CN110003307A - A kind of method of Protein Recovery in proteinic wastewater - Google Patents
A kind of method of Protein Recovery in proteinic wastewater Download PDFInfo
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- CN110003307A CN110003307A CN201910357152.XA CN201910357152A CN110003307A CN 110003307 A CN110003307 A CN 110003307A CN 201910357152 A CN201910357152 A CN 201910357152A CN 110003307 A CN110003307 A CN 110003307A
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Abstract
The present invention provides a kind of methods of the Protein Recovery in proteinic wastewater, which comprises is passed through in proteinic wastewater using air carrying volatile acid and adjusts pH value to isoelectric points of proteins, precipitating recycling is realized and recycles protein from proteinic wastewater；Method provided by the invention passes through using the volatile acid that air carries as acid regulating measure, the pH value of waste water of high protein concentration is set to be adjustable to the isoelectric point of each protein at low pressures by the pressure of air, carrying temperature, carrying time etc., precipitating removes the protein of different isoelectric points in waste water respectively, improve the removal rate of protein, it is even higher that the overall recovery of albumen can reach 95% or so, be conducive to industrialized production, when practical application value with higher.
Description
Technical field
The invention belongs to bio-chemistry separation field, it is related to a kind of method of the Protein Recovery in proteinic wastewater.
Background technique
High concentration proteinic wastewater mostly uses greatly traditional bioremediation, but either at Aerobic Process for Treatment or anaerobism
Reason, all there is the generation of sludge pollution object and stench, long processing period, it is complicated for operation the problems such as.Especially biological method is not
The protein in high protein waste water only cannot be effectively recycled, but also secondary pollution can be generated, is resulted in waste of resources.Cause
This, in processing high protein waste water, many researchers attempt various methods to recycle protein, such as membrane separation process, flocculation sedimentation
Method and ohm heat treating process etc..But there are fouling membrane, the processing time is long and at high cost the problems such as be difficult to industrial applications.Industrially
Most widely used method is isoelectric precipitation, because it is easy to operate, saves the time, at low cost, Protein Recovery is relatively pure
Only.During traditional isoelectric precipitation, there is pH to adjust inaccuracy, local overacidification, introduces salt secondary pollution and albumen
The problems such as matter rate of recovery is low.
CN102659233A discloses a kind of minimizing technology of protein in rich proteinic wastewater, by the following steps: (1) will
Protein component contained by rich proteinic wastewater to be processed carries out isoelectric point analysis, and presses isoelectric points of proteins certainly according to analysis result
Big extremely small determining packet classification processing scheme；(2) reaction will be transferred to after rich proteinic wastewater pretreatment to be processed in step (1)
Kettle；(3) volatility weak acid gas is filled in the reaction kettle for being transferred to rich proteinic wastewater to step (2) as acid regulator, anti-
It answers the volatility weak acid gas pressure and pH value of waste water in kettle to constitute corresponding relationship, adjusts rich proteinic wastewater pH value and reach grouping point
Relatively large isoelectric points of proteins in grade, and precipitate the protein at the isoelectric point sufficiently, it is opposite to obtain isoelectric points of proteins
Biggish protein precipitation and supernatant；(4) the relatively large protein of isoelectric points of proteins obtained in step (3) is heavy
It forms sediment and supernatant is separated by solid-liquid separation, remove the relatively large protein precipitation of isoelectric points of proteins, it then will be separating obtained
Supernatant is transferred to reaction kettle again；(5) above-mentioned steps (3), (4) are repeated in, continue to be filled with volatility weak acid into reaction kettle
Gas reduces solution ph step by step, successively obtains the supernatant of corresponding protein precipitations and final purification at different levels；(6) by gained
Final purification supernatant in volatility weak acid gas release, recycling.But the preferred CO of the method2But there is pH value tune
Save the poor defect of controllability, cannot achieve multistage isoelectric precipitation, more it is essential that, CO2It is weak for the volatility of representative
Acid gas pH value obtained must just be able to maintain stabilization in pressure maintaining, therefore precipitation and separation needs under high pressure could be real
It is existing, it does not meet and industrializes quick a large amount of waste water, simplicity, the demand of low-cost processes.
