CN102617720B - Steam type protein separation and recycling system - Google Patents
Steam type protein separation and recycling system Download PDFInfo
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- CN102617720B CN102617720B CN201210094239.0A CN201210094239A CN102617720B CN 102617720 B CN102617720 B CN 102617720B CN 201210094239 A CN201210094239 A CN 201210094239A CN 102617720 B CN102617720 B CN 102617720B
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Abstract
The invention relates to a steam type protein separation and recycling system. The system comprises a heat exchanger, a buffer tank, a steam micro-vortex flocculation reaction kettle, and a floc reverse separation device; the steam micro-vortex flocculation reaction kettle is adopted, so the separation juice such as atomized starch and the like and steam are flocculated through three-dimensional contact, and are fully reacted, so that flocculation reaction efficiency is greatly improved, the recovery rate of protein is high, and a good effect of purifying the juice is achieved; the settled floc stays transiently at the bottom of the reaction kettle to form micro vortex flow, so that the recovery rate of protein is increased, and the effect of purifying the separation juice is improved further; according to the system, equipment is few, the floor space is small, investment is low, and running cost is low; and the system has a closed structure, and is pollution-free, low in energy consumption, large in treatment amount, high in efficiency, and suitable for starch processing separation juice of potatoes, corns and the like, and high-efficiency protein recovery of various protein-enriched separation juice, and high-efficiency separation and purification of relevant separation juice.
Description
Technical field
The invention belongs to technical field of chemical, relate to a kind of separation and recovery system of protein, relate in particular to a kind of steam-type protein separation recovery system, be mainly used in Separation and Recovery and the wastewater treatment of protein in the processing of farm products separation juice such as potato, cassava, W-Gum.
Background technology
The processing of farm products such as potato, cassava, W-Gum separates any discharge that the nutritive substances such as juice and numerous kinds rich in proteins separate juice environment and agricultural production security to processing enterprise region and has formed significant damage.If adopt the processing of routine biochemistry method, have that investment is large, running cost is high, envrionment temperature is too low, treatment unit is difficult for starting and the difficult problem such as cannot throughout the year turn round.And adopt embrane method processing, there is again the problems such as cost is high, film easily pollutes, and life cycle is short.Though flocculence separate in this class have application aspect the processing of juice produce the too low flocculation agent weak effect causing of season envrionment temperature, flocculation agent consumption is excessive, reclaims the problem such as of poor quality that obtains protein.
Chinese patent 200810006643.1 is disclosed separates method for extracting proteins juice from yam starch processing, it is only a kind of intermittent process introduction, and there is following problem and have a strong impact on efficiency and the practical effect of whole technique: 1. the constitutional features of the hot flocculation reaction equipment of protein is very large to efficiency and the influential effect of heat flocculation, be the key part that determines energy consumption height, but this invention does not relate to; 2. the pedesis under high-temperature condition of protein flco is very serious, high temperature and do not use completely flocculation agent will cause settling of floccus slowly, flco solution solid content is too low, makes horizontal spiral separator high loaded process, inefficiency; Do not have heat-exchange equipment to cause the heat of flocculation solution to be wasted simultaneously, further increased the energy consumption of whole technique; 3. preheating and adjustment pH value there is no need, such separates juice and is easy to cause the technological problemses such as pipeline obstruction through the tiny protein flco of preheating and the generation of adjustment pH value, and hot flocculation reaction step is subsequently enough to ensure the abundant flocculation of protein, simultaneously, detect through long-term, the intrinsic pH value that this type of processing separates juice is between 4.6-5.1, conventionally do not need to regulate pH value can reach processing requirement, and too much can cause serious corrosion and shorten work-ing life of complete assembly pipeline only adding of strong acid; 4. too much facility investment causes the whole cost of technology higher, starch processing industry is small profit trade, the key problem that starch processing separation juice recycling treatment will solve is processing cost problem, and the centrifugal screen using in this patent and horizontal spiral separator need purchasing and recondition expense of writing, greatly increase the economical load of enterprise, affected the practicality of whole technique.
Summary of the invention
The object of the invention is for problems of the prior art, a kind of steam-type protein separation recovery system is provided.
Steam-type protein separation recovery system of the present invention, comprises interchanger, surge tank, steam micro swirl flocculation reaction still, flco reverse-separating device; In described interchanger, be provided with juice layer and flocbed, and be respectively arranged with juice import at the two ends of juice layer and flocbed, juice outlet and flocculation import, flocculation outlet; The juice import of interchanger is connected to juice pond by in-line pump, and the juice outlet of interchanger is communicated with the bottom of surge tank; In described steam micro swirl flocculation reaction still, middle part is provided with ring-type steam-pipe, and on ring-type steam-pipe, is provided with steam atomizing shower nozzle; Steam micro swirl flocculation reaction still is provided with the vapour pipe being communicated with ring-type steam-pipe outward; The top of steam micro swirl flocculation reaction still is provided with juice atomizer, and this juice atomizer is communicated with the top of surge tank by pipeline; The bottom of steam micro swirl flocculation reaction still is flco settling banker, and the bottom of this flco settling banker is communicated with the flocculation entrance of interchanger by pipeline; The flocculation outlet of interchanger is communicated with the water-in of flco reverse-separating device, and goes out to be connected with flocculation agent medicine-chest at the water-in of flco reverse-separating device.
The processings of farm products such as potato, cassava, W-Gum separate juice and pump into interchanger by in-line pump, after heat exchange, enter surge tank, the juice atomizer that enters steam micro swirl flocculation reaction still top by pipeline after the stable pressure that separates juice of surge tank sprays in micro swirl flocculation reaction still, forms juice atomizing droplet.Simultaneously, in ring-type steam-pipe, be filled with steam by the vapour pipe outside steam micro swirl flocculation reaction still, and sprayed in micro swirl flocculation reaction still by the steam atomizing shower nozzle on ring-type steam-pipe, separate juice atomizing droplet and under the effect of atomizing steam, in reactor, form micro swirl, and fully act on atomizing steam, in micro swirl reaction chamber, make to separate in the protein in juice abundant sex change of moment in warm environment and separate out, form flco flocculation sediment; The flco aqueous solution after flocculation flows into the flco settling banker of below, by the pipeline inflow heat exchanger of bottom, the separation juice that not yet enters reactor is carried out to preheating again afterwards, and cooling flocculation to be to reduce pedesis, thereby accelerates flco precipitate and separate; Then enter reverse flco tripping device by interchanger flocculation outlet by pipeline, after further flocculation separation, protein flco is wadded a quilt with cotton to manage by the row of reverse flco separation unit bottoms and is reclaimed, by press dewatering or the dry laggard step deep processing and utilization of spraying; Water quality substantially transparent after separation, free from extraneous odour, reaches agricultural irrigation water quality standard, also can reuse as potato starch factory material potato wash-down water.
The entrance of described surge tank is provided with flow and takes into account relief valve, and the flow of the juice that enters surge tank is regulated to control; The outlet of surge tank is provided with tensimeter, and the pressure at surge tank top is detected online.
Described ring-type steam-pipe divides the upper and lower two-layer middle part that is arranged on micro swirl flocculation reaction still, and the direction that is arranged on the steam atomizing shower nozzle on upper and lower two-layer ring-type steam-pipe is relative, thereby ensure to separate the abundant effect of juice atomizing droplet and atomizing steam.Steam atomizing shower nozzle is movably arranged on ring-type steam-pipe, makes the horizontal sextant angle of itself and ring-type steam-pipe 0～90
ointerior adjustable.
Described juice atomizer is movably arranged on the top of micro swirl flocculation reaction still, to realize the adjusting of steam atomizing sprinkler height and angle.
