter residue in collecting tank, during filter residue is sent into corresponding reactor by collecting tank by conveyer belt or delivery chute.
Wherein, the first inspissator is an effect inspissator, and two female inspissators are Three-effect concentration device.
Wherein, the unification of watery hydrochloric acid, ammoniacal liquor and liquefied ammonia is provided, and NaOH solution is to be allocated when using, then the first decoloring reaction kettle, the second decoloring reaction kettle, two female decoloring reaction kettles, three female acid neutralization reaction kettles and three female decoloring reaction kettles etc. are connected to provide watery hydrochloric acid with watery hydrochloric acid offer device in said structure, ammonia neutralization reaction kettle and two female neutralization reaction kettles etc. are connected to provide ammoniacal liquor with ammoniacal liquor offer device, and two female ammonolysis reaction kettles and three female ammonolysis reaction kettles are connected to provide liquefied ammonia with liquefied ammonia offer device.
Further, the device also includes arginine workshop section or compound amino acid workshop section, and filtrate (liquid and the arginine workshop section or compound amino acid workshop section of the first plate and frame filter press are connected to produce arginine or compound amino acid.
Wherein, HCl recovery structure is including reflux condensing tube, Vacuuming structure, condenser, diluted acid storage tank and water scrubber etc..Wherein, reflux condensing tube is connected located at the top and its gas outlet of hydrolytic reaction pot with the import of condenser, the gas outlet of condenser is connected with Vacuuming structure, the exhaust outlet of Vacuuming structure and water scrubber is connected with exhaust treatment system, the exhaust gas inlet of water scrubber is connected with the gas outlet of alkali neutralization reaction kettle, the diluted acid outlet of water scrubber, the condensation-water drain of the first inspissator（Contain a small amount of watery hydrochloric acid in condensed water）Import with the liquid outlet of condenser with diluted acid storage tank is connected, the outlet of diluted acid storage tank and the charging aperture connection of dissolving tank.Wherein, reflux condensing tube is used for cooling steam, by hydrochloric acid reflux to hydrolytic reaction pot, is specifically as follows spherical, snakelike or straight configuration, preferably dimroth's condensing tube.Wherein, condenser is the condenser for being commonly used in recovery.Wherein, Vacuuming structure is vavuum pump, wherein, water scrubber is circulating water wash structure, is internally provided with spray head and densimeter, when its concentration reaches certain value, by washing acid feeding diluted acid storage tank.Further, alkali cleaning structure is provided between condenser and Vacuuming structure.
Wherein, in said structure, a plate and frame filter press can be shared in each step or a reactor is shared, as the 3rd plate and frame filter press and the 4th plate and frame filter press can be realized by same plate and frame filter press, as the first decoloring reaction kettle and the second decoloring reaction kettle can be realized by same reactor, i.e. above-mentioned annexation is mainly functionally defined, and is not intended as restriction of the invention.But in actual production process, in order to produce the carrying out of smoothness, foregoing each structure is all realized by single structure.
Wherein, " first " in foregoing description, " second " ... wait description to be served only for distinguishing, to facilitate description, without other Special Significances.
Technical scheme provided in an embodiment of the present invention has the beneficial effect that：The device that a kind of feather produces several amino acids is the embodiment of the invention provides, the device has carried out many places adjustment on the basis of existing production technology, with the yield for reducing cost and improving product, meanwhile, the technique that the present invention is provided is more smooth, is adapted to industrialized production.
Brief description of the drawings
Technical scheme in order to illustrate more clearly the embodiments of the present invention, the accompanying drawing to be used needed for being described to embodiment below is briefly described, apparently, drawings in the following description are only some embodiments of the present invention, for those of ordinary skill in the art, on the premise of not paying creative work, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is the structured flowchart of the device that feather provided in an embodiment of the present invention produces several amino acids；
Fig. 2 is the structured flowchart of HCl recovery structure provided in an embodiment of the present invention；
Fig. 3 is the process chart of cystine workshop section provided in an embodiment of the present invention；
Fig. 4 is the process chart of leucine workshop section provided in an embodiment of the present invention；
Fig. 5 is the process 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 accompanying drawing, embodiment of the present invention is described further in detail.
