CN204848706U - Device of multiple amino acid is prepared to feather - Google Patents
Device of multiple amino acid is prepared to feather Download PDFInfo
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- CN204848706U CN204848706U CN201520409492.XU CN201520409492U CN204848706U CN 204848706 U CN204848706 U CN 204848706U CN 201520409492 U CN201520409492 U CN 201520409492U CN 204848706 U CN204848706 U CN 204848706U
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Abstract
The utility model discloses a device of multiple amino acid is prepared to feather belongs to amino acid production technical field. The device coproduction cystine, leucine and tyrosine. Wherein, cystine workshop section including hydrolysis, concentration, alkali neutralization, a parent stock from, sour neutralization, once decolour, secondary decoloration, ammonia neutralization and cystine refine, wherein, leucine workshop section includes that two female concentrated, condensation, two mothers are ammonolyzed, two female decolorations, two female ammonia neutralizations and leucine be refined, wherein, tyrosine workshop section includes alkaline bath, three female alkali neutralizations, secondary alkaline bath, three female sour neutralizations, three female decolorations, three mothers are ammonolyzed and tyrosine refined. The device has carried out the many places adjustment on the basis of current production technology to the yield that reduces the cost and improve the product, simultaneously, the utility model provides a technology is more smooth, is fit for the industrial production.
Description
Technical field
The utility model relates to technical field of amino acid production, and particularly a kind of feather produces the device of multiple amino acids, particularly relates to a kind of device adopting drake feather or goose feather to produce Gelucystine, tryptophane and tyrosine.
Background technology
Because world market is to the great demand of poultry meat product, butchering in the course of processing of bird produces a large amount of feathers, and make annual feather waste reach millions of tons, these feathers are as directly discarded, rotten degradation time is long under field conditions (factors), and it is smelly to environment to rot; As burning and burying needs a large amount of man power and materials, also may cause secondary pollution, waste valuable resource.Because feather contains a large amount of protein, as being degraded to amino acid by the method for chemistry, both avoided the pollution that feather waste produces, have again good economic benefit, can yet be regarded as is the best method processing feather at present.
The method of amino-acids that is degraded to by feather of current routine is acid hydrolyzation, feather is sent in acid hydrolysis tank by acid hydrolyzation after physical treatment, after repeatedly neutralizing and decolouring, produce mother liquor, secondary mother liquid, three mother liquors and a Cystine Product, one time mother liquor, secondary mother liquid, three mother liquors send aminoacids complex workshop section, leucine workshop section and tyrosine workshop section to produce different amino acid respectively.Below the technical process of different workshop section is described:
One, the technical process of Gelucystine workshop section is: 1.1 hydrolysis section
Raw material: hair; Auxiliary material: hydrochloric acid, steam; Hair is dropped in hydrolytic decomposition pot and seals, pass into hydrochloric acid (concentration ﹥ 30%), steam; Temperature 120 DEG C, acidolysis time 7h; Terminal product: hydrolyzed solution (removing a neutralizing zone).
1.2 neutralizing zones
Auxiliary material: liquefied ammonia (or liquid caustic soda); Hydrolyzed solution enters a neutralization tank, passes into liquefied ammonia (or liquid caustic soda); Temperature 80 DEG C, in and time 20h, terminal pH=5.0, filter; Terminal product: 1, filtrate (i.e. a mother liquor, send L-arginine workshop to do raw material) 2, filter residue (going the once section of decolouring).
The 1.3 once sections of decolouring
Auxiliary material: hydrochloric acid, steam, pure water, gac; Filter residue enters bleacher, and throwing (leading to) enters hydrochloric acid, steam, pure water, gac; Temperature 80 DEG C, bleaching time 2h, terminal pH=0.5, filter; Terminal product: 1, filter residue (burning) 2, filtrate (going Two-step neutralization section).
1.4 Two-step neutralization sections
Auxiliary material: bicarbonate of ammonia; Filtrate enters Two-step neutralization tank, drops into bicarbonate of ammonia; Temperature 80 DEG C, in and time 12h, terminal pH=5.0, filter; Terminal product: 1, filtrate (i.e. secondary mother liquid send L-Leu workshop to do raw material) 2, filter residue (going secondary decolourization section).
1.5 secondary decolourization sections
Auxiliary material: hydrochloric acid, steam, pure water, gac; Filter residue enters bleacher, and throwing (leading to) enters hydrochloric acid, steam, pure water, gac, temperature 80 DEG C, bleaching time 2h, terminal pH=0.5, filters; Terminal product: 1, filter residue (recycling) 2, filtrate (removing three neutralizing zones).
1.6 3 neutralizing zones
Auxiliary material: ammoniacal liquor; Filtrate enters three neutralization tanks, passes into ammoniacal liquor, temperature 80, in and time 3h, terminal pH=4.0, filter; Terminal product: 1, filtrate (i.e. three mother liquors, send TYR workshop to do raw material) 2, filter residue (namely CYSTINE crude product, removes refining stage).