The outer wall of described micro swirl flocculation reaction still is provided with thermal insulation layer, makes the temperature of reactor keep constant, to ensure carrying out smoothly of flocculation reaction.
On described micro swirl flocculation reaction still, be provided with viewing window, so that the response situation in reactor is observed.
The top of described micro swirl flocculation reaction still is provided with exhaust-valve and tensimeter, tensimeter detects online to the pressure in reactor, exhaust-valve regulates the pressure in reactor by regulated valve manually or automatically, thereby ensures that the vapor pressure of reactor is stable.
In the described micro swirl flocculation reaction still of described micro swirl flocculation reaction still bottom, be provided with thermometer, the temperature in reactor detected online, to ensure the effect of flocculation reaction.
For the ease of controlling, on the pipeline of above-mentioned each road, be provided with control valve.
The structure of described flco reverse-separating device and principle of work are shown in Chinese patent 200910022772.4: water-distribution anti-disturbance floc precipitation reverse separation device or patent 2009100 22771.X: anti-destabilization flocculent precipitate reversed separating jar.
The present invention is relative, and prior art has the following advantages:
1, the present invention adopts steam micro swirl flocculation reaction still, makes the starch etc. of atomization separate juice and steam by three-dimensional contact flocculation, and fully reaction, has increased substantially flocculation reaction efficiency, and protein recovery is high, juice good purification; The flco of sedimentation, in the small vortex flow of reactor bottom short stay formation, has further improved the rate of recovery and the decontamination effect improving that separates juice of albumen.
2, the equipment of system of the present invention is few, and floor space is little, less investment, and running cost is low.
3, system of the present invention adopts enclosed construction, pollution-free, energy consumption is low.
4, system of the present invention is can treatment capacity large, and efficiency is high, is suitable for potato, corn and other starches processing separates juice and all kinds of rich in proteins separates juice high efficiente callback protein and the relevant high efficiency separation that separates juice purifies.
brief description of the drawings
The structural representation of Fig. 1 embodiment of the present invention 1 system;
Fig. 2 is the structural representation of the embodiment of the present invention 2 systems;
Fig. 3 is the structural representation of steam micro swirl flocculation reaction still annular steam pipeline and steam atomizing shower nozzle;
Fig. 4 is the cut-away view of interchanger.
embodiment
By tool embodiment, the structure to system of the present invention and treatment process are elaborated line face.
Embodiment 1
(1) system architecture
With reference to Fig. 1, a kind of steaming process protein separation retrieving arrangement, comprises interchanger 5, surge tank 8, steam micro swirl flocculation reaction still 11 and 22 4 parts of flco reverse-separating device.
In interchanger 5, be provided with juice layer and flocbed, and be respectively arranged with juice import 4 at the two ends of juice layer and flocbed, juice outlet 6 and flocculation import 18, flocculation outlet 19; The juice import 4 of interchanger 5 is connected to juice pond 1 by in-line pump 3, and the juice outlet 6 of interchanger 5 is communicated with the bottom of surge tank 8.The operating pressure of interchanger 5 is 0.0～1.0MPa, and heat interchanging area is 60～120M
2, heat-exchange temperature interval is 0～150
oc.