CN106007107A discloses a kind of recovery method of protein in high concentration proteinic wastewater, and the method is benefit
Entrained acetic acid, which is realized in high concentration proteinic wastewater, when with the nitrogen circulation of pressurization adjusts pH variation, so that the electricity such as classification is heavy
Form sediment the albumen recycled in waste water.But the method, during protein salvage, there are cost recovery height, processing unit are complicated and complete
Closing (system whole high pressure resistant reach at 10atm or more), compressed nitrogen are not easy to obtain, nitrogen needs to recycle always and causes energy consumption excessively high
Etc. problems, it is very difficult to realize large-scale industry amplification.
Therefore, a kind of high and conducive to industrialization promotion time of rate of recovery easy to operate, at low cost, protein how is developed
The method for receiving high concentration proteinic wastewater utilizes actual protein salvage and is of great significance and is worth.
Summary of the invention
In view of the deficiencies of the prior art, the purpose of the present invention is to provide a kind of sides of the Protein Recovery in proteinic wastewater
Method, to solve, the sour ability of tune existing in the prior art is limited, cost recovery is higher, complex process is unfavorable for industrialized ask
Topic.
In order to achieve that object of the invention, the invention adopts the following technical scheme:
The present invention provides a kind of methods of the Protein Recovery in proteinic wastewater, which comprises is taken using air
Band volatile acid, which is passed through in proteinic wastewater, adjusts pH value to isoelectric points of proteins, and precipitating recycling is realized and recycled from proteinic wastewater
Protein.
Recovery method provided by the invention passes through the pressure of air by carrying volatile acid as sour means are adjusted using air
Power, carrying temperature, carrying time etc. make the pH value of waste water of high protein concentration at low pressures (not higher than normal atmosphere (An)
It 2atm) is adjustable to the isoelectric point of each protein, precipitating removes the protein of different isoelectric points in waste water respectively, improves albumen
The removal rate of matter, it is even higher that the overall recovery of albumen can reach 95% or so.
Currently, the carrying of acetic acid is mainly realized in existing method by the circulation of pressurized nitrogen, the reason is that from molecule
Between interact and thermodynamic (al) angle on from the point of view of, pressurized nitrogen, which has acetic acid, specific high carries efficiency.But it uses
When pressurized nitrogen circulation carries out acetic acid carrying, need to be maintained at carry kettle and adjust sour kettle keep carrying out under higher pressure etc. it is electric
The adjusting of point, it is more demanding to the resistance to pressure of complete equipment, and adjust sour ability limited, it is unable to reach lower pH value, technology
Higher cost.And exists since pressurized nitrogen recycles the technique imagination for carrying acetic acid, obtain protein precipitation from the sour kettle of tune every time
It is higher to be required to sequence of maneuvers, the complex operation degree such as release nitrogen decompression.
It is followed in addition, air of the present invention can be realized (not higher than normal atmosphere (An) 2atm) at low pressures than pressurization
The higher volatile acid of ring nitrogen carries efficiency, this is because in composition of air other than the nitrogen gas component containing 78%, also
Containing the ingredient that oxygen, carbon dioxide etc. promote a variety of acids to volatilize at low pressures, packet can be realized under normal pressure
Include the carrying of a variety of escaping gas including volatile acid.From actual effect, air can be obtained directly from atmosphere, be made
Cost is extremely low；It uses instead and takes sour kettle operating pressure after air and occur that (the pressure higher than atmospheric pressure kept is greatly reduced
Value main purpose is that the hydraulic pressure of sour kettle is adjusted in confrontation, guarantees that gas smoothly overflows)；Sour kettle is adjusted to directly adopt normal pressure after using air instead
Operation, equipment and operating cost decline to a great extent；Entire reaction process is accurately easy to control, strong operability, without any nocuousness
Residual, production security are high.
It preferably, further include isoelectric point analysis and removal solid content before air carrying volatile acid is passed through protein waste water
The step of.
Preferably, the isoelectric point analysis is that protein component contained in proteinic wastewater is carried out isoelectric point analysis,
Then the gradient pH value to be adjusted is determined by the size of isoelectric points of proteins according to analysis result.
Preferably, the removal solid content is to be transferred to after the solid content removal in proteinic wastewater in the sour kettle of tune.
Preferably, the protein content in the proteinic wastewater is no less than 7mg/mL.