1.7 refining stage
Auxiliary material: distilled water, steam; With distilled water flushing epimere process product and centrifuge dripping, send into dryer, pass into drying with steam, packaging, warehouse-in, bake out temperature 100 DEG C, drying time 3h; Terminal product: CYSTINE finished product.
Two, the technical process of leucine workshop section is:
2.1 enriching section
Raw material: steam; Secondary mother liquid is passed in concentration tank, pass into steam, temperature 120 DEG C, air pressure-0.09MPa, concentration time 6h, crystallization; Terminal product: crystal solution (removing a neutralizing zone).
2.2 neutralizing zones
Auxiliary material: sulfuric acid, pure water; Crystal solution enters a neutralization tank, passes into sulfuric acid, pure water, temperature 80 DEG C, in and time 4h, filter; Terminal product: 1, filtrate (recycling) 2, filter residue (deammoniation solution section)
2.3 ammonia solution sections
Auxiliary material: ammoniacal liquor, pure water, steam; Filter residue enters ammonia solution tank, passes into ammoniacal liquor, pure water, steam, temperature 80 DEG C, ammonia solution time 3h, filters; Terminal product, 1, filtrate (recycling) 2, filter residue (going section of decolouring) (Gelucystine).
2.4 decolouring sections
Auxiliary material: steam, pure water, gac; Filter residue enters bleacher, and logical (throwing) enters steam, pure water, gac, temperature 80 DEG C, bleaching time 2h, filters; Terminal product: 1, filter residue (recycling) 2, filtrate (going Two-step neutralization section)
2.5 Two-step neutralization sections
Auxiliary material: ammoniacal liquor, steam; Filtrate enters Two-step neutralization tank, passes into ammoniacal liquor, steam, temperature 80 DEG C, in and time 4h, filter; Terminal product, 1, filtrate (recycling) 2, filter residue (namely L-Leu crude product, removes refining stage)
2.6 refining stage
Auxiliary material: distilled water, steam (L-Histidine hydrochloride); With distilled water flushing epimere process product and centrifuge dripping, send into dryer, pass into drying with steam, packaging, warehouse-in, bake out temperature 100 DEG C, drying time 3h; Terminal product: L-Leu finished product.
The technical process of tyrosine workshop section is:
Molten section of 3.1 alkali
Raw material: three mother liquors (in CYSTINE production three neutralizing zone products); Auxiliary material: liquid caustic soda, pure water, gac; Pass in the molten tank of alkali by three mother liquors, logical (throwing) enters liquid caustic soda, pure water, gac, temperature 90 DEG C, the molten time 6h of alkali, filters; Terminal product: 1, filter residue (recycling) 2, filtrate (removing a neutralizing zone).
3.2 neutralizing zones
Auxiliary material: hydrochloric acid; Filtrate enters a neutralization tank, passes into hydrochloric acid, temperature 80 DEG C, in and time 6h, terminal pH=8.5, filter; Terminal product: 1, filtrate (recycling) 2, filter residue (going section of decolouring).
3.3 decolouring sections
Auxiliary material: hydrochloric acid, steam, pure water, gac; Filter residue enters bleacher, and logical (throwing) enters hydrochloric acid, steam, pure water, gac, temperature 80 DEG C, bleaching time 2h, terminal pH=0.5, filters; Terminal product: 1, filter residue (recycling) 2, filtrate (going Two-step neutralization section).
3.4 Two-step neutralization sections
Auxiliary material: ammoniacal liquor; Filtrate enters Two-step neutralization tank, passes into ammoniacal liquor, temperature 80 DEG C, in and time 4h, terminal pH=4.0, crystallization, filter; Terminal product: 1, filtrate (recycling) 2, filter residue (namely TYR crude product, removes refining stage).
3.5 refining stage
Auxiliary material: distilled water, steam; With distilled water flushing epimere process product and centrifuge dripping, send into dryer, pass into drying with steam, packaging, warehouse-in, bake out temperature 100 DEG C, air pressure-0.09Mpa, drying time 5h.
When applicant states process in realization, find acid, alkali and gac consumption large, cause production cost higher; Meanwhile, a large amount of waste water is created; In addition, the output of Gelucystine, leucine and tyrosine is lower.
Summary of the invention
In order to solve the problem, the purpose of this utility model is to provide a kind of feather to produce the device of multiple amino acids, for reducing cost and raising productive rate, to obtain larger economic benefit.Described technical scheme is as follows:
The utility model embodiment still provides the device that a kind of feather produces multiple amino acids, and this device comprises Gelucystine workshop section, leucine workshop section and tyrosine workshop section etc.
Wherein, Gelucystine workshop section comprises HCl recovery structure and hydrolytic reaction pot, the first thickener, alkali neutralization reaction still, settling tank, the first plate-and-frame filter press, dissolving vessel, sour neutralization reaction still, the second plate-and-frame filter press, the first decoloring reaction still, the 3rd plate-and-frame filter press, the second decoloring reaction still, the 4th plate-and-frame filter press, ammonia neutralization reaction still and the first whizzer etc. that set gradually.Wherein, HCl recovery structure is connected the dilute hydrochloric acid being used for recycle-water solution reaction kettle, the first thickener and alkali neutralization reaction still and discharging with hydrolytic reaction pot, the first thickener, alkali neutralization reaction still and dissolving vessel, the sludge outlet of the 4th plate-and-frame filter press is connected for recycling waste active carbon by the opening for feed of structure for conveying with the first decoloring reaction still.
In pre-structure, liquid realizes transport by pipeline, and filter residue is transported by structure for conveying.
Wherein, leucine workshop section comprises material-compound tank and two female thickeners, condensation reaction still, cooling reactor, the 5th plate-and-frame filter press, two female ammonolysis reaction stills, the 6th plate-and-frame filter press, two female decoloring reaction stills, the 7th plate-and-frame filter press, two female ammonia neutralization reaction stills and the two female whizzers etc. that set gradually.Wherein, material-compound tank is connected with the opening for feed of condensation reaction still for allocating sulfuric acid and o-Xylol to obtain o-Xylol-4-sulfonic acid, and the liquid feeding end of two female thickeners is connected with the filtrate outlet of the second plate-and-frame filter press.Preferably, the filtrate outlet of the 5th plate-and-frame filter press is connected for improving leucic productive rate with the opening for feed of condensation reaction still.
In pre-structure, liquid realizes transport by pipeline, and filter residue is transported by structure for conveying.
Wherein, tyrosine workshop section comprises the molten reactor of the first alkali, three female alkali neutralization reaction stills, the 8th plate-and-frame filter press, the molten reactor of the second alkali, the 9th plate-and-frame filter press, three female sour neutralization reaction stills, the tenth plate-and-frame filter press, three female decoloring reaction stills, the 11 plate-and-frame filter press, three female ammonolysis reaction stills and the three female whizzers etc. that set gradually, the opening for feed of the molten reactor of the first alkali exports with the centrifugate of the first whizzer and is connected, and the sludge outlet of the 11 plate-and-frame filter press is connected for recycling waste active carbon by the opening for feed of structure for conveying with the molten reactor of the second alkali.
Preferably, the sludge outlet of the 9th plate-and-frame filter press is connected for recycling waste active carbon (certainly, also can directly manually be transported by go-cart) here with the opening for feed of two female decoloring reaction stills by structure for conveying.The filtrate outlet of the 8th plate-and-frame filter press is connected for improving leucic productive rate with the opening for feed of two female ammonolysis reaction stills.
In pre-structure, liquid realizes transport by pipeline, and filter residue is transported by structure for conveying.
In aforementioned structure, each structure connects (wherein the structure for conveying that is conducted through of filter residue transports) in turn essentially by pipeline, and pipeline arranges the structures such as power-driven pump, valve and flow valve as required.Simultaneously, aforementioned each structure is all acidproof or caustic corrosion structure, reactor is enamel reaction still or glass reaction still (capacity adopts 10 cubes, 15 cubes or 20 cubes as required), and each reactor arranges stirring, thermometer, weather gauge, insulation jacket, cooling water jecket etc. as required or is connected with exhaust treatment system.Further, two-layer setting is divided in each workshop, and each reactor or settling tank or dissolving vessel etc. are located at one deck, and plate-and-frame filter press is located at two layers.The receiving tank that detachable swash plate and its side (slag-drip opening side) be arranged in parallel is set below the slag-drip opening that structure for conveying comprises plate-and-frame filter press, filter residue is sent in receiving tank by swash plate, and filter residue is sent in corresponding reactor by conveying belt or conveyer trough by receiving tank.
Wherein, the first thickener is an effect thickener, and two female thickeners are Three-effect concentration device.
Wherein, dilute hydrochloric acid, ammoniacal liquor and liquefied ammonia are unified to be provided, and NaOH solution is allotment during use, then the first decoloring reaction still in said structure, the second decoloring reaction still, two female decoloring reaction stills, three female sour neutralization reaction stills are all connected with dilute hydrochloric acid generator with three female decoloring reaction stills etc. and are used for providing dilute hydrochloric acid, ammonia neutralization reaction still is all connected with ammoniacal liquor generator with two female neutralization reaction stills etc. and is used for providing ammoniacal liquor, and two female ammonolysis reaction stills are all connected with liquefied ammonia generator with three female ammonolysis reaction stills and are used for providing liquefied ammonia.
Further, this device also comprises arginine workshop section or aminoacids complex workshop section, and the filtrate outlet of the first plate-and-frame filter press is connected for the production of arginine or aminoacids complex with arginine workshop section or aminoacids complex workshop section.