Referring to Fig. 1, the embodiment of the invention provides the device that a kind of feather produces several amino acids, the device include cystine 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 for setting gradually, the first 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 plate and frame filter press 9, the first decoloring reaction kettle 10, the 3rd 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 is connected with hydrolytic reaction pot 2, the first inspissator 3, alkali neutralization reaction kettle 4 and dissolving tank 7, and the sludge outlet of the 4th plate and frame filter press 13 is connected by structure for conveying with the charging aperture of the first decoloring reaction kettle 10.
Wherein, referring to Fig. 1, leucine workshop section includes material-compound tank 37 and the two female inspissators 16 for setting gradually, condensation reaction kettle 17, cooling reactor 18, the female ammonolysis reaction kettle 20 of the 5th plate and frame filter press 19, two, the female decoloring reaction kettle 22 of the 6th plate and frame filter press 21, two, the female centrifuge 25 of the mother's ammonia neutralization reaction of the 7th plate and frame filter press 23, two kettle 24 and two etc..Wherein, material-compound tank 37 is connected with the charging aperture of condensation reaction kettle 17, and the liquid feeding end of two female inspissators 16 is connected 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 connected to improve the yield of leucine with the charging aperture of condensation reaction kettle 17.
Wherein, referring to Fig. 1, tyrosine workshop section includes the first alkali soluble reactor 26 for setting gradually, three female alkali neutralization reaction kettles 27, 8th plate and frame filter press 28, second alkali soluble reactor 29, 9th plate and frame filter press 30, three female acid neutralization reaction kettles 31, tenth plate and frame filter press 32, three female decoloring reaction kettles 33, 11st plate and frame filter press 34, female centrifuge 36 of three female ammonolysis reaction kettle 35 and three etc., the charging aperture of the first alkali soluble reactor 26 is connected with the centrifugate outlet of the first centrifuge 15, the sludge outlet of the 11st plate and frame filter press 34 is connected by structure for conveying with the charging aperture of the second alkali soluble reactor 29.
Preferably, the sludge outlet of the 9th plate and frame filter press 30 is connected to recycle waste active carbon by the charging aperture of structure for conveying and two female decoloring reaction kettles 22（Certainly, directly can also be manually transported through by go-cart here）.The charging aperture of the filtrate (liquid of the 8th plate and frame filter press 28 and two female ammonolysis reaction kettles 20 is connected to improve the yield of leucine.
Aforementioned structure is sequentially connected with essentially by pipeline, and kinetic pump, valve and flow valve are arranged as required on pipeline.Meanwhile, foregoing each structure is all acidproof or caustic corrosion structure, and reactor is enamel reaction still or glass reaction kettle.Further, each workshop point two-layer is set, and reactor is located at one layer, and plate and frame filter press is located at two layers.Wherein, structure for conveying for conveying filter residue includes that the slag-drip opening lower section of plate and frame filter press sets the collecting tank that detachable swash plate and its side be arranged in parallel, swash plate is sent into filter residue in collecting tank, and collecting tank is by conveyer belt or delivery chute by filter residue feeding reactor.
Further, the device also includes arginine workshop section or compound amino acid workshop section, and filtrate (liquid and the arginine workshop section or compound amino acid workshop section of the first plate and frame filter press 6 are connected to produce 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 connected located at the top and its gas outlet of hydrolytic reaction pot 2 with the import of condenser 40, the gas outlet of condenser 40 is connected with Vacuuming structure 39, the exhaust outlet of Vacuuming structure 39 and the exhaust outlet of water scrubber 42 are connected with exhaust treatment system, the exhaust gas inlet of water scrubber 42 is connected with the gas outlet of alkali neutralization reaction kettle 4, import of the liquid outlet of the diluted acid outlet, the condensation-water drain of the first inspissator 3 and condenser 40 of water scrubber 42 with diluted acid storage tank 41 is connected, and the outlet of diluted acid storage tank 41 and dissolving tank 7 are connected.