Preferably, the air is deposited in steel cylinder, and the volatile acid, which is placed in, to be taken in sour kettle, the steel cylinder successively with take
Sour kettle adjusts sour kettle connection.
Preferably, the volatile acid taken in sour kettle is the volatile acid aqueous solution of pure volatile acid or any concentration.
Volatile acid of the present invention can be acetic acid, propionic acid, butyric acid etc., it is generally preferable to be acetic acid；It is also possible to second
The aqueous solution of acid, propionic acid aqueous solution of any concentration etc..
Volatile acid in the present invention is not limited to acetic acid, but in view of acetic acid is in various safety issues such as food,
Still it is preferable to use acetic acid, this can make the pH degree of regulation of whole system higher, and the pace of change of pH value in sour kettle is adjusted in control.Example
Such as, in the high ph-values acidification stage of 5.5-7, when adjusting that pH value decrease speed is too fast in sour kettle, can in taking sour kettle a certain concentration
Acetic acid aqueous solution, by pH value decline speed reduce, be more advantageous to promoted precipitating efficiency.
Preferably, the absolute pressure for taking sour kettle be 1-3atm, such as can be 1atm, 1.01atm, 1.05atm,
1.1atm, 1.5atm, 1.8atm, 2atm, 2.2atm, 2.5atm or 3atm etc., preferably 1~2atm.
Preferably, the temperature for taking sour kettle be 10~70 DEG C, such as can be 10 DEG C, 15 DEG C, 20 DEG C, 25 DEG C, 30 DEG C,
35 DEG C, 40 DEG C, 45 DEG C, 50 DEG C, 55 DEG C, 60 DEG C, 65 DEG C or 70 DEG C etc., preferably 20~30 DEG C.
Preferably, the pressure for adjusting sour kettle is normal pressure.
Preferably, the sour kettle of the tune is communicated with atmosphere.
In the present invention, adjusting sour kettle is non-pressure vessel, can reduce the requirement of equipment pressure resistance, and expands the model for adjusting acid
Enclose, compared to use nitrogen circulation recycling albumen method, it is minimum for the adjusting lower limit of the proteinic wastewater pH value of same concentration can
Be reduced to it is 3.0 even lower, can preferably suitable for different isoelectric point waste water albumen adjusting, and the air flowed out can be straight
Run in and be put in atmosphere, pollution-free, the device for avoiding pressurized circulation circulation uses, and is more advantageous to industrialized production and application.
Preferably, the temperature for adjusting sour kettle is 10~60 DEG C；Such as can be 10 DEG C, 15 DEG C, 20 DEG C, 25 DEG C, 30 DEG C,
35 DEG C, 40 DEG C, 45 DEG C, 50 DEG C, 55 DEG C or 60 DEG C etc., preferably 20~30 DEG C.
In the present invention, it adjusts sour kettle under normal temperature and pressure conditions, such as 1atm, albumen etc. can be transferred under the conditions of 25 DEG C
Electric point, it is possible to reduce system heat demand further saves equipment and operating cost.
Preferably, after adjusting pH value to isoelectric points of proteins, stop being passed through the air for carrying volatile acid, so that protein
Sufficiently after precipitating, emptying adjusts sour kettle pressure to be separated by solid-liquid separation, and precipitating recycling obtains protein, again by isolated supernatant
It is secondary to be transferred to the sour kettle of tune.Wherein stop being passed through air by way of closing the valve taken between sour kettle and the sour kettle of tune.
It is precipitated obtained in it, is directly separated recycling；Obtained from supernatant then can further progress precipitating.
Preferably, repeat precipitating recycling albumen and separation supernatant be transferred to the step of adjusting sour kettle, reduce pH value step by step,
Until obtaining the supernatant of protein precipitations and purification at different levels.
In the present invention, precipitating recycling albumen and the separation supernatant of repeating is transferred to the step of adjusting sour kettle, essence
On be exactly to carry out multi-level hierarchical precipitating, according to isoelectric point analysis as a result, gradient adjusts pH value, gradient precipitating, precise precipitation mentioned
Rise deposition efficiency.
Steel cylinder of the present invention is generally voltage stabilizing steel cylinder.