Wherein, HCl recovery structure comprises reflux condensing tube, Vacuuming structure, condenser, diluted acid storage tank and water wash column etc.Wherein, reflux condensing tube is located at the top of hydrolytic reaction pot and its air outlet is connected with the import of condenser, the air outlet of condenser is connected with Vacuuming structure, Vacuuming structure is connected with exhaust treatment system with the venting port of water wash column, the exhaust gas inlet of water wash column is connected with the air outlet of alkali neutralization reaction still, the diluted acid outlet of water wash column, the condensation-water drain (containing a small amount of dilute hydrochloric acid in water of condensation) of the first thickener are all connected with the import of diluted acid storage tank with the liquid outlet of condenser, and the outlet of diluted acid storage tank is connected with the opening for feed of dissolving vessel.Wherein, reflux condensing tube is used for cooling steam, by hydrochloric acid reflux in hydrolytic reaction pot, is specifically as follows spherical, snakelike or straight shape structure, is preferably dimroth's condensing tube.Wherein, condenser is the common condenser for reclaiming.Wherein, Vacuuming structure is vacuum pump, and wherein, water wash column is circulating water wash structure, and its inside is provided with spray header and densitometer, when its concentration reaches certain value, will wash acid and send into diluted acid storage tank.Further, alkali cleaning structure is provided with between condenser and Vacuuming structure.
Wherein, in said structure, a plate-and-frame filter press can be shared in each step or share a reactor, 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 still and the second decoloring reaction still can be realized by same reactor, the i.e. main functionally restriction of above-mentioned annexation, not as restriction of the present utility model.But in actual production process, in order to produce smooth carrying out, aforementioned each structure is all realized by independent structure.
Wherein, " first " in foregoing description, " second " ... Deng description only for distinguishing, to facilitate description, and not there are other Special Significance.
The beneficial effect of the technical scheme that the utility model embodiment provides is: the utility model embodiment provides the device that a kind of feather produces multiple amino acids, this device is on the basis of existing production technique, carry out many places adjustment, to reduce the yield of cost and raising product, simultaneously, the technique that the utility model provides is more smooth, is applicable to suitability for industrialized production.
Accompanying drawing explanation
In order to be illustrated more clearly in the technical scheme in the utility model embodiment, below the accompanying drawing used required in describing embodiment is briefly described, apparently, accompanying drawing in the following describes is only embodiments more of the present utility model, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the structured flowchart that feather that the utility model embodiment provides produces the device of multiple amino acids;
Fig. 2 is the structured flowchart of the HCl recovery structure that the utility model embodiment provides;
Fig. 3 is the process flow sheet of the Gelucystine workshop section that the utility model embodiment provides;
Fig. 4 is the process flow sheet of the leucine workshop section that the utility model embodiment provides;
Fig. 5 is the process flow sheet of the tyrosine workshop section that the utility model embodiment provides.
Embodiment
For making the purpose of this utility model, technical scheme and advantage clearly, below in conjunction with accompanying drawing, the utility model embodiment is described in further detail.
See Fig. 1, the utility model embodiment provides the device that a kind of feather produces multiple amino acids, and this device comprises Gelucystine workshop section, leucine workshop section and tyrosine workshop section etc.
Wherein, see Fig. 1, hydrolytic reaction pot 2, first thickener 3, alkali neutralization reaction still 4, settling tank 5, first plate-and-frame filter press 6, dissolving vessel 7, sour neutralization reaction still 8, second plate-and-frame filter press 9, first decoloring reaction still 10, the 3rd plate-and-frame filter press 11, second decoloring reaction still 12, the 4th plate-and-frame filter press 13, ammonia neutralization reaction still 14 and the first whizzer 15 etc. that Gelucystine workshop section comprises HCl recovery structure 1 and sets gradually.Wherein, HCl recovery structure 1 is connected with hydrolytic reaction pot 2, first thickener 3, alkali neutralization reaction still 4 and dissolving vessel 7, and the sludge outlet of the 4th plate-and-frame filter press 13 is connected by the opening for feed of structure for conveying with the first decoloring reaction still 10.
Wherein, see Fig. 1, two female thickeners 16, condensation reaction still 17, cooling reactor 18, the female ammonolysis reaction still 20 of the 5th plate-and-frame filter press 19, two, the female decoloring reaction still 22 of the 6th plate-and-frame filter press 21, two, the 7th female ammonia neutralization reaction still 24 of plate-and-frame filter press 23, two and two female whizzers 25 etc. that leucine workshop section comprises material-compound tank 37 and sets gradually.Wherein, material-compound tank 37 is connected with the opening for feed of condensation reaction still 17, and the liquid feeding end of two female thickeners 16 is connected with the filtrate outlet of the second plate-and-frame filter press 9.
Preferably, the filtrate outlet of the 5th plate-and-frame filter press 19 is connected for improving leucic productive rate with the opening for feed of condensation reaction still 17.
Wherein, see Fig. 1, tyrosine workshop section comprises the molten reactor 26 of the first alkali set gradually, three female alkali neutralization reaction stills 27, 8th plate-and-frame filter press 28, the molten reactor 29 of second alkali, 9th plate-and-frame filter press 30, three female sour neutralization reaction stills 31, tenth plate-and-frame filter press 32, three female decoloring reaction stills 33, 11 plate-and-frame filter press 34, three female ammonolysis reaction stills 35 and three female whizzers 36 etc., the opening for feed of the molten reactor 26 of the first alkali exports with the centrifugate of the first whizzer 15 and is connected, the sludge outlet of the 11 plate-and-frame filter press 34 is connected by the opening for feed of structure for conveying with the molten reactor 29 of the second alkali.
Preferably, the sludge outlet of the 9th plate-and-frame filter press 30 is connected for recycling waste active carbon (certainly, also can directly manually be transported by go-cart) here with the opening for feed of two female decoloring reaction stills 22 by structure for conveying.The filtrate outlet of the 8th plate-and-frame filter press 28 is connected for improving leucic productive rate with the opening for feed of two female ammonolysis reaction stills 20.
Aforementioned structure connects in turn essentially by pipeline, and pipeline arranges power-driven pump, valve and flow valve as required.Meanwhile, aforementioned each structure is all acidproof or caustic corrosion structure, and reactor is enamel reaction still or glass reaction still.Further, two-layer setting is divided in each workshop, and one deck is located at by reactor, and plate-and-frame filter press is located at two layers.Wherein, the receiving tank that detachable swash plate and its side be arranged in parallel is set below the slag-drip opening comprising plate-and-frame filter press for carrying the structure for conveying of filter residue, filter residue is sent in receiving tank by swash plate, and filter residue is sent in reactor by conveying belt or conveyer trough by receiving tank.
Further, this device also comprises arginine workshop section or aminoacids complex workshop section, and the filtrate outlet of the first plate-and-frame filter press 6 is connected for the production of arginine or aminoacids complex with arginine workshop section or aminoacids complex workshop section.
Wherein, see Fig. 2, HCl recovery structure 1 comprises reflux condensing tube 38, Vacuuming structure 39, condenser 40, diluted acid storage tank 41 and water wash column 42 etc.Wherein, reflux condensing tube 38 is located at the top of hydrolytic reaction pot 2 and its air outlet is connected with the import of condenser 40, the air outlet of condenser 40 is connected with Vacuuming structure 39, the venting port of Vacuuming structure 39 is all connected with exhaust treatment system with the venting port of water wash column 42, the exhaust gas inlet of water wash column 42 is connected with the air outlet of alkali neutralization reaction still 4, the diluted acid outlet of water wash column 42, the condensation-water drain of the first thickener 3 are all connected with the import of diluted acid storage tank 41 with the liquid outlet of condenser 40, and the outlet of diluted acid storage tank 41 is connected with dissolving vessel 7.
See Fig. 3-5, below the technical process of said apparatus is described, comprises the following steps:
Wherein, see Fig. 3, Gelucystine workshop section comprises the following steps:
101 hydrolysis: be hydrolyzed through selecting hair machine to select after hair 4 tons of drake feathers to send in the hydrolytic reaction pot 2 of 15 cubes with the hydrochloric acid of 30wt%, hydrolysis temperature is 115 DEG C, hydrolysis time 5h, the mass ratio of drake feather (dry weight) and hydrochloric acid is 1:1.8, and to reclaim hydrochloric acid for subsequent use for HCl recovery structure 1 simultaneously.
102 concentrate: hydrolyzed solution step 101 obtained the first thickener 3 is concentrated into 1/3 of original weight amount, and thickening temperature is 90 DEG C, while HCl recovery structure 1 to reclaim hydrochloric acid for subsequent use, obtain about 3 tons of concentrated solutions.
103 alkali neutralizations: the concentrated solution 10 tons of steps 102 obtained is sent in alkali neutralization reaction still 4, and adds 500KgNa
2cO
3the NaOH solution of solid and 3 tons of 30wt% is reacted, temperature of reaction 70 DEG C, reaction times 8h, and simultaneously to reclaim hydrochloric acid for subsequent use for HCl recovery structure 1.
104 1 mother stocks to send in settling tank 5 natural subsidence 30 hours from: the neutralizer that step 103 obtained, send into again in the first plate-and-frame filter press 6 and carry out press filtration, obtaining a mother liquor send arginine workshop section or aminoacids complex workshop section for the production of arginine or composite fertilizer, and filter residue send dissolving vessel 7 by structure for conveying.
105 acid neutralizations, filter residue step 104 obtained sends into dissolving vessel 7, adopt the step 101 that HCl recovery structure 1 reclaims, 102 and the 103 whole hydrochloric acid reclaimed carry out dissolving (it is about 1:2.5 that ratio is about filter residue with the mass ratio of recovery hydrochloric acid), adjustment pH is 0.85, after dissolving completely, send in sour neutralization reaction still 8, the hydrochloric acid adding 30wt% hydrochloric acid or HCl recovery structure 1 recovery carries out acid neutralization, adjustment pH is 0.55, 25 minutes room temperature reaction time, react rear feeding second plate-and-frame filter press 9 and carry out press filtration, obtain secondary mother liquid and send into two female thickeners 16 for the production of leucine, filter residue send the first decoloring reaction still 10 by structure for conveying.