Referring to Fig. 3-5, the technological process to said apparatus below is illustrated, comprised the following steps：
Wherein, referring to Fig. 3, cystine workshop section comprises the following steps：
101 hydrolysis：It is hydrolyzed with the hydrochloric acid of 30wt% in the hydrolytic reaction pot 2 that 4 tons of drake feathers after selecting hair machine to select hair are sent into 15 cubes, hydrolysis temperature is 115 DEG C, hydrolysis time 5h, drake feather（Dry weight）It is 1 with the mass ratio of hydrochloric acid:1.8, while the recovery hydrochloric acid of HCl recovery structure 1 is standby.
102 concentrations：The first inspissator 3 of the hydrolyzate that step 101 is obtained is concentrated into the 1/3 of original weight amount, and thickening temperature is 90 DEG C, while the recovery hydrochloric acid of HCl recovery structure 1 is standby, obtains about 3 tons of concentrates.
103 alkali are neutralized：In the concentrate feeding alkali neutralization reaction kettle 4 that 10 tons of steps 102 are obtained, and add 500KgNa2CO3The NaOH solution of solid and 3 tons of 30wt% is reacted, 70 DEG C of reaction temperature, reaction time 8h, while the recovery hydrochloric acid of HCl recovery structure 1 is standby.
104 1 mother stocks from：Natural subsidence 30 hours in the neutralizer feeding sedimentation basin 5 that step 103 is obtained, it is re-fed into carrying out press filtration in the first plate and frame filter press 6, obtaining a mother liquor send arginine workshop section or compound amino acid workshop section for producing arginine or composite fertilizer, and filter residue send dissolving tank 7 by structure for conveying.
105 acid are neutralized；The filter residue feeding dissolving tank 7 that step 104 is obtained, whole hydrochloric acid of 101,102 and 103 recovery are dissolved the step of is reclaimed using HCl recovery structure 1（It is 1 that ratio is about filter residue with the mass ratio for reclaiming hydrochloric acid:2.5 or so）Adjustment pH is 0.85, after being completely dissolved, in the sour neutralization reaction kettle 8 of feeding, the hydrochloric acid for adding 30wt% hydrochloric acid or HCl recovery structure 1 to reclaim carries out sour neutralization, and adjustment pH is 0.55,25 minutes room temperature reaction time, the second plate and frame filter press 9 is sent into after the completion of reaction carries out press filtration, and obtaining the female inspissator 16 of secondary mother liquid feeding two is used to produce leucine, and filter residue send the first decoloring reaction kettle 10 by structure for conveying.
106 once decolourize：The filter residue that step 105 is obtained is sent into the first decoloring reaction kettle 10, adds appropriate pure water, activated carbon and 30wt% hydrochloric acid to be decolourized, and decolorization condition is：65 DEG C of temperature, pH is 0.5, and activated carbon is whole waste active carbons that step 107 is produced, and in 30 minutes reaction time, the 3rd plate and frame filter press 11 is sent into after the completion of decolouring carries out press filtration, and filtrate send the second decoloring reaction kettle 12, and 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, adds appropriate pure water, activated carbon and 30wt% hydrochloric acid to be decolourized, and decolorization condition is：65 DEG C of temperature, pH is 0.5, and the usage amount of activated carbon is 20Kg/ ton hair of fresh activity charcoal, 30 minutes reaction time, and the 4th plate and frame filter press 13 of feeding carries out press filtration after the completion of decolouring, filter residue reclaim activated carbon send step 106 by structure for conveying（First decoloring reaction kettle 10）Use, filtrate send ammonia neutralization reaction kettle 14.
108 ammonia are neutralized：In the filtrate feeding ammonia neutralization reaction kettle 14 that step 107 is obtained, the ammoniacal liquor of 20wt% is added to be neutralized, neutrality condition is：75 DEG C of temperature, the usage amount of ammoniacal liquor is 200Kg/ tons of hair, the centrifugation of the first centrifuge 15 is sent into after the completion of reaction and obtains cystine crude product and three mother liquors, and three times the first alkali soluble reactor of mother liquor feeding 26 is used to produce tyrosine, and cystine crude product send step 109.
109 cystines are refined：Cystine crude product that step 108 is obtained is scrubbed, dry and obtain cystine fine work after crushing, and is detected through the chromatography of national regulations, and the purity of cystine fine work is 95.4%, and yield is 47.1Kg hairs per ton.
Wherein, referring to Fig. 4, leucine workshop section comprises the following steps：
201 2 female concentrations：The female inspissator 16 of secondary mother liquid feeding two that step 105 is obtained（Triple effect）In, under the conditions of 100 DEG C, 17 Baume degrees being 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 carries out allotment reaction obtains 18 cubes of concentrates that mixed liquor is standby, and step 201 is obtained（While hot）, in mixed liquor and 200KgNaCl feedings condensation reaction kettle 17 after 500L allotments, cooling reactor 18 is sent into after the completion of reaction and is cooled to room temperature, being re-fed into the 5th plate and frame filter press 19 carries out press filtration, filter residue send two female ammonolysis reaction kettles 20 by structure for conveying, is condensed in the charging aperture of filtrate return condensation reaction kettle 17.
203 2 female ammonolysis：In the female ammonolysis reaction kettle 20 of filter residue feeding two that step 202 is obtained, dissolving（The filtrate that appropriate pure water and step 302 are obtained）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 defined by reacting completion, send the 6th plate and frame filter press 21 to carry out press filtration after the completion of reaction, and filter residue send two female decoloring reaction kettles 22 by structure for conveying.
204 2 female decolourings：In the female decoloring reaction kettle 22 of filter residue feeding two that step 203 is obtained, appropriate pure water, activated carbon and 30wt% hydrochloric acid is added to be decolourized, decolorization condition is：80 DEG C of temperature, activated carbon is whole waste active carbons that step 305 is reclaimed, and pH is 1, in 2 hours reaction time, the 7th plate and frame filter press 23 is sent to carry out press filtration after the completion of decolouring, filtrate send two female ammonia neutralization reaction kettles 24, certainly, the step can also use 15Kg/8 tons of hair of fresh activity charcoal.
205 2 female ammonia are neutralized：In sending two female ammonia neutralization reaction kettles 24 by the filtrate that step 204 is obtained, 30wt% ammoniacal liquor is added to carry out ammonolysis, aminolysis conditions are：Temperature 70 C, terminal pH is 4.6,20 minutes reaction time, send two female centrifugations of centrifuge 25 to obtain leucine crude product after the completion of reaction, and leucine crude product send step 206.
206 leucines are refined：Leucine crude product that step 205 is obtained is scrubbed, dry and obtain leucine fine work after crushing, and is detected through the chromatography of national regulations, and the purity of leucine fine work is 95.5%, and yield is 34.7Kg hairs per ton.
Wherein, the filtrate for obtaining in above process and centrifugate can be returned applies mechanically.
Wherein, referring to Fig. 5, tyrosine workshop section comprises the following steps：
301 alkali solubles：In three mother liquors that step 108 is obtained send the first alkali soluble reactor 26,30wt%NaOH solution is added to carry out alkali soluble, condition is：Temperature 70 C, 5 hours reaction time, terminal pH is 12, and three female alkali neutralization reaction kettles 27 are sent after the completion of reaction.