Preferably, described method includes following steps:
(1) protein component contained in proteinic wastewater is subjected to isoelectric point analysis, then presses egg according to analysis result
The size of white matter isoelectric point determines the gradient pH value to be adjusted, and will be transferred to the sour kettle of tune after the solid content removal in proteinic wastewater
In；
(2) volatile acid is added in taking sour kettle, opening takes sour kettle and adjusts sour kettle blow valve, simultaneously closes off and take sour kettle and tune
Valve between sour kettle, by air by after voltage stabilizing steel cylinder or voltage stabilizing air pump by taking sour kettle；
(3) the emptying valve taken sour kettle and adjust sour kettle is closed, steel cylinder is opened, the pressure for taking sour kettle is adjusted to 1~3atm, takes
The temperature of sour kettle is 10~70 DEG C, and sour kettle is adjusted to communicate with atmosphere, and adjusting the temperature of sour kettle is 10~60 DEG C；
Wherein, the emptying valve of sour kettle is preferably taken in step (3) by gradually closing, while gradually opening and taking sour kettle and tune
Valve method between sour kettle, pressure to the sour kettle gas of tune that sour kettle is taken in adjusting within the scope of absolute pressure 1-3atm can be stablized excessive
Out, the temperature for taking sour kettle is 10~70 DEG C, and sour kettle is adjusted to communicate with atmosphere, and adjusting the temperature of sour kettle is 10~60 DEG C；
(4) wait take the pressure of sour kettle it is constant after, sour kettle blow valve is taken in closing, and air carrying volatile acid is passed through albumen and is given up
In water, when adjusting pH value to isoelectric points of proteins, opening takes sour kettle blow valve, simultaneously closes off and takes valve between sour kettle and the sour kettle of tune,
Stopping is passed through air, so that protein sufficiently precipitates, precipitating and supernatant are separated by solid-liquid separation, recycling precipitating, by supernatant
It is transferred in the sour kettle of tune again；
(5) step (4) are repeated, reduces pH value step by step, until obtaining the supernatant of protein precipitations and purification at different levels.
Wherein reclaimer includes sequentially connected voltage stabilizing steel cylinder (or voltage stabilizing air pump), takes sour kettle and adjust sour kettle.Steel cylinder with
It takes and is provided with valve on the pipeline of sour kettle connection, take and be provided with valve and gas flow on the pipeline between sour kettle and the sour kettle of tune
Meter, and take and may be provided with blow valve, safety valve and pressure gauge on sour kettle, it adjusts and is provided with emptying valve on sour kettle.
Compared with the existing technology, the invention has the following advantages:
(1) present invention by the pressure of air, carries temperature using the volatile acid that air carries as acid regulating measure
Degree, carrying time etc. make the pH value of waste water of high protein concentration (not higher than normal atmosphere (An) 2atm, guarantee to adjust acid at low pressures
Kettle gas normally overflows) it is adjustable to the isoelectric point of each protein, precipitating removes the egg of different isoelectric points in waste water respectively
White matter improves the removal rate of protein, and it is even higher that the rate of recovery of albumen can reach 95% or so.
(2) adjusting sour kettle is non-pressure vessel, reduces requirement of the equipment to pressure resistance, and expand the range for adjusting acid, compared to making
With the method for nitrogen circulation recycling albumen, for the proteinic wastewater of same concentration, pH adjusts that lower limit is minimum drops to 3.0 even more
It is low；The accurate tune for using the raw materials such as volatile acid aqueous solution that system is made also to be able to achieve pH value within the scope of the high pH of 5.5-7 simultaneously
Section.It the multistage isoelectric precipitation of albumen can be adjusted more preferably suitable for different isoelectric point waste water, it is easier to realization of industrialization and popularization.
(3) air is directly obtained from atmosphere, and use cost is extremely low.Entire reaction process is accurately easily-controllable, strong operability,
Without any hazard residue, production security is high.
(4) volatile acid that the present invention uses allows the raw material added as a kind of feed, field of food, makes to recycle albumen
It is used directly for above-mentioned field.The Selective Separation of protein ingredient is imitated simultaneously because classification isoelectric precipitation also has simultaneously
Fruit, this will make separated albumen have higher added value of product.