106 once decolour: filter residue step 105 obtained is sent in the first decoloring reaction still 10, add appropriate pure water, gac and 30wt% hydrochloric acid to decolour, decolorization condition is: temperature 65 DEG C, pH is 0.5, gac is whole waste active carbons that step 107 produces, and in 30 minutes reaction times, rear feeding of having decoloured the 3rd plate-and-frame filter press 11 carries out press filtration, filtrate send the second decoloring reaction still 12, and filter residue send solid waste disposal.
107 secondary decolourizations: filtrate step 106 obtained is sent in the second decoloring reaction still 12, add appropriate pure water, gac and 30wt% hydrochloric acid to decolour, decolorization condition is: temperature 65 DEG C, pH is 0.5, the usage quantity of gac is fresh activity charcoal 20Kg/ ton hair, 30 minutes reaction times, rear feeding of having decoloured the 4th plate-and-frame filter press 13 carries out press filtration, filter residue carries out reclaiming gac send step 106(first decoloring reaction still 10 by structure for conveying) use, filtrate send ammonia neutralization reaction still 14.
108 ammonia neutralizations: filtrate step 107 obtained is sent in ammonia neutralization reaction still 14, the ammoniacal liquor adding 20wt% neutralizes, neutrality condition is: temperature 75 DEG C, the usage quantity of ammoniacal liquor is 200Kg/ ton hair, react the centrifugation of rear feeding first whizzer 15 and obtain Gelucystine crude product and three mother liquors, three times mother liquor sends into the molten reactor 26 of the first alkali for the production of tyrosine, and Gelucystine crude product send step 109.
109 Gelucystines are refined: the Gelucystine crude product that step 108 obtains is through washing, drying and obtain Gelucystine fine work after pulverizing, and the chromatography through national regulations detects, and the purity of Gelucystine fine work is 95.4%, and output is 47.1Kg hair per ton.
Wherein, see Fig. 4, leucine workshop section comprises the following steps:
201 2 is female concentrated: secondary mother liquid step 105 obtained sends into two female thickener 16(triple effects) in, under 100 DEG C of conditions, be concentrated into 17 degree Beaume, the concentrated solution after concentrated send condensation reaction still 17.
202 contractings and: in material-compound tank 37, the 1:1 by volume of the vitriol oil and o-Xylol carries out allotment to be obtained by reacting mixed solution for subsequent use, mixed solution after the 18 cubes of concentrated solutions (while hot) step 201 obtained, 500L allotment and 200KgNaCl send in condensation reaction still 17, react rear feeding cooling reactor 18 and be cooled to room temperature, send into the 5th plate-and-frame filter press 19 again and carry out press filtration, filter residue send two female ammonolysis reaction stills 20 by structure for conveying, and filtrate returns in the opening for feed of condensation reaction still 17 carries out condensation.
203 2 female ammonia solutions: filter residue step 202 obtained is sent in two female ammonolysis reaction stills 20, add liquefied ammonia after dissolving (filtrate that appropriate pure water and step 302 obtain) and carry out ammonia solution, aminolysis conditions is: temperature 95 DEG C, terminal pH is 8.0, time is as the criterion to have reacted, send the 6th plate-and-frame filter press 21 to carry out press filtration after having reacted, filter residue send two female decoloring reaction stills 22 by structure for conveying.
204 2 female decolourings: filter residue step 203 obtained is sent in two female decoloring reaction stills 22, add appropriate pure water, gac and 30wt% hydrochloric acid to decolour, decolorization condition is: temperature 80 DEG C, gac is whole waste active carbons that step 305 reclaims, and pH is 1,2 hours reaction times, the 7th plate-and-frame filter press 23 is sent to carry out press filtration after having decoloured, filtrate send two female ammonia neutralization reaction stills 24, and certainly, this step also can adopt fresh activity charcoal 15Kg/8 ton hair.
205 2 female ammonia neutralizations: filtrate step 204 obtained is sent in two female ammonia neutralization reaction stills 24, add 30wt% ammoniacal liquor and carry out ammonia solution, aminolysis conditions is: temperature 70 C, terminal pH is 4.6,20 minutes reaction times, send after having reacted that two female whizzers 25 are centrifugal obtains leucine crude product, leucine crude product send step 206.
206 leucines are refined: the leucine crude product that step 205 obtains is through washing, drying and obtain leucine fine work after pulverizing, and the chromatography through national regulations detects, and the purity of leucine fine work is 95.5%, and output is 34.7Kg hair per ton.
Wherein, the filtrate obtained in above process and centrifugate can return applies mechanically.
Wherein, see Fig. 5, tyrosine workshop section comprises the following steps:
301 1 times alkali is molten: three mother liquors obtained in step 108 send in the molten reactor 26 of the first alkali, and adding 30wt%NaOH solution, to carry out alkali molten, and condition is: temperature 70 C, and in 5 hours reaction times, terminal pH is 12, send three female alkali neutralization reaction stills 27 after having reacted.
302 3 female alkali neutralizations: reaction solution step 301 obtained send in three female alkali neutralization reaction stills 27, and adds (NH
4)
2cO
3carry out neutralization reaction, reaction conditions is: to room temperature after reacting while hot, terminal pH is 4.7,1 hour reaction times, the 8th plate-and-frame filter press 28 press filtration is sent after having reacted, filter residue send the second alkali molten reactor 29 by structure for conveying, and filtrate send step 203(bis-female ammonolysis reaction still 20) in the filter residue that obtains for dissolving step 202.
303 2 times alkali is molten: filter residue step 302 obtained is sent in the molten reactor 29 of the second alkali, the whole waste active carbons adding the generation of appropriate pure water, 30wt%NaOH solution and step 305 react, reaction conditions is: temperature 70 C, pH is 12, in 5 hours reaction times, send the 9th plate-and-frame filter press 30 press filtration after having reacted, filter residue recovered carbon, filtrate send three female neutralization reaction stills 31, and the gac of recovery send step 204(bis-female decoloring reaction still 22) in carry out decoloring reaction.
304 3 female acid neutralizations: filtrate step 303 obtained send three female neutralization reaction stills 31, add 30wt% hydrochloric acid again and carry out neutralization reaction, reaction conditions is: terminal is pH8.5, room temperature reaction time 2 h, send the tenth plate-and-frame filter press 32 press filtration after having reacted, filter residue send three female decoloring reaction stills 33 by structure for conveying.
305 3 female decolourings: filter residue step 304 obtained send three female decoloring reaction stills 33, add the pure water of 12 times of weight, 30wt% hydrochloric acid and fresh activity charcoal, decolorization condition is: temperature 60 C, fresh activity charcoal 20Kg/ ton hair, pH is 0.5, the reaction times hour, send the 11 plate-and-frame filter press 34 press filtration after having decoloured, filter residue recovered carbon send the second alkali molten reactor 29 by structure for conveying, and filtrate send three female ammonolysis reaction stills 35.
306 3 female ammonia solutions: filtrate step 305 obtained is sent in three female ammonolysis reaction stills 35, and add liquefied ammonia and react, reaction conditions is: temperature 70 C, terminal is pH2.4, in 2 hours reaction times, reacted rear filter-cloth filtering, filter residue send three female whizzers 36 to dry and centrifugally obtains tyrosine crude product.
307 tyrosine are refined: the tyrosine crude product that step 306 obtains is through washing, drying and obtain tyrosine fine work after pulverizing, and the chromatography through national regulations detects, and the purity of tyrosine fine work is 93.9%, and output is 25.2Kg hair per ton.
Wherein, the filtrate obtained in above process and centrifugate can return applies mechanically.
Wherein, dilute hydrochloric acid, ammoniacal liquor and liquefied ammonia are unified to be provided, and NaOH solution is allotment during use, then in said structure, the female sour neutralization reaction still 31 of first decoloring reaction still 10, second decoloring reaction still 13, two female decoloring reaction still 22, three is all connected with dilute hydrochloric acid generator with three female decoloring reaction stills 33 etc. and is used for providing dilute hydrochloric acid, ammonia neutralization reaction still 14 is all connected with ammoniacal liquor generator with two female neutralization reaction still 24 grades and is used for providing ammoniacal liquor, and two female ammonolysis reaction stills 20 are all connected with liquefied ammonia generator with three female ammonolysis reaction stills 35 and are used for providing liquefied ammonia.
The utility model embodiment provides the device that a kind of feather produces multiple amino acids, and this device comprises HCl recovery structure, hydrolytic reaction pot, first thickener, alkali neutralization reaction still, settling tank, first plate-and-frame filter press, dissolving vessel, acid neutralization reaction still, second plate-and-frame filter press, first decoloring reaction still, 3rd plate-and-frame filter press, second decoloring reaction still, 4th plate-and-frame filter press, ammonia neutralization reaction still, first whizzer, two female thickeners, condensation reaction still, cooling reactor, 5th plate-and-frame filter press, two female ammonolysis reaction stills, 6th plate-and-frame filter press, two female decoloring reaction stills, 7th plate-and-frame filter press, two female ammonia neutralization reaction stills, two female whizzers, the molten reactor of first alkali, three female alkali neutralization reaction stills, 8th plate-and-frame filter press, the molten reactor of second alkali, 9th plate-and-frame filter press, three female sour neutralization reaction stills, tenth plate-and-frame filter press, three female decoloring reaction stills, 11 plate-and-frame filter press, three female ammonolysis reaction stills and three female whizzers, this device is on the basis of existing production equipment, carry out many places adjustment, to reduce the yield of cost and raising product, meanwhile, in the device that the utility model provides, each structure is common structure and annexation is simple, is convenient to recovered carbon, compact construction, is applicable to suitability for industrialized production.
The above embodiment of the present utility model, does not form the restriction to the utility model protection domain.Any various other made according to technical conceive of the present utility model change and distortion accordingly, all should be included in the protection domain of the utility model claim.
