CN205295199U - A air heating unit for production of potato albumen - Google Patents

Abstract

The utility model relates to an air heating unit for production of potato albumen, including an air heater, the flash drying machine is connected with an air heater's air outlet, and an air heater follows first, two, three heat exchange tube group that wind sent the orientation to set gradually in including casing and casing, and a heat exchange tube group is connected with the hot -fluid export of first heating flocculator, and the 2nd heat exchange tube group is connected with the hot -fluid export of third heating flocculator, and the 3rd heat exchange tube group is connected with delivery duct, and an air heater is connected with first fan. Through above -mentioned system, it can be used for albumen dry by quick heated air, energy saving and reduction in production cost.

Description

A kind of air-heating unit produced for Rhizoma Solani tuber osi protein

Technical field

This utility model relates to protein production field, is specifically related to a kind of air-heating unit produced for Rhizoma Solani tuber osi protein.

Background technology

Potato starch production line can discharge substantial amounts of waste water, due in waste water containing substantial amounts of albumen, therefore this effluent part is pumped to protein production systems and carries out extracting and reclaim albumen by general manufacturer. But, all there is different defects in presently used protein production systems, it is therefore necessary to make improvements in production efficiency, the response rate and energy consumption etc., to improve the economic benefit that Rhizoma Solani tuber osi protein produces further.

Utility model content

The purpose of this utility model is just to provide a kind of air-heating unit produced for Rhizoma Solani tuber osi protein, and it can be used for extracting from starch production wastewater reclaiming albumen.

For achieving the above object, this utility model have employed techniques below scheme:

A kind of air-heating unit produced for Rhizoma Solani tuber osi protein, it is characterized in that: include the first air heater, the air outlet of flash dryer and the first air heater is connected, first air heater includes 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 air heater and the first blower fan are connected.

By said system, it can quickly add hot-air and dry for albumen, saves the energy and reduces production cost.

Accompanying drawing explanation

Fig. 1 is the structural representation of Rhizoma Solani tuber osi protein production system;

Fig. 2 is the structural representation of separative element;

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 air heater;

Fig. 7 is the structural representation of sloped footing;

Fig. 8 is the structural representation of rabbling mechanism.

Detailed description of the invention

In order to make the purpose of this utility model and advantage clearly understand, below in conjunction with embodiment, this utility model is specifically described.Should be appreciated that following word is only in order to describe one or more specific embodiments of the present utility model, the protection domain this utility model specifically not asked carries out considered critical.

A kind of air-heating unit produced for Rhizoma Solani tuber osi protein, including the sequentially front latter linked separative element F1 for the starch in starch wastewater, albumen, fiber are easily separated, for the separative element F1 albumen feed liquid separated and recovered being carried out the PH regulon P1 of PH adjustment, for the albumen feed liquid after regulating PH being carried out the flocculation unit X1 of flocculation treatment, for the albumen after flocculation being carried out the dewatering unit T1 of solid-liquid separation, and the drying unit G1 for the albumen after dehydration is dried.

Its technological operation is:

A kind of Rhizoma Solani tuber osi protein production technology, including following operation:

S1: the fiber in starch waste liquor and starch removal are obtained albumen feed liquid at separative element F1;

S2: the PH of albumen feed liquid is regulated to 5��5.2 at PH regulon P1;

S3: first albumen feed liquid heated piecemeal to 90��100 DEG C at flocculation unit X1, then adopts steam that to 120 DEG C, the heating of albumen feed liquid is carried out insulation flocculation, cools down after insulation flocculation;

S4: the albumen feed liquid after flocculation is delivered to dewatering unit T1 and carries out dehydration, be delivered to drying unit G1 after dehydration and be dried.

The starch waste liquor that overflow is discharged is reclaimed, containing a small amount of nominal particle size starch and fiber fines in waste liquid from Starch Production line rotational flow station. Hot flocculation process can be extracted albumen and produce very big adverse effect by the existence of these materials, it is necessary to adopt an effective measure removal remaining starch and fiber.

Concrete measure is, such as Fig. 1, 2, shown in 3, separative element F1 includes the foam tank F20 that disappears, the foam tank F20 that disappears includes 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, it is provided with in tank body, the first of lower layout, two cone-shaped hoods, the cover mouth of the first cone-shaped hood F21 is upwards, the cover mouth of the second cone-shaped hood F22 is downward, tank body is also respectively provided with protein recycling pipe F26, fiber recovery pipe F27 and recovery of starch pipe F28, the arrival 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 arrival end of protein recycling pipe F26 extends to, the arrival end of recovery of starch pipe F28 is positioned at the bottom of tank body. cloth mouth F23 is that arc pipe fitting is constituted, and arc pipe fitting is gradually increased along the cross section of feed liquid conveying 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 by the screen centrifuge F14 of the first pump housing F13 with separation and recovery fiber, and the waste water discharge opening of screen centrifuge 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 into tank bottoms, and is discharged by the recovery of starch pipe F28 of tank bottoms setting. light phase portion foam and fine fibre float up to the foam tank F20 top that disappears, by discharging from fiber recovery pipe F27 after shower water froth breaking, discharge liquid and enter a thin fine screen centrifuge F14, fine fibre is separated and removes, and eliminate foam further, last blowback again, to the foam tank F20 that disappears, sprays foam that the foam in tank body is disappeared from shower nozzle.

First cone-shaped hood F21 arranges the collection being mainly beneficial to fiber, and arranging of the second cone-shaped hood F22 mainly prevents from being stirred by the starch that tank base precipitates during fluid backspin, affects the reliable separation of starch, albumen. It is 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 is adjusted.

More specifically scheme is, disappear and the top tank skin of foam tank F20 is additionally provided with connection mouth of pipe F24, connect mouth of pipe F24 and be positioned at the top of the first cone-shaped hood F21, connect mouth of pipe F24 and be sequentially connected with the 3rd blower fan F11 and bubble collapse device F12, bubble collapse device F12 includes body, and in body, interval is provided to break up the filter of foam or grid and disappears a large amount of foams produced in foam tank F20 with further removing.

PH regulon P1 includes acid solution storage tank and membrane pump, stores food stage sulphuric acid in acid solution storage tank, regulates the pH value of albumen feed liquid by being continuously added into food stage sulphuric acid in albumen feed liquid conveying pipe (the pump preceding pipeline of feed pump). From disappearing, the foam tank F20 albumen feed liquid discharged squeezes into flocculation unit X1 by feed pump, it is contemplated that the feed liquid conveying of whole extraction system for protein relies primarily on feed pump and completes, and feed liquid flow process is longer, therefore adopts high-lift multi-stage centrifugal pump. Canned sulphuric acid is quantitatively delivered into albumen feed liquid conveying pipe by membrane pump, due to the physical characteristic of dilute sulfuric acid, it is impossible to produce feed liquid refluence phenomenon, otherwise can produce major accident.

Flocculation unit X1 specifically adopts technical scheme to be as shown in Figure 4 carried out, flocculation unit X1 include sequentially connecting arrange for albumen feed liquid being heated each heating flocculator of flocculation and for albumen feed liquid being carried out the insulation flocculator X04 of insulation flocculation, insulation flocculator X04 includes 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 conveying pipe caliber, albumen feed liquid conveying pipe is be used for the pipeline that albumen feed liquid carries out carrying between neighbouring device, such feed liquid flowing velocity in insulation flocculator X04 is slower, albumen can fully be flocculated condensation. flocculation unit X1 includes first, two, three heating flocculators and insulation flocculator X04, first, two heating flocculators are spiral-plate heat exchanger and constitute, 3rd heating flocculator X03 is steam heater or spiral-plate heat exchanger composition, 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 and the cold fluid inlet of the second heating flocculator X02 are connected, the cold fluid outlet of the second heating flocculator X02 and the cold fluid inlet of the 3rd heating flocculator X03 are connected, 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 and the thermal fluid inlet of the first heating flocculator X01 are connected.

Adopting above-mentioned flocculation unit X1 to flocculate, the albumen flocculation in feed liquid includes following operation:

One-level preheats: 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, add thermal medium be in the second heating flocculator X02 flow out add thermal medium, 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.

Two grades of flocculations: the feed liquid after first heats flocculator X01 preheating enters the second heating further heat temperature raising of flocculator X02, feed temperature will be promoted to 90��100 DEG C, albumen in feed liquid flocculates further under heating and acid condition, the thermal medium of the second heating flocculator X02 derives from insulation flocculator X04, and temperature is about 120 DEG C. Feed liquid after deuterostrophies flocculator heats is transported to steam heater by pipeline. First and second heating flocculator adopts spiral-plate heat exchanger to constitute, and it is complete welded structure, is separated by long pipeline, and this allows the albumen of flocculation keep same flow velocity to be slowly heated in whole warm, it is ensured that the quality of albumen and uniformity.

Heating and thermal insulation: through the second feed liquid heating flocculator X02 heating, a steam heater being injected in feed liquid by the steam of boiler room, steam and feed liquid are thoroughly mixed, by the most efficient this heat energy utilization, more than feed temperature transient rise to 120 DEG C. Feed liquid after heating enters and carries out insulation flocculation in follow-up insulation flocculator X04, makes the albumen in feed liquid (including the albumen of little strand) conglomeration of fully flocculating, improves the extraction efficiency of albumen.

Cooling separate: after insulation containing albumen feed liquid, respectively through first and second heat flocculator as thermal source, newly entering albumen feed liquid is heated, it is achieved flocculation albumen feed liquid cooling, promote flocculation and energy efficient.

Dewatering unit T1 is that horizontal spiral dewaterer is constituted, for drying unit G1, specifically adopt such as Fig. 5, technical scheme shown in 6 is carried out, drying unit G1 includes the flash dryer G11 sequentially arranged, pneumatic drier and first, two cyclone separator, pneumatic drier includes inverted U-shaped drying tube G12, one end of drying tube G12 connects the material inlet of the first cyclone separator G13, the other end of drying tube G12 connects the material outlet of flash dryer G11 and the air outlet of the second air heater G152 respectively, second air heater G152 and the second blower fan G162 is connected, the air outlet of the first cyclone separator G13 and the material inlet of the second cyclone separator G14 are connected. the air outlet of flash dryer G11 and the first air heater G151 is connected, first air heater G151 includes 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 air heater G151 and the first blower fan G161 is connected. heat flocculator X01 feed liquid out from first and enter the first air heