CN105111276A - Potato protein production process - Google Patents
Potato protein production process Download PDFInfo
- Publication number
- CN105111276A CN105111276A CN201510616389.7A CN201510616389A CN105111276A CN 105111276 A CN105111276 A CN 105111276A CN 201510616389 A CN201510616389 A CN 201510616389A CN 105111276 A CN105111276 A CN 105111276A
- Authority
- CN
- China
- Prior art keywords
- flocculator
- heating
- feed liquid
- flocculation
- protein production
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Peptides Or Proteins (AREA)
Abstract
The invention relates to a potato protein production process. The potato protein production process includes: removing fiber and starch in starch wastewater in a separation unit to obtain protein liquid; adjusting PH of the protein liquid to 5-5.2 in a PH adjusting unit; sectionally heating the protein liquid to 90-100 DEG C in a flocculation unit, adopting steam to heat the protein liquid to 120 DEG C for temperature-maintaining flocculation, and cooling after temperature-maintaining flocculation; delivering the protein liquid after flocculation to a dehydrating unit for dehydration, and delivering the protein liquid after being dehydrated to a drying unit for drying. By the above process, potato protein can be recovered quickly from the starch wastewater, recovery rate is high, energy consumption is low, and product purity is high.
Description
Technical field
The present invention relates to protein production field, be specifically related to a kind of Rhizoma Solani tuber osi protein production technique.
Background technology
Yam starch production line can discharge a large amount of waste water, due in waste water containing a large amount of albumen, therefore this effluent part is pumped to protein production systems and carries out extractions recovery albumen by general manufacturer.But protein production systems used at present all exists different defects in production efficiency, the rate of recovery and energy consumption etc., is therefore necessary to make improvements, to improve the economic benefit that Rhizoma Solani tuber osi protein is produced further.
Summary of the invention
Object of the present invention is just to provide a kind of Rhizoma Solani tuber osi protein production technique, and it can be used for extracting from starch production wastewater reclaiming albumen.
For achieving the above object, present invention employs following technical scheme:
A kind of Rhizoma Solani tuber osi protein production technique, comprises following operation:
S1: the fiber in starch waste liquor and starch removal are obtained albumen feed liquid at separating unit;
S2: the PH of albumen feed liquid is adjusted to 5 ~ 5.2 at PH regulon;
S3: first albumen feed liquid is heated to 90 ~ 100 DEG C piecemeal at flocculation unit, then adopts steam albumen feed liquid to be heated to 120 DEG C and carries out insulation flocculation, cool after insulation flocculation;
S4: the albumen feed liquid after flocculation is delivered to dewatering unit and dewaters, be delivered to drying unit after dehydration and carry out drying.
By above-mentioned technique, it can reclaim Rhizoma Solani tuber osi protein fast from starch wastewater, and the rate of recovery is high, and energy consumption is low, good product purity.
Accompanying drawing explanation
Fig. 1 is the structural representation of Rhizoma Solani tuber osi protein production technique;
Fig. 2 is the structural representation of separating unit;
Fig. 3 is the structural representation of foam tank of disappearing;
Fig. 4 is the structural representation of flocculation unit;
Fig. 5 is the structural representation of drying unit;
Fig. 6 is the structural representation of the first airheater;
Fig. 7 is the structural representation of sloped footing;
Fig. 8 is the structural representation of stirring mechanism.
Embodiment
In order to make objects and advantages of the present invention clearly understand, below in conjunction with embodiment, the present invention is specifically described.Should be appreciated that following word only in order to describe one or more concrete embodiments of the present invention, considered critical is not carried out to the protection domain that the present invention specifically asks.
A kind of Rhizoma Solani tuber osi protein production technique, comprise the latter linked separating unit F1 for being separated the starch in starch wastewater, albumen, fiber sequentially, for carrying out the PH regulon P1 of PH adjustment to the albumen feed liquid of separating unit F1 Separation and Recovery, for carrying out the flocculation unit X1 of flocculation treatment to the albumen feed liquid after adjustment PH, for carrying out the dewatering unit T1 of solid-liquid separation to the albumen after flocculation, and for carrying out dry drying unit G1 to the albumen after dehydration.