Claims (7)
1. feather produces a device for multiple amino acids, comprises Gelucystine workshop section, leucine workshop section and tyrosine workshop section, it is characterized in that,
The hydrolytic reaction pot that described Gelucystine workshop section comprises HCl recovery structure and sets gradually, first thickener, alkali neutralization reaction still, settling tank, first plate-and-frame filter press, dissolving vessel, acid neutralization reaction still, second plate-and-frame filter press, first decoloring reaction still, 3rd plate-and-frame filter press, second decoloring reaction still, 4th plate-and-frame filter press, ammonia neutralization reaction still and the first whizzer, described HCl recovery structure and hydrolytic reaction pot, first thickener, alkali neutralization reaction still is connected with dissolving vessel, the sludge outlet of described 4th plate-and-frame filter press is connected by the opening for feed of structure for conveying with the first decoloring reaction still,
Two female thickeners, condensation reaction still, cooling reactor, the 5th plate-and-frame filter press, two female ammonolysis reaction stills, the 6th plate-and-frame filter press, two female decoloring reaction stills, the 7th plate-and-frame filter press, two female ammonia neutralization reaction stills and two female whizzers that described leucine workshop section comprises material-compound tank and sets gradually, described material-compound tank is connected with the opening for feed of condensation reaction still, and the liquid feeding end of described two female thickeners is connected with the filtrate outlet of the second plate-and-frame filter press;
Described tyrosine workshop section comprises the molten reactor of the first alkali, three female alkali neutralization reaction stills, the 8th plate-and-frame filter press, the molten reactor of the second alkali, the 9th plate-and-frame filter press, three female sour neutralization reaction stills, the tenth plate-and-frame filter press, three female decoloring reaction stills, the 11 plate-and-frame filter press, three female ammonolysis reaction stills and the three female whizzers that set gradually, the opening for feed of the molten reactor of described first alkali exports with the centrifugate of the first whizzer and is connected, and the sludge outlet of described 11 plate-and-frame filter press is connected by the opening for feed of structure for conveying with the molten reactor of the second alkali.
2. feather according to claim 1 produces the device of multiple amino acids, it is characterized in that, described device also comprises arginine workshop section or aminoacids complex workshop section, and the filtrate outlet of described first plate-and-frame filter press is connected with arginine workshop section or aminoacids complex workshop section.
3. feather according to claim 1 produces the device of multiple amino acids, it is characterized in that, the sludge outlet of described 9th plate-and-frame filter press is connected by the opening for feed of structure for conveying with two female decoloring reaction stills.
4. feather according to claim 1 produces the device of multiple amino acids, it is characterized in that, the filtrate outlet of described 5th plate-and-frame filter press is connected with the opening for feed of condensation reaction still.
5. feather according to claim 1 produces the device of multiple amino acids, it is characterized in that, the filtrate outlet of described 8th plate-and-frame filter press is connected with the opening for feed of two female ammonolysis reaction stills.
6. feather according to claim 1 produces the device of multiple amino acids, it is characterized in that, described first thickener is an effect thickener, and described two female thickeners are Three-effect concentration device.
7. the feather according to any one of claim 1-6 produces the device of multiple amino acids, it is characterized in that, described HCl recovery structure comprises reflux condensing tube, Vacuuming structure, condenser, diluted acid storage tank and water wash column, described reflux condensing tube is located at the top of hydrolytic reaction pot and its air outlet is connected with the import of condenser, the air outlet of described condenser is connected with Vacuuming structure, the exhaust gas inlet of described water wash column is connected with the air outlet of alkali neutralization reaction still, the diluted acid outlet of described water wash column, the condensation-water drain of the first thickener is all connected with the import of diluted acid storage tank with the liquid outlet of condenser, the described outlet of diluted acid storage tank is connected with the opening for feed of dissolving vessel.
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| CN201520409492.XU CN204848706U (en) | 2015-06-15 | 2015-06-15 | Device of multiple amino acid is prepared to feather |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106496082A (en) * | 2016-10-31 | 2017-03-15 | 荆门市欣胱生物工程股份有限公司 | A kind of aminoacids complex powder spraying system and the production method of aminoacid powder |
| CN106496054A (en) * | 2016-10-31 | 2017-03-15 | 荆门市欣胱生物工程股份有限公司 | A kind of feather produces the production method of aminoacids complex |
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2015
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106496082A (en) * | 2016-10-31 | 2017-03-15 | 荆门市欣胱生物工程股份有限公司 | A kind of aminoacids complex powder spraying system and the production method of aminoacid powder |
| CN106496054A (en) * | 2016-10-31 | 2017-03-15 | 荆门市欣胱生物工程股份有限公司 | A kind of feather produces the production method of aminoacids complex |
| CN106496082B (en) * | 2016-10-31 | 2018-03-06 | 荆门市欣胱生物工程股份有限公司 | A kind of production method of compound amino acid powder spraying system and amino acid powder |
| CN106496054B (en) * | 2016-10-31 | 2018-06-12 | 荆门市欣胱生物工程股份有限公司 | A kind of production method of feather production compound amino acid |
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