Detailed description of the invention
Fig. 1 is the schematic device that the present invention recycles protein from proteinic wastewater.
Specific embodiment
The technical scheme of the invention is further explained by means of specific implementation.Those skilled in the art should be bright
, the described embodiments are merely helpful in understanding the present invention, should not be regarded as a specific limitation of the invention.
Provided by the present invention is only a kind of schematic device for recycling protein, and wherein volatile acid is with acetic acid
Example, it is not limited to using this acid；Furthermore when actually being recycled, device can be modified according to the actual situation or connect
It connects, is not limited only to the structure type.
Embodiment 1
The present embodiment recycles protein from proteinic wastewater by the following method:
The waste water generated after a kind of processing of wall pollack minced fillet is chosen, which is about 7.0 or so, through albumen
Matter constituent analysis discovery, waste water protein concentration after centrifugation pretreatment is 7.6mg/mL, and isoelectric point is more densely concentrated
In near 6.40,5.10 and 4.30, it is divided into three-level by arrogant to the small determination of isoelectric points of proteins according to the analysis result.Wherein
Reclaimer is as shown in Figure 1.
Acetic acid is added in taking sour kettle in level-one isoelectric precipitation, by air by pressure buffer steel cylinder, is passed through to taking in sour kettle
Air takes sour kettle safety valve and remains absolute pressure 1.5atm, and taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, adjust
Sour kettle pH value reaches 6.40 ± 0.05.Close communicating valve between two kettles, staticly settle 20min, then by high concentration proteinic wastewater from
The heart obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 5.1mg/mL.
Then secondary tune acid is carried out to above-mentioned supernatant, realizes second level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.5atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, adjust acid kettle pH to reach 5.10 ± 0.02 attached
Closely.After adjusting sour kettle gas emptying, 20min is staticly settled, the proteinic wastewater after second level isoelectric precipitation is centrifuged again then, is obtained
Protein precipitation and supernatant are obtained, measuring protein content in supernatant at this time is 3.4mg/mL.
Then above-mentioned supernatant is carried out adjusting acid three times, realizes three-level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.5atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle normal temperature and pressure, and sour kettle pH value is adjusted to reach 4.30 ± 0.02.Adjust acid
After the emptying of kettle gas, 20min is staticly settled, the proteinic wastewater after second level isoelectric precipitation is centrifuged again then, is precipitated
Albumen and supernatant, measuring protein content in supernatant at this time is 0.5mg/mL.By three-level isoelectric precipitation, the total protein rate of recovery reaches
To 93.4%.
Embodiment 2
The present embodiment recycles protein from proteinic wastewater by the following method:
The waste water generated after a kind of processing of blue whiting minced fillet is chosen, which is about 7.2 or so, through albumen
Matter constituent analysis discovery, waste water protein concentration after centrifugation pretreatment is 7.1mg/mL, and isoelectric point is more densely concentrated
In near 6.45,5.20 and 3.25, it is divided into three-level by arrogant to the small determination of isoelectric points of proteins according to the analysis result.
Acetic acid is added in taking sour kettle in level-one isoelectric precipitation, by air by pressure buffer steel cylinder, is passed through to taking in sour kettle
Air takes sour kettle safety valve and remains absolute pressure 1.2atm, and taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, adjust
Sour kettle pH value reaches 6.45 ± 0.05.After adjusting sour kettle gas emptying, communicating valve between two kettles is closed, 30min is staticly settled, then will
The centrifugation of high concentration proteinic wastewater, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 5.5mg/mL.
Then secondary tune acid is carried out to above-mentioned supernatant, realizes second level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.2atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, when duration of ventilation 1.8min, adjusts sour kettle pH
Reach 5.20 ± 0.02.After adjusting sour kettle gas emptying, 20min is staticly settled, then the albumen after second level isoelectric precipitation gives up
Water is centrifuged again, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 3.52mg/mL.
Then above-mentioned supernatant is carried out adjusting acid three times, realizes three-level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.2atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle normal temperature and pressure, when duration of ventilation reaches 7.5min, adjusts sour kettle pH
Value reaches 3.25 ± 0.02.After adjusting sour kettle gas emptying, 20min is staticly settled, then by the albumen after second level isoelectric precipitation
Waste water is centrifuged again, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 0.4mg/mL.By three-level etc.
Electroprecipitation, the total protein rate of recovery reach 94.4%.
Embodiment 3
The present embodiment recycles protein from proteinic wastewater by the following method:
A kind of waste water for mixing and generating after minced fillet processing is chosen, which is about 7.2 or so, through albumen
Matter constituent analysis discovery, waste water protein concentration after centrifugation pretreatment is 8.9mg/mL, and isoelectric point is more densely concentrated
In near 6.40,5.15,4.30 and 3.25, it is divided into three by arrogant to the small determination of isoelectric points of proteins according to the analysis result
Grade.
Acetic acid is added in taking sour kettle in level-one isoelectric precipitation, by air by pressure buffer steel cylinder, is passed through to taking in sour kettle
Air takes sour kettle safety valve and remains absolute pressure 1.3atm, and taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, adjust
Sour kettle pH value reaches 6.40 ± 0.05.After adjusting sour kettle gas emptying, communicating valve between two kettles is closed, 30min is staticly settled, then will
The centrifugation of high concentration proteinic wastewater, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 5.8mg/mL.
Then secondary tune acid is carried out to above-mentioned supernatant, realizes second level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.3atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, when duration of ventilation 1.8min, adjusts sour kettle pH
Reach 5.15 ± 0.02.After adjusting sour kettle gas emptying, 20min is staticly settled, then the albumen after second level isoelectric precipitation gives up
Water is centrifuged again, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 3.8mg/mL.
Then above-mentioned supernatant is carried out adjusting acid three times, realizes three-level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.3atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle normal temperature and pressure, when duration of ventilation reaches 7.5min, adjusts sour kettle pH
Value reaches 4.20 ± 0.02.After adjusting sour kettle gas emptying, 20min is staticly settled, then by the albumen after second level isoelectric precipitation
Waste water is centrifuged again, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 1.7mg/mL.
Then four tune acid are carried out to above-mentioned supernatant, realizes level Four isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.3atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle normal temperature and pressure, when duration of ventilation reaches 7.5min, adjusts sour kettle pH
Value reaches 3.25 ± 0.02.After adjusting sour kettle gas emptying, 20min is staticly settled, then by the albumen after second level isoelectric precipitation
Waste water is centrifuged again, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 0.3mg/mL.By three-level etc.
Electroprecipitation, the total protein rate of recovery reach 96.6%.
Embodiment 4
The present embodiment recycles protein from proteinic wastewater by the following method:
The waste water generated after a kind of processing of minced fish is chosen, which is about 7.5 or so, through albumen
Matter constituent analysis discovery, waste water protein concentration after centrifugation pretreatment is 9.1mg/mL, and isoelectric point is more densely concentrated
In near 6.25,5.00 and 3.85, it is divided into three-level by arrogant to the small determination of isoelectric points of proteins according to the analysis result.
Acetic acid is added in taking sour kettle in level-one isoelectric precipitation, by air by pressure buffer steel cylinder, is passed through to taking in sour kettle
Air takes sour kettle safety valve and remains absolute pressure 1.2atm, and taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, lead to
When the gas time is 1.2min, sour kettle pH value is adjusted to reach 6.25 ± 0.05.After adjusting sour kettle gas emptying, 30min is staticly settled, then
High concentration proteinic wastewater is centrifuged, protein precipitation and supernatant are obtained, measuring protein content in supernatant at this time is 5.0mg/mL.
Then secondary tune acid is carried out to above-mentioned supernatant, realizes second level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.2atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle the temperature remains within the normal range normal pressure, when duration of ventilation 1.5min, adjusts sour kettle pH
Reach 5.00 ± 0.02.After adjusting sour kettle gas emptying, 20min is staticly settled, then the albumen after second level isoelectric precipitation gives up
Water is centrifuged again, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 2.88mg/mL.
Then above-mentioned supernatant is carried out adjusting acid three times, realizes three-level isoelectric precipitation.Sour kettle safety valve is taken at this time to remain
Absolute pressure 1.2atm, taking sour kettle temperature degree is 25 DEG C, adjusts sour kettle normal temperature and pressure, when duration of ventilation reaches 7.1min, adjusts sour kettle pH
Value reaches 3.85 ± 0.02.After adjusting sour kettle gas emptying, 20min is staticly settled, then by the albumen after second level isoelectric precipitation
Waste water is centrifuged again, obtains protein precipitation and supernatant, and measuring protein content in supernatant at this time is 0.5.It is heavy by the electricity such as three-level
It forms sediment, the total protein rate of recovery reaches 94.5%.