Its technological operation is:
A kind of Rhizoma Solani tuber osi protein production technique, comprises following operation:
S1: the fiber in starch waste liquor and starch removal are obtained albumen feed liquid at separating unit F1;
S2: the PH of albumen feed liquid is adjusted to 5 ~ 5.2 at PH regulon P1;
S3: first albumen feed liquid is heated to 90 ~ 100 DEG C piecemeal at flocculation unit X1, then adopts steam albumen feed liquid to be heated to 120 DEG C and carries out insulation flocculation, cool after insulation flocculation;
S4: the albumen feed liquid after flocculation is delivered to dewatering unit T1 and dewaters, be delivered to drying unit G1 after dehydration and carry out drying.
The starch waste liquor of overflow discharge is reclaimed, containing a small amount of nominal particle size starch and fiber fines in waste liquid from Starch Production line rotational flow station.The existence of these materials can be extracted albumen to hot flocculation process and be produced very large disadvantageous effect, needs to adopt an effective measure and removes remaining starch and fiber.
Concrete measure is, as Fig. 1, 2, shown in 3, separating unit F1 comprises the foam tank F20 that disappears, the foam tank F20 that disappears comprises the tank body that circular vertical shape is arranged, outer tank skin in the middle part of tank body is provided with the cloth mouth F23 tangentially sending into starch wastewater in tank body, be provided with in tank body, first of lower layout, two cone-shaped hoods, the cover mouth of the first cone-shaped hood F21 upwards, the cover mouth of the second cone-shaped hood F22 is downward, tank body is also respectively arranged with protein recycling pipe F26, fiber recovery pipe F27 and recovery of starch pipe F28, the inlet end of fiber recovery pipe F27 extends to the bottom in the first cone-shaped hood F21, top in the second cone-shaped hood F22 that the inlet end of protein recycling pipe F26 extends to, the inlet end of recovery of starch pipe F28 is positioned at the bottom of tank body.Cloth mouth F23 is that arc pipe fitting is formed, and arc pipe fitting increases gradually along the cross section of feed liquid throughput direction, and the liquid outlet of arc pipe fitting is arranged to the arc consistent with tank wall face, and in arc pipe fitting, interval arranges filter.The disappear top of foam tank F20 is provided with shower nozzle F25, the other end of fiber recovery pipe F27 is connected with the centrifugal screen F14 of Separation and Recovery fiber by the first pump housing F13, and the waste water discharge opening of centrifugal screen F14 is connected with shower nozzle F25, cloth mouth respectively by the second pump housing F15.By the foam tank F20 that disappears arranged, starch waste liquor tangentially enters the foam tank F20 that disappears in the middle part of tank body, and starch waste liquor forms eddy flow in tank, by first and second cone-shaped hood arranged in tank, heavy phase starch sinks down at the bottom of tank, and is discharged by the recovery of starch pipe F28 arranged at the bottom of tank.Light phase portion foam and fine-fibered float up to the foam tank F20 top that disappears, by discharging from fiber recovery pipe F27 after spray water froth breaking, liquid effluent enters a thin fine centrifugal screen F14, fine-fibered is separated and removes, and eliminate foam further, last blowback again, to the foam tank F20 that disappears, sprays and to disappear foam to the foam in tank body from shower nozzle.
The setting of the first cone-shaped hood F21 is mainly beneficial to the collection of fiber, the setting of the second cone-shaped hood F22 mainly anti-fluid backspin time the starch that tank base precipitates is stirred, affect the reliable separation of starch, albumen.Be pumped to flocculation unit X1 containing albumen feed liquid through waste water pump in the middle part of tank, before entering flocculation unit X1, waste water PH adjusted.
More specifically scheme is, disappear foam tank F20 top tank skin on be also provided with and connect mouth of pipe F24, connect the top that mouth of pipe F24 is positioned at the first cone-shaped hood F21, connect mouth of pipe F24 and connect the 3rd blower fan F11 and bubble collapse device F12 successively, bubble collapse device F12 comprises body, and in body, interval arranges and is used for the filter of broken foam or grid to remove a large amount of foams produced in the foam tank F20 that disappears further.