Steam micro swirl flocculation reaction still 11 is upright cylindrical shell shells, and bottom is inverted triangle taper, and shell is enclosed with thermal insulation layer (for the urethane material of thickness 40～120 mm).In reactor, middle part is provided with the ring-type steam-pipe 15 that upper and lower two-layer caliber is 33～50mm, and on ring-type steam-pipe 15, is evenly movably installed with steam atomizing shower nozzle 12, and the direction of upper and lower two-layer steam atomizing shower nozzle 12 (referring to Fig. 3) relatively.Vapo(u)r blasting shower nozzle 12 operating pressure are at 0.1～1.2 MPa, and the atomizing steam of its injection forms and is 0～120
othe solid conical shape of drift angle.The number of vapo(u)r blasting shower nozzle and making the appropriate adjustments with the requirement of the visual hot flocculation reaction temperature of horizontal sextant angle of ring-type steam-pipe.The outer logical steam-pipe being communicated with ring-type steam-pipe 15 that is provided with of reactor 11.On logical steam-pipe, steam valve, tensimeter are installed, by steam regulation valve manually or automatically, the vapor pressure that ensures to enter reactor is stable.The top of reactor 11 is provided with juice atomizer 10, and this juice atomizer is communicated with the top of surge tank 8 by pipeline.Juice atomizer 10 is arranged on the top of steam micro swirl flocculation reaction still 11 by screw socket, highly adjustable (its distance that stretches into reactor 11 tops is adjustable in 0～200 mm).Separate the operating pressure of juice atomizer under 0.1～1.2 MPa, eject drift angle and be 0～120
othe atomizing steam of solid conical shape has ensured to separate the abundant effect of juice atomizing droplet and atomizing steam.The inverted triangle taper bottom of steam micro swirl flocculation reaction still 11 is flco settling banker 17, and the bottom of this flco settling banker is communicated with the flocculation entrance 18 of interchanger 5 by pipeline.On steam micro swirl flocculation reaction still 11, be provided with viewing window 16, the response situation in reactor can be observed by viewing window 16.The top of steam micro swirl flocculation reaction still 11 is provided with exhaust-valve 20 and tensimeter 9, the safe operation of assurance device.In steam micro swirl flocculation reaction still 11, be provided with thermometer 13.
The structure of flco reverse-separating device and principle of work are shown in Chinese patent 200910022772.4: water-distribution anti-disturbance floc precipitation reverse separation device, it comprises water-in, water storage, cloth pool, flco flow deflector, flco storage warehouse and reverse filtration storehouse, and described water storage is by device case, first vertical baffle of cloth pool and be positioned at that their middle and lower parts are staggered is the warehouse that oblique funnelform flco flow deflector forms; Described cloth pool is provided with multiple vertical baffles that leave up and down passage that shorten gradually, and at the each flco flow deflector of installing in the middle and lower part of each baffle plate both sides, the flco flow deflector on every adjacent vertical baffle interlocks and is oblique funnel-form; Described flco storage warehouse is located at the below in cloth pool, and its bottom is connected with row's wadding pipeline; Described reverse filtration storehouse is located at the end in cloth pool, and its top sets out the mouth of a river, and water outlet is communicated with outlet pipeline by a filtering net.
The flocculation outlet of interchanger 5 is communicated with the water-in of flco reverse-separating device 22, and be connected with flocculation agent medicine-chest 21 at the water-in of flco reverse-separating device, the water-in of flco reverse-separating device 22 is also provided with thermometer 13, temperature to the flocculation water that enters flco reverse-separating device is monitored in real time, to ensure the effect of flocculation reaction.
(2) Separation and Recovery of protein
In system operational process, regulate the pressure of back with water inlet line by detecting the temperature of interchanger juice outlet, ensure heat transfer effect simultaneously.Control back with water inlet line pressure at 0.20～0.62 MPa.Enter the temperature of surge tank juice 0 ~ 25
oc, the pressure in surge tank is-0.2 ~ 1.0MPa; The temperature of steam micro swirl flocculation reaction still is 80 ~ 120
oc, the pressure in reactor is 0.2 ~ 0.6MPa; The operating pressure of vapo(u)r blasting shower nozzle 16 is at 0.1～1.2 MPa, and the operating pressure that separates juice atomizer 12 is 0.1～1.2 MPa, and the leaving water temperature(LWT) that interchanger flows to flco reverse-separating device is controlled at 20～40
oc, flocculation reaction temperature is 80～120
oc, operating pressure is 0.2 ~ 0.62 MPa.