302 3 female alkali are neutralized：In sending three female alkali neutralization reaction kettles 27 by the reaction solution that step 301 is obtained, and add (NH4)2CO3Neutralization reaction is carried out, reaction condition is：To room temperature after being reacted while hot, terminal pH is 4.7, in 1 hour reaction time, the press filtration of the 8th plate and frame filter press 28 is sent after the completion of reaction, and filter residue send the second alkali soluble reactor 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 reactor 29, and the whole waste active carbons for adding appropriate pure water, 30wt%NaOH solution and step 305 to produce are reacted, and reaction condition is：Temperature 70 C, pH is 12,5 hours reaction time, and the press filtration of the 9th plate and frame filter press 30, filter residue recovered carbon are sent after the completion of reaction, and filtrate send three female neutralization reaction kettles 31, and the activated carbon of recovery send step 204（Two female decoloring reaction kettles 22）In carry out decoloring reaction.
304 3 female acid are neutralized：Three female neutralization reaction kettles 31 are sent by the filtrate that step 303 is obtained, adding 30wt% hydrochloric acid carries out neutralization reaction, and reaction condition is：Terminal is pH8.5, and room temperature reaction time 2 h send the press filtration of the tenth plate and frame filter press 32 after the completion of reaction, filter residue send three female decoloring reaction kettles 33 by structure for conveying.
305 3 female decolourings：Three female decoloring reaction kettles 33 are sent by the filter residue that step 304 is obtained, adds 12 times of pure water of weight, 30wt% hydrochloric acid and the fresh activity charcoals, decolorization condition to be：Temperature 60 C, 20Kg/ tons of hair of fresh activity charcoal, pH is 0.5, the reaction time hour, and the press filtration of the 11st plate and frame filter press 34 is sent after the completion of decolouring, and filter residue recovered carbon send the second alkali soluble reactor 29 by structure for conveying, and filtrate send three female ammonolysis reaction kettles 35.
306 3 female ammonolysis：In sending three female ammonolysis reaction kettles 35 by the filtrate that step 305 is obtained, liquefied ammonia is added to be reacted, reaction condition is：Temperature 70 C, terminal is pH2.4, and 2 hours reaction time, filter-cloth filtering after the completion of reaction, filter residue send three female centrifuges 36 to dry centrifugation and obtains tyrosine crude product.
307 tyrosine are refined：Tyrosine crude product that step 306 is obtained is scrubbed, dry and obtain tyrosine fine work after crushing, and is detected through the chromatography of national regulations, and the purity of tyrosine fine work is 93.9%, and yield is 25.2Kg hairs per ton.
Wherein, the filtrate for obtaining in above process and centrifugate can be returned applies mechanically.
Wherein, the unification of watery hydrochloric acid, ammoniacal liquor and liquefied ammonia is provided, and NaOH solution is to be allocated when using, then female decoloring reaction kettle 33 of the female acid neutralization reaction kettle 31 and three of the female decoloring reaction kettle 22, three of the first decoloring reaction kettle 10, the second decoloring reaction kettle 13, two etc. is connected to provide watery hydrochloric acid with watery hydrochloric acid offer device in said structure, the female grade of neutralization reaction kettle 24 of ammonia neutralization reaction kettle 14 and two is connected to provide ammoniacal liquor with ammoniacal liquor offer device, and the female ammonolysis reaction kettle 35 of two female ammonolysis reaction kettle 20 and three is connected to provide liquefied ammonia with liquefied ammonia offer device.