PH regulon P1 comprises acid solution storage tank and membrane pump, storing food level sulfuric acid in acid solution storage tank, by continuing the pH value adding food grade sulfuric acid Function protein feed liquid on albumen feed liquid transfer lime (the pump preceding pipeline of feed pump).The albumen feed liquid of discharging from the foam tank F20 that disappears squeezes into flocculation unit X1 by feed pump, and consider that the main feed pump that relies on of the feed liquid conveying of whole extraction system for protein completes, feed liquid flow process is longer, therefore adopts high-lift multi-stage centrifugal pump.Canned sulfuric acid is quantitatively delivered into albumen feed liquid transfer lime by membrane pump, due to the physical property of dilute sulphuric acid, can not produce feed liquid refluence phenomenon, otherwise can produce Serious Accident.
Flocculation unit X1 specifically adopts technical scheme as shown in Figure 4 to implement, flocculation unit X1 comprise sequentially connect arrange for albumen feed liquid is carried out heat flocculation each heating flocculator and for albumen feed liquid is carried out be incubated flocculation insulation flocculator X04, insulation flocculator X04 comprises the spiral conveying tube arranged in insulation shell and insulation shell, the heart yearn of spiral conveying tube is arranged in the horizontal direction, the caliber of spiral conveying tube is 1.5 ~ 2.5 times of albumen feed liquid transfer lime caliber, albumen feed liquid transfer lime is carry out for albumen feed liquid the pipeline carried between neighbouring device, the velocity of flow of such feed liquid in insulation flocculator X04 is slower, albumen can fully be flocculated condensation.Flocculation unit X1 comprises first, two, three heating flocculators and insulation flocculator X04, first, two heating flocculators are spiral-plate heat exchanger and form, 3rd heating flocculator X03 is that steam heater or spiral-plate heat exchanger are formed, the cold fluid inlet of the first heating flocculator X01 is connected with PH regulon P1, the cold fluid outlet of the first heating flocculator X01 is connected with the second cold fluid inlet heating flocculator X02, the cold fluid outlet of the second heating flocculator X02 is connected with the 3rd cold fluid inlet heating flocculator X03, the cold fluid outlet of the 3rd heating flocculator X03 is connected with the material inlet of insulation flocculator X04, the thermal fluid inlet of the 3rd heating flocculator X03 is connected with steam pipeline, the thermal fluid inlet of the second heating flocculator X02 is connected with the material outlet of insulation flocculator X04, the hot fluid outlet ports of the second heating flocculator X02 is connected with the first thermal fluid inlet heating flocculator X01.
Adopt above-mentioned flocculation unit X1 to flocculate, the albumen flocculation in feed liquid comprises following operation:
One-level preheating: feed liquid is delivered to the first heating flocculator X01 by High pressure feeding pump, feed liquid feeding temperature is 22 DEG C, after heat exchange, temperature of charge is increased to 60 ~ 70 DEG C, heating medium is the heating medium flowed out in the second heating flocculator X02, namely the temperature drop feed liquid of anterior backflow, is sent to the second heating flocculator X02 the feed liquid of preheating by pipeline subsequently.
Secondary flocculates: the feed liquid after the first heating flocculator X01 preheating enters the further heat temperature raising of the second heating flocculator X02, feed temperature will be promoted to 90 ~ 100 DEG C, albumen in feed liquid flocculates further under heating and acidic conditions, the thermal medium of the second heating flocculator X02 derives from insulation flocculator X04, and temperature is about 120 DEG C.Feed liquid after the heating of deuterostrophies flocculator is transported to steam heater by pipeline.First and second heating flocculator adopts spiral-plate heat exchanger to form, and it is complete welded structure, is separated by long pipeline, and this allows the albumen of flocculation in whole warm, keep same flow velocity slowly to heat, and ensure that quality and the homogeneity of albumen.
Heating and thermal insulation: through the feed liquid of the second heating flocculator X02 heating, by a steam heater by the steam injection of boiler house in feed liquid, steam mixes completely with feed liquid, by the most efficient this heat energy utilization, by more than feed temperature transient rise to 120 DEG C.Feed liquid after heating enters in follow-up insulation flocculator X04 carries out insulation flocculation, makes the albumen in feed liquid (comprising the albumen of small molecules chain) conglomeration of fully flocculating, improves the extraction efficiency of albumen.
Cooling is separated: after insulation containing albumen feed liquid, as thermal source, the albumen feed liquid newly entered is heated respectively by first and second heating flocculator, realizes the cooling of flocculation albumen feed liquid, promote flocculation and energy efficient.
Dewatering unit T1 is that horizontal spiral water extracter is formed, for drying unit G1, concrete employing is as Fig. 5, technical scheme shown in 6 is implemented, drying unit G1 comprises the flash dryer G11 sequentially arranged, pneumatic drier and first, two cyclonic separators, pneumatic drier comprises inverted U-shaped drying tube G12, one end of drying tube G12 connects the material inlet of the first cyclonic separator G13, the other end of drying tube G12 connects the material outlet of flash dryer G11 and the air outlet of the second airheater G152 respectively, second airheater G152 is connected with the second blower fan G162, the air outlet of the first cyclonic separator G13 is connected with the material inlet of the second cyclonic separator G14.Flash dryer G11 is connected with the air outlet of the first airheater G151, first airheater G151 comprises first, second and third set of heat exchange tubes sending direction to set gradually along wind in housing and housing, first set of heat exchange tubes is connected with the first hot fluid outlet ports heating flocculator X01, second set of heat exchange tubes is connected with the 3rd hot fluid outlet ports heating flocculator X03,3rd set of heat exchange tubes is connected with steam pipeline, and the first airheater G151 is connected with the first blower fan G161.The first airheater G151 is entered by pipeline from the first heating flocculator X01 feed liquid out, be preheating of air by temperature remaining in feed liquid, carry out energy-conservation further, the flocculation albumen feed liquid after airheater heat exchange enters horizontal spiral centrifuge and carries out solid-liquid separation.Isolated liquid enters subsequent evaporation upgrading unit, is finally made into liquid fertilizer.Isolated solid materials is wet albumen, the water content about about 70% of wet albumen.
The horizontal screw conveyer arranged by bottom through the isolated albumen of horizontal spiral centrifuge and inclined screw conveyor enter drying unit G1.Consider that the material characteristic of Rhizoma Solani tuber osi protein adopts flash dryer G11 and pneumatic drier coupling to carry out drying.Albumen enters the kiln of flash dryer G11 by screw feeder (auger G17); warm air enters stirring by inlet tube with suitable spout velocity and pulverizes kiln bottom flash dryer G11; strong shearing is produced to albumen, blows floating, turning effort; albumen be subject to centrifugal, shear, collision, friction and by micronize, enhancing mass and heat transfer.Bottom flash dryer G11, comparatively large comparatively wet granule protein group is by mechanical disintegration under the effect of stirring mechanism, and the protein grain that moisture content is lower, granularity is less is carried secretly rising by swirling eddy, dry further in uphill process.Because gas-particle two-phase makes rotational flow, solid phase inertia is greater than gas phase, and the speed of relative movement that solid and gas two is alternate is comparatively large, and the mass-and heat-transfer that strengthening two is alternate, so this machine production intensity is high.The dried albumen water content of drying unit G1 is about about 10 ~ 12%, enters screening packaging unit subsequently.
Detailed scheme is as Fig. 7, shown in 8, the bottom of flash dryer G11 is provided with sloped footing G111 and stirring mechanism, stirring mechanism comprises the stir shaft G101 that vertical shape is arranged, one end of stir shaft G101 to extend in flash dryer G11 through sloped footing G111 and arranges the stirrer gear G103 for comminuting matter at this end, the other end of stir shaft G101 carries out rotation by the bearing support that flash dryer G11 bottom outside is arranged and installs, stirrer gear G103 is provided with the scraper plate G104 for striking off adhesion protein on flash dryer G11 inwall away from one end of stir shaft, the top of flash dryer G11 arranges spinning disk.The blade G102 of the layered arrangement that stir shaft is arranged and rake teeth, make material and gas mix reinforcement in length and breadth, and inter-particle collision, friction are accelerated, and bubble is broken, and aggregative fluidization becomes particulate fluidization, improves heat and mass efficiency, and play certain porphyrization.Be provided with inner cone structure bottom drying machine, warm air flow area is constantly expanded from bottom to top, gas speed in bottom is large, and top gas speed is little, makes bottom macrobead and top small-particle be in good fluidized state.In addition, sloped footing G111 can shorten stir shaft G101 jib-length, and increase serviceability, bearing support is located at outside machine, avoids bearing in high-temperature zone long term operation, extends the work-ing life of bearing.While wet stock is stirred tooth pulverizing, part is thrown toward wall, being bonded on wall, as scraped not in time, can affecting quality product, by arranging scraper plate G104 on stirrer gear G103 top, preventing material from gluing wall and crossing thermally denature.The spinning disk that kiln top is arranged, effectively ensures material moisture content and fineness.In addition, cold wind protection can be provided with at cone hot-wind inlet place, the end, prevent material from contacting with high temperature air and produced thermal metamorphism.Because flash dryer G11 inlet temperature is higher, therefore bearing support also can arrange hydrologic cycle cooling system; The outer wall of flash dryer G11 adopts carbon steel to make, and is incubated, and lagging material is high-quality pure aluminium silicate, arranges the foreskin that A3 steel is made outside lagging material.First cyclonic separator G13 is centrifugal cyclonic separator, and to make the separated collection of the material of more than 85%, the first cyclonic separator G13 bottom adopts star air sealer to carry out discharging.Second cyclonic separator G14 is cleaning apparatus, and object collects superfine material, makes exhaust emissions reach the emission standard of country.
Dried albumen enters packaging feed bin, according to customer demand screening, packaging, finally delivers to warehouse and stores.Long-time storage and long-distance transportation is realized because dried albumen water content is low.
This system is also configured with the cleaning unit Q1 of full-automatic on-line cleaning in addition, cleaning unit Q1 comprises alkali liquor storage tank Q12 and process water storage tank Q13, solution in alkali liquor storage tank Q12 is prepared by the sodium hydroxide in sodium hydroxide storage tank Q11 and process water and is obtained, sodium hydroxide solution and process water are pumped to each unit by flushing water pump Q14 and clean each equipment, only need 1 operator to operate.The non-soluble protein extraction yield of this system is up to 90%, and energy consumption is low, can need production feed grade albumen and food-grade albumen according to client.
The above is only the preferred embodiment of the present invention; should be understood that; for those skilled in the art; to know in the present invention after contents; under the premise without departing from the principles of the invention; can also make some equal conversion to it and substitute, these convert on an equal basis and substitute and also should be considered as belonging to protection scope of the present invention.
Claims (10)
1. a Rhizoma Solani tuber osi protein production technique, comprises following operation:
S1: the fiber in starch waste liquor and starch removal are obtained albumen feed liquid at separating unit;
S2: the PH of albumen feed liquid is adjusted to 5 ~ 5.2 at PH regulon;
S3: first albumen feed liquid is heated to 90 ~ 100 DEG C piecemeal at flocculation unit, then adopts steam albumen feed liquid to be heated to 120 DEG C and carries out insulation flocculation, cool after insulation flocculation;
S4: the albumen feed liquid after flocculation is delivered to dewatering unit and dewaters, be delivered to drying unit after dehydration and carry out drying.
2. Rhizoma Solani tuber osi protein production technique according to claim 1, it is characterized in that: separating unit comprises the foam tank that disappears, the foam tank that disappears comprises the tank body that circular vertical shape is arranged, outer tank skin in the middle part of tank body is provided with the cloth mouth tangentially sending into starch wastewater in tank body, be provided with in tank body, first of lower layout, two cone-shaped hoods, the cover mouth of the first cone-shaped hood upwards, the cover mouth of the second cone-shaped hood is downward, tank body is also respectively arranged with protein recycling pipe, fiber recovery pipe and recovery of starch pipe, the inlet end of fiber recovery pipe extends to the bottom in the first cone-shaped hood, top in the second cone-shaped hood that the inlet end of protein recycling pipe extends to, the inlet end of recovery of starch pipe is positioned at the bottom of tank body.
3. Rhizoma Solani tuber osi protein production technique according to claim 1 and 2, it is characterized in that: flocculation unit comprise sequentially connect arrange for albumen feed liquid is carried out heat flocculation each heating flocculator and for albumen feed liquid is carried out be incubated flocculation insulation flocculator, insulation flocculator comprises the spiral conveying tube arranged in insulation shell and insulation shell, the heart yearn of spiral conveying tube is arranged in the horizontal direction, the caliber of spiral conveying tube is 1.5 ~ 2.5 times of albumen feed liquid transfer lime caliber, albumen feed liquid transfer lime is carry out for albumen feed liquid the pipeline carried between neighbouring device.
4. Rhizoma Solani tuber osi protein production technique according to claim 1 and 2, it is characterized in that: drying unit comprises the flash dryer, pneumatic drier and first and second cyclonic separator that sequentially arrange, pneumatic drier comprises inverted U-shaped drying tube, one end of drying tube connects the material inlet of the first cyclonic separator, the other end of drying tube connects the material outlet of flash dryer and the air outlet of the second airheater respectively, second airheater is connected with the second blower fan, and the air outlet of the first cyclonic separator is connected with the material inlet of the second cyclonic separator.
5. Rhizoma Solani tuber osi protein production technique according to claim 4, it is characterized in that: the bottom of flash dryer is provided with sloped footing and stirring mechanism, stirring mechanism comprises the stir shaft that vertical shape is arranged, one end of stir shaft to extend in flash dryer through sloped footing and arranges the stirrer gear for comminuting matter at this end, the other end of stir shaft carries out rotation by the bearing support that flash dryer bottom outside is arranged and installs, stirrer gear is provided with the scraper plate for striking off adhesion protein on flash dryer inwall away from one end of stir shaft, the top of flash dryer arranges spinning disk.
6. Rhizoma Solani tuber osi protein production technique according to claim 3, it is characterized in that: flocculation unit comprises first, two, three heating flocculators and insulation flocculator, first, two heating flocculators are spiral-plate heat exchanger and form, 3rd heating flocculator is that steam heater is formed, the cold fluid inlet of the first heating flocculator is connected with PH regulon, the cold fluid outlet of the first heating flocculator is connected with the second cold fluid inlet heating flocculator, the cold fluid outlet of the second heating flocculator is connected with the 3rd cold fluid inlet heating flocculator, the cold fluid outlet of the 3rd heating flocculator is connected with the material inlet of insulation flocculator, the thermal fluid inlet of the 3rd heating flocculator is connected with steam pipeline, the thermal fluid inlet of the second heating flocculator is connected with the material outlet of insulation flocculator, the hot fluid outlet ports of the second heating flocculator is connected with the first thermal fluid inlet heating flocculator.
7. Rhizoma Solani tuber osi protein production technique according to claim 2, it is characterized in that: the top tank skin of the foam tank that disappears also is provided with the connection mouth of pipe, connect the top that the mouth of pipe is positioned at the first cone-shaped hood, connect the mouth of pipe and connect the 3rd blower fan and bubble collapse device successively, bubble collapse device comprises body, and in body, interval arranges the filter or grid that are used for broken foam.
8. Rhizoma Solani tuber osi protein production technique according to claim 2, it is characterized in that: the top of the foam tank that disappears is provided with shower nozzle, the other end of fiber recovery pipe is connected by the centrifugal screen of first pump housing with Separation and Recovery fiber, and the waste water discharge opening of centrifugal screen is connected with shower nozzle by second pump housing.
9. Rhizoma Solani tuber osi protein production technique according to claim 5, it is characterized in that: flash dryer is connected with the air outlet of the first airheater, first airheater comprises first, second and third set of heat exchange tubes sending direction to set gradually along wind in housing and housing, first set of heat exchange tubes is connected with the first hot fluid outlet ports heating flocculator, second set of heat exchange tubes is connected with the 3rd hot fluid outlet ports heating flocculator, 3rd set of heat exchange tubes is connected with steam pipeline, and the first airheater is connected with the first blower fan.
10. Rhizoma Solani tuber osi protein production technique according to claim 1, is characterized in that: dewatering unit is that horizontal spiral water extracter is formed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510616389.7A CN105111276A (en) | 2015-09-24 | 2015-09-24 | Potato protein production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510616389.7A CN105111276A (en) | 2015-09-24 | 2015-09-24 | Potato protein production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105111276A true CN105111276A (en) | 2015-12-02 |
Family
ID=54659425
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510616389.7A Pending CN105111276A (en) | 2015-09-24 | 2015-09-24 | Potato protein production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105111276A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111499017A (en) * | 2020-03-14 | 2020-08-07 | 烟台大学 | Device and method for quickly separating protein and starch in wastewater in starch processing process |
| CN111518160A (en) * | 2020-04-27 | 2020-08-11 | 中国环境科学研究院 | Process and device for recovering protein in starch production wastewater |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204939352U (en) * | 2015-09-15 | 2016-01-06 | 安徽泰德康农业科技发展有限公司 | A kind of drying unit produced for Rhizoma Solani tuber osi protein |
| CN204939354U (en) * | 2015-09-16 | 2016-01-06 | 安徽泰德康农业科技发展有限公司 | A kind of foam tank that disappears produced for Rhizoma Solani tuber osi protein |
| CN204939353U (en) * | 2015-09-16 | 2016-01-06 | 安徽泰德康农业科技发展有限公司 | A kind of flocculation unit produced for Rhizoma Solani tuber osi protein |
| CN204981704U (en) * | 2015-09-15 | 2016-01-20 | 安徽泰德康农业科技发展有限公司 | A separating element for production of potato albumen |
-
2015
- 2015-09-24 CN CN201510616389.7A patent/CN105111276A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204939352U (en) * | 2015-09-15 | 2016-01-06 | 安徽泰德康农业科技发展有限公司 | A kind of drying unit produced for Rhizoma Solani tuber osi protein |
| CN204981704U (en) * | 2015-09-15 | 2016-01-20 | 安徽泰德康农业科技发展有限公司 | A separating element for production of potato albumen |
| CN204939354U (en) * | 2015-09-16 | 2016-01-06 | 安徽泰德康农业科技发展有限公司 | A kind of foam tank that disappears produced for Rhizoma Solani tuber osi protein |
| CN204939353U (en) * | 2015-09-16 | 2016-01-06 | 安徽泰德康农业科技发展有限公司 | A kind of flocculation unit produced for Rhizoma Solani tuber osi protein |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111499017A (en) * | 2020-03-14 | 2020-08-07 | 烟台大学 | Device and method for quickly separating protein and starch in wastewater in starch processing process |
| CN111518160A (en) * | 2020-04-27 | 2020-08-11 | 中国环境科学研究院 | Process and device for recovering protein in starch production wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR100965932B1 (en) | Control system for efficient drying and bad smell of organic waste | |
| CN204939354U (en) | A kind of foam tank that disappears produced for Rhizoma Solani tuber osi protein | |
| KR101082508B1 (en) | The apparatus for drying food waste sludge using superheated-steam and the second gas | |
| CN203928599U (en) | Energy saving expansion drying combination unit | |
| CN102531315A (en) | Sludge hydrothermal drying treating device and hydrothermal reactor thereof | |
| JP2012187449A (en) | Thermal dehydration of sludge | |
| CN107048248A (en) | A kind of device for krill high speed cooking | |
| CN109574426A (en) | A kind of oily sludge object harmless resource utilization device and method | |
| CN105111276A (en) | Potato protein production process | |
| CN203964623U (en) | The flash distillation main frame of energy saving expansion drying combination unit | |
| CN204939353U (en) | A kind of flocculation unit produced for Rhizoma Solani tuber osi protein | |
| CN204939352U (en) | A kind of drying unit produced for Rhizoma Solani tuber osi protein | |
| CN205473498U (en) | Potato albumen production system | |
| CN204981704U (en) | A separating element for production of potato albumen | |
| CN105327765A (en) | High-moisture low-rank coal pulverizing and water recycling system and method | |
| CN102531314B (en) | Sludge water heat drying treatment device and flashing reactor thereof | |
| CN100551264C (en) | The recoverying and utilizing method of steam drying waste heat in the glutamate production process | |
| CN110229690A (en) | Containing solid oils or oil-containing solid phase solvent extraction recycling and processing device and method | |
| CN205295199U (en) | A air heating unit for production of potato albumen | |
| CN102531321A (en) | Sludge water heat drying treatment device and homogeneous reactor thereof | |
| CN209602363U (en) | A kind of device using brickkiln smoke residual heat to dry sludge | |
| CN216426800U (en) | System for chloride ion content in slurry at bottom of ammonia process desulfurizing tower | |
| JP2005083644A (en) | Drier | |
| CN212205356U (en) | Industrial salt drying equipment | |
| CN102557384A (en) | Sludge hydrothermal drying treatment device and slurry reactor thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20151202 |
|
| WD01 | Invention patent application deemed withdrawn after publication |