Water inlet: it is 11.81 tons/hour that yam starch processing separates juice flow, turbidity 1007-1165 NTU, COD is 39043-57326 mg/L, total nitrogen is 2.90-3.74 mg/mL.Operation 10h continuously; Add flocculation agent Poly Dimethyl Diallyl Ammonium Chloride 100mg/L, 2 hours residence time.
Water outlet: delivery turbidity clearance reaches 85.63%-89.21%, device water outlet is as clear as crystal; COD clearance reaches 53.88%-58.44%, and nutrition major part is recovered utilization; Nitrogen removal rate reaches 43.88%-58.12%, and protein recovery reaches more than 90%.Extract altogether albumen 1.42 t, water outlet naked eyes range estimations water quality substantially transparent, free from extraneous odour, reaches agricultural irrigation water quality standard, also can reuse as potato starch factory material potato wash-down water.
Embodiment 2
(1) system architecture: with reference to Fig. 2, a kind of steaming process protein separation retrieving arrangement, comprises interchanger 5, surge tank 8, steam micro swirl flocculation reaction still 11 and 22 4 parts of flco reverse-separating device.Wherein the structure of interchanger 5, surge tank 8, steam micro swirl flocculation reaction still 11 is identical with embodiment 1, the structure of flco reverse-separating device 22 is shown in Chinese patent 2009100 22771.X: anti-destabilization flocculent precipitate reversed separating jar, it comprises water-in, water storage, cloth pool, flco flow deflector, flco storage warehouse and reverse filtration storehouse, and described water storage is by device case, first vertical baffle of cloth pool and be positioned at that their middle and lower parts are staggered is the warehouse that oblique funnelform flco flow deflector forms; Described cloth pool is provided with multiple vertical baffles that leave up and down passage that shorten gradually, and at the each flco flow deflector of installing in the middle and lower part of each baffle plate both sides, the flco flow deflector on every adjacent vertical baffle interlocks and is oblique funnel-form; Described flco storage warehouse is located at the below in cloth pool, and its bottom is connected with row's wadding pipeline; Described reverse filtration storehouse is located at the end in cloth pool, and its top sets out the mouth of a river, and water outlet is communicated with outlet pipeline by a filtering net.
(2) Separation and Recovery of protein
The working temperature of each equipment and operating pressure are with embodiment 1.
Water inlet: it is 12 tons/hour that yam starch processing separates juice flow, moves continuously 10h, and influent turbidity is 1301-1456 NTU, and COD is 38004-53917 mg/L, and total nitrogen is 2.77-3.51 mg/L.Adding flocculation agent is bodied ferric sulfate 150mg/L, 2 hours residence time.
Water outlet: delivery turbidity clearance reaches 90.81%-93.52%, device water outlet is as clear as crystal; COD clearance reaches 51.22%-53.07%, and nutrition major part is recovered utilization; Nitrogen removal rate reaches 49.83%-54.60%, and protein recovery reaches more than 90%.Extract altogether albumen 1.56t, water outlet naked eyes range estimations water quality substantially transparent, free from extraneous odour, reaches agricultural irrigation water quality standard, also can reuse as potato starch factory material potato wash-down water.