The embodiment of the invention provides the device that a kind of feather produces several amino acids,The device includes HCl recovery structure,Hydrolytic reaction pot,First inspissator,Alkali neutralization reaction kettle,Sedimentation basin,First plate and frame filter press,Dissolving tank,Sour neutralization reaction kettle,Second plate and frame filter press,First decoloring reaction kettle,3rd plate and frame filter press,Second decoloring reaction kettle,4th plate and frame filter press,Ammonia neutralization reaction kettle,First centrifuge,Two female inspissators,Condensation reaction kettle,Cooling reactor,5th plate and frame filter press,Two female ammonolysis reaction kettles,6th plate and frame filter press,Two female decoloring reaction kettles,7th plate and frame filter press,Two female ammonia neutralization reaction kettles,Two female centrifuges,First alkali soluble reactor,Three female alkali neutralization reaction kettles,8th plate and frame filter press,Second alkali soluble reactor,9th plate and frame filter press,Three female acid neutralization reaction kettles,Tenth plate and frame filter press,Three female decoloring reaction kettles,11st plate and frame filter press,Three female ammonolysis reaction kettles and three female centrifuges,The device is on the basis of existing process units,Many places adjustment is carried out,With the yield for reducing cost and improving product,Simultaneously,Each structure is common structure and annexation is simple in the device that the present invention is provided,It is easy to recovered carbon,Compact conformation,It is adapted to industrialized production.
The specific embodiment of present invention described above, is not intended to limit the scope of the present invention..Various other corresponding change and deformation that any technology according to the present invention design is made, should be included in the protection domain of the claims in the present invention.
Claims (7)
1. a kind of feather produces the device of several amino acids, including cystine workshop section, leucine workshop section and tyrosine workshop section, it is characterised in that
The cystine workshop section includes HCl recovery structure and the hydrolytic reaction pot for setting gradually, first inspissator, alkali neutralization reaction kettle, sedimentation basin, first plate and frame filter press, dissolving tank, sour neutralization reaction kettle, second plate and frame filter press, first decoloring reaction kettle, 3rd plate and frame filter press, second decoloring reaction kettle, 4th plate and frame filter press, ammonia neutralization reaction kettle and the first centrifuge, the HCl recovery structure and hydrolytic reaction pot, first inspissator, alkali neutralization reaction kettle and dissolving tank are connected, the sludge outlet of the 4th plate and frame filter press is connected by structure for conveying with the charging aperture of the first decoloring reaction kettle；
The leucine workshop section includes material-compound tank and the two female inspissators, condensation reaction kettle, cooling reactor, the 5th 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 female ammonia neutralization reaction kettles and the two female centrifuges that set gradually, the material-compound tank is connected with the charging aperture of condensation reaction kettle, and the liquid feeding end of described two female inspissators is connected with the filtrate (liquid of the second plate and frame filter press；
The tyrosine workshop section includes the first alkali soluble reactor, three female alkali neutralization reaction kettles, the 8th plate and frame filter press, the second alkali soluble reactor, the 9th plate and frame filter press, three female acid 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 kettles and the three female centrifuges that set gradually, the charging aperture of the first alkali soluble reactor is connected with the centrifugate outlet of the first centrifuge, and the sludge outlet of the 11st plate and frame filter press is connected by structure for conveying with the charging aperture of the second alkali soluble reactor.
2. feather according to claim 1 produces the device of several amino acids, it is characterised in that described device also includes arginine workshop section or compound amino acid workshop section, and the filtrate (liquid of first plate and frame filter press is connected with arginine workshop section or compound amino acid workshop section.
3. feather according to claim 1 produces the device of several amino acids, it is characterised in that the sludge outlet of the 9th plate and frame filter press is connected by structure for conveying with the charging aperture of two female decoloring reaction kettles.
4. feather according to claim 1 produces the device of several amino acids, it is characterised in that the filtrate (liquid of the 5th plate and frame filter press is connected with the charging aperture of condensation reaction kettle.
5. feather according to claim 1 produces the device of several amino acids, it is characterised in that the filtrate (liquid of the 8th plate and frame filter press is connected with the charging aperture of two female ammonolysis reaction kettles.
6. feather according to claim 1 produces the device of several amino acids, it is characterised in that first inspissator is an effect inspissator, and described two female inspissators are Three-effect concentration device.