Comparative example 1
This comparative example the difference from embodiment 1 is that: this comparative example is passed through using compressed nitrogen takes sour kettle.
Known to the result of comparison:
1, in terms of device structure, equipment used by embodiment 1 is more succinct, and no nitrogen moves in circles structure, adjusts acid
Process is easy to operate, while there is no the decompression demands of release nitrogen for precipitation and separation process.
2, it to be open equipment that sour kettle is adjusted from the point of view of equipment pressure resistance performance, in embodiment 1, take sour kettle also only need to have 3atm with
Interior voltage endurance capability, and comparative example needs to take sour kettle and the sour kettle of tune all has the voltage endurance capability of 30atm.
3, in terms of operating flexibility and cost, comparative example is only limitted to using acetic acid, and the present embodiment then uses and arbitrarily meets
The volatile acid of production requirement.Pressurized circulation nitrogen employed in comparative example has part release loss in precipitating, follows
The pressurized nitrogen that loopback is gone be also required to task equipment it is carried out it is recycled after corresponding purified treatment.In 1 air of embodiment
Then directly from Free Acquisition around.Therefore, comparative example integrated operation cost is obviously higher than embodiment 1.
4, from the point of view of adjusting sour accuracy, no matter embodiment 1 circulates smoothness or in terms of taking sour accuracy in gas,
There are more accurate control means.No matter in high ph-values (5.5-7.0) range or low ph value (3.0-5.5) range, can reach
Degree of regulation within ± 0.05, this has also ensured pH degree of regulation of the embodiment 1 during multistage isoelectric precipitation.And it compares
Do not embody the sour process possessed levels of precision on pH value degree of regulation of tune in example then, this and its higher operating pressure
There is certain relationship.
The Applicant declares that Protein Recovery in the present invention is explained by the above embodiments proteinic wastewater of the invention
Method, but the invention is not limited to above-mentioned processing steps, that is, do not mean that the present invention must rely on above-mentioned processing step ability
Implement.It should be clear to those skilled in the art, any improvement in the present invention, to raw material selected by the present invention etc.
Effect replacement and addition, the selection of concrete mode of auxiliary element etc., all of which fall within the scope of protection and disclosure of the present invention.
Claims (10)
1. a kind of method of the Protein Recovery in proteinic wastewater, which is characterized in that the described method includes: being waved using air carrying
Hair property acid, which is passed through in proteinic wastewater, adjusts pH value to isoelectric points of proteins, and precipitating recycling is realized and recycles albumen from proteinic wastewater
Matter.
2. the method according to claim 1, wherein being gone back before air carrying volatile acid is passed through protein waste water
Include the steps that isoelectric point analysis and removal solid content.
3. method according to claim 1 or 2, which is characterized in that the isoelectric point analysis is will be contained in proteinic wastewater
Some protein components carry out isoelectric point analysis, then to be adjusted according to analysis result by the size determination of isoelectric points of proteins
Gradient pH value.
4. method according to any one of claim 1-3, which is characterized in that the removal solid content is by proteinic wastewater
In solid content removal after, be transferred in the sour kettle of tune；
Preferably, the protein content in the proteinic wastewater is no less than 7mg/mL.
5. method according to any of claims 1-4, which is characterized in that the air is deposited in steel cylinder, described
Volatile acid, which is placed in, to be taken in sour kettle, the steel cylinder successively with take sour kettle, sour kettle adjusted to be connected to.
6. method according to any one of claims 1-5, which is characterized in that the volatile acid taken in sour kettle is pure
The volatile acid aqueous solution of volatile acid or any concentration.
7. method according to claim 1 to 6, which is characterized in that the absolute pressure for taking sour kettle be 1~
3atm, preferably 1~2atm；
Preferably, the temperature for taking sour kettle is 10~70 DEG C；Preferably 20~30 DEG C；
Preferably, the pressure for adjusting sour kettle is normal pressure；
Preferably, the sour kettle of the tune is communicated with atmosphere；
Preferably, the temperature for adjusting sour kettle is 10~60 DEG C；Preferably 20~30 DEG C.
8. method according to any one of claims 1-7, which is characterized in that after adjusting pH value to isoelectric points of proteins,
Stop being passed through the air for carrying volatile acid, so that protein precipitation, emptying adjusts sour kettle pressure to be separated by solid-liquid separation, and precipitating recycling obtains
Isolated supernatant is transferred to the sour kettle of tune by protein again.
9. method according to claim 1 to 8, which is characterized in that repeat precipitating recycling albumen and separation
Supernatant is transferred to the step of tune acid kettle, reduces pH value step by step, until obtaining the supernatant of protein precipitations and purification at different levels.
10. method according to claim 1 to 9, which is characterized in that described method includes following steps:
(1) protein component contained in proteinic wastewater is subjected to isoelectric point analysis, then presses protein according to analysis result
The size of isoelectric point determines the gradient pH value to be adjusted, and will be transferred in the sour kettle of tune after the solid content removal in proteinic wastewater；
(2) volatile acid is added in taking sour kettle, by air by pressure buffer steel cylinder or voltage stabilizing air pump adjustment after successively with take
Sour kettle adjusts sour kettle connection；
(3) the emptying valve taken sour kettle and adjust sour kettle is closed, steel cylinder is opened, the pressure for taking sour kettle is adjusted to 1~3atm, takes sour kettle
Temperature be 10~70 DEG C, adjust sour kettle to communicate with atmosphere, adjusting the temperature of sour kettle is 10~60 DEG C；
(4) wait take the pressure of sour kettle it is constant after, closing take sour kettle blow valve, by air carrying volatile acid be passed through proteinic wastewater
In, when adjusting pH value to isoelectric points of proteins, opening takes sour kettle blow valve, simultaneously closes off and takes sour kettle and adjust valve between sour kettle, stops
It is only passed through air, so that protein sufficiently precipitates, precipitating and supernatant are separated by solid-liquid separation, recycling precipitating, again by supernatant
It is secondary to be transferred in the sour kettle of tune；
(5) step (4) are repeated, reduces pH value step by step, until obtaining the supernatant of protein precipitations and purification at different levels.
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| CN113999278A (en) * | 2021-12-03 | 2022-02-01 | 西安全奥生物科技有限公司 | Method for extracting protein from potatoes |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1121926A (en) * | 1994-10-22 | 1996-05-08 | 王崴 | Extraction method and application of plant protein |
| CN101263859A (en) * | 2007-03-16 | 2008-09-17 | 浙江海洋学院 | Method for extracting fish protein from wastewater for processing aquatic product |
| CN102659233A (en) * | 2012-05-04 | 2012-09-12 | 泰祥集团技术开发有限公司 | Method for removing proteins in protein-enriched wastewater |
| CN106007107A (en) * | 2016-08-03 | 2016-10-12 | 中国海洋大学 | Recovery method of protein in high concentration protein wastewater |
-
2019
- 2019-04-29 CN CN201910357152.XA patent/CN110003307B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1121926A (en) * | 1994-10-22 | 1996-05-08 | 王崴 | Extraction method and application of plant protein |
| CN101263859A (en) * | 2007-03-16 | 2008-09-17 | 浙江海洋学院 | Method for extracting fish protein from wastewater for processing aquatic product |
| CN102659233A (en) * | 2012-05-04 | 2012-09-12 | 泰祥集团技术开发有限公司 | Method for removing proteins in protein-enriched wastewater |
| CN106007107A (en) * | 2016-08-03 | 2016-10-12 | 中国海洋大学 | Recovery method of protein in high concentration protein wastewater |
Non-Patent Citations (2)
| Title |
|---|
| TOBIAS GUCKEISEN，等: "Isoelectric Points of Proteins at the Air/Liquid Interface and in", 《LANGMUIR》 * |
| 齐祥明: "加压CO2-乙醇-水体系等电沉淀蛋白质过程的研究", 《中国博士论文全文数据库 工程科技I辑》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113999278A (en) * | 2021-12-03 | 2022-02-01 | 西安全奥生物科技有限公司 | Method for extracting protein from potatoes |
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