Claims (8)
1. a steaming process protein separation retrieving arrangement, is characterized in that: comprise interchanger (5), surge tank (8), steam micro swirl flocculation reaction still (11) and flco reverse-separating device (22); Described interchanger is provided with juice layer and flocbed in (5), and be respectively arranged with juice import (4) at the two ends of juice layer and flocbed, juice outlet (6) and flocculation import (18), flocculation export (19); The juice import (4) of interchanger (5) is connected to juice pond (1) by in-line pump (3), and the juice outlet (6) of interchanger (5) is communicated with the bottom of surge tank (8); In described steam micro swirl flocculation reaction still (11), middle part is provided with ring-type steam-pipe (15), and on ring-type steam-pipe (15), is provided with steam atomizing shower nozzle (12); The outer steam-pipe being communicated with ring-type steam-pipe (15) that is provided with of steam micro swirl flocculation reaction still (11); The top of steam micro swirl flocculation reaction still (11) is provided with juice atomizer (10), and this juice atomizer (10) is communicated with the top of surge tank (8) by pipeline; The bottom of steam micro swirl flocculation reaction still (11) is flco settling banker (17), and the bottom of this flco settling banker is communicated with the flocculation entrance (18) of interchanger (5) by pipeline; The flocculation outlet (19) of interchanger (5) is communicated with the water-in of flco reverse-separating device (22), and is connected with flocculation agent medicine-chest (21) at the water-in of flco reverse-separating device (22) by in-line pump (3); Described ring-type steam-pipe (15) point upper and lower two-layer middle part that is arranged on steam micro swirl flocculation reaction still (11), and it is relative to be arranged on the direction of the steam atomizing shower nozzle (12) on upper and lower two-layer ring-type steam-pipe (15); Described steam atomizing shower nozzle (12) is movably arranged on ring-type steam-pipe (15).
2. steaming process protein separation retrieving arrangement as described in claim 1, is characterized in that: the entrance of described surge tank (8) is provided with under meter (7) and relief valve (2); Surge tank (8) outlet is provided with tensimeter (9).
3. steaming process protein separation retrieving arrangement as described in claim 1, is characterized in that: described juice atomizer (12) is movably arranged on the top of micro swirl flocculation reaction still.
4. steaming process protein separation retrieving arrangement as described in claim 1, is characterized in that: the skin of described steam micro swirl flocculation reaction still (11) is thermal insulation layer (14).
5. steaming process protein separation retrieving arrangement as described in claim 1, is characterized in that: on described steam micro swirl flocculation reaction still (11), be provided with viewing window (16).
6. steaming process protein separation retrieving arrangement as described in claim 1, is characterized in that: the top of described steam micro swirl flocculation reaction still (11) is provided with exhaust-valve (20) and tensimeter (9).
7. steaming process protein separation retrieving arrangement as described in claim 1, is characterized in that: in described steam micro swirl flocculation reaction still (11), be provided with thermometer (13).
8. steaming process protein separation retrieving arrangement as described in claim 1, is characterized in that: the entrance of described flco reverse-separating device (22) is provided with thermometer (13).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210094239.0A CN102617720B (en) | 2012-04-01 | 2012-04-01 | Steam type protein separation and recycling system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210094239.0A CN102617720B (en) | 2012-04-01 | 2012-04-01 | Steam type protein separation and recycling system |
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| CN102617720A CN102617720A (en) | 2012-08-01 |
| CN102617720B true CN102617720B (en) | 2014-06-04 |
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| CN105230964A (en) * | 2015-11-18 | 2016-01-13 | 中国科学院兰州化学物理研究所 | Technology for extracting potato protein through hot flocculence method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1048020A (en) * | 1990-06-20 | 1990-12-26 | 北京市环境保护科学研究所 | Be used to reclaim proteinic novel flocculant |
| CN101560000A (en) * | 2009-06-03 | 2009-10-21 | 中国科学院兰州化学物理研究所 | Anti-destabilization flocculent precipitate reversed separating jar |
| CN101580292A (en) * | 2009-06-03 | 2009-11-18 | 中国科学院兰州化学物理研究所 | Water-distribution anti-disturbance floc precipitation reverse separation device |
-
2012
- 2012-04-01 CN CN201210094239.0A patent/CN102617720B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1048020A (en) * | 1990-06-20 | 1990-12-26 | 北京市环境保护科学研究所 | Be used to reclaim proteinic novel flocculant |
| CN101560000A (en) * | 2009-06-03 | 2009-10-21 | 中国科学院兰州化学物理研究所 | Anti-destabilization flocculent precipitate reversed separating jar |
| CN101580292A (en) * | 2009-06-03 | 2009-11-18 | 中国科学院兰州化学物理研究所 | Water-distribution anti-disturbance floc precipitation reverse separation device |
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