7. the feather according to claim any one of 1-6 produces the device of several amino acids, it is characterized in that, the HCl recovery structure includes reflux condensing tube, Vacuuming structure, condenser, diluted acid storage tank and water scrubber, the reflux condensing tube is connected located at the top and its gas outlet of hydrolytic reaction pot with the import of condenser, the gas outlet of the condenser is connected with Vacuuming structure, the exhaust gas inlet of the water scrubber is connected with the gas outlet of alkali neutralization reaction kettle, the diluted acid outlet of the water scrubber, the import of the condensation-water drain of the first inspissator and the liquid outlet of condenser with diluted acid storage tank is connected, the outlet of the diluted acid storage tank and the charging aperture connection of dissolving tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510911531.0A CN106866476A (en) | 2015-12-11 | 2015-12-11 | A kind of feather produces the device of several amino acids |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510911531.0A CN106866476A (en) | 2015-12-11 | 2015-12-11 | A kind of feather produces the device of several amino acids |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106866476A true CN106866476A (en) | 2017-06-20 |
Family
ID=59237643
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510911531.0A Pending CN106866476A (en) | 2015-12-11 | 2015-12-11 | A kind of feather produces the device of several amino acids |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106866476A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110981557A (en) * | 2019-12-10 | 2020-04-10 | 安徽尘缘节能环保科技有限公司 | System for preparing compound amino acid by microwave acidolysis of waste protein |
-
2015
- 2015-12-11 CN CN201510911531.0A patent/CN106866476A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110981557A (en) * | 2019-12-10 | 2020-04-10 | 安徽尘缘节能环保科技有限公司 | System for preparing compound amino acid by microwave acidolysis of waste protein |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108128826B (en) | Nitric acid-containing wastewater treatment device and treatment method | |
| CN105036141A (en) | Method for producing nanosilicon dioxide and by-product hydrochloric acid through chlorosilane waste gas | |
| CN104513174A (en) | Cyclic utilization process and device for waste acid produced during production of dinitolmide | |
| CN204824684U (en) | Cystine purification device | |
| CN204848706U (en) | Device of multiple amino acid is prepared to feather | |
| CN101117314A (en) | Production method of sodium citrate | |
| CN102206140A (en) | Method and production system for separating and recovering phenol oil and simultaneously producing sodium sulfite through sodium phenolate acidolysis | |
| CN103848929A (en) | Process for high-efficiently extracting sodium heparin | |
| CN106866476A (en) | A kind of feather produces the device of several amino acids | |
| CN204824149U (en) | Hydrochloric acid recovery unit of amino acid is produced to acid system | |
| CN204874354U (en) | Device of feather production cystine | |
| CN104529801A (en) | Synthetic method for p-hydroxyphenyl glycine | |
| CN206266463U (en) | It is a kind of to hydrolyze the decoloration device that feather produces amino acid system | |
| CN204874353U (en) | Device of cystine waste liquid production leucine | |
| CN106674071A (en) | Apparatus for preparing a variety of amino acids from feathers | |
| CN103265443A (en) | Industrial production method of high-purity iminodiacetic acid | |
| CN106496082B (en) | A kind of production method of compound amino acid powder spraying system and amino acid powder | |
| CN205933523U (en) | High salt organic wastewater of EDTA and resources recovery system | |
| CN204508823U (en) | Its Future about Alkaline Residue Treatment Unit is mixed in indigo production | |
| CN106866442A (en) | A kind of leucine process units | |
| CN108863868A (en) | A kind of feather produces the device of a variety of amino acid | |
| CN106866477A (en) | A kind of method that feather produces several amino acids | |
| CN108863869A (en) | A kind of method that feather produces a variety of amino acid | |
| CN106674072A (en) | Method for preparing a plurality of amino acids from feathers | |
| CN204848707U (en) | Device of cystine waste liquid production tyrosine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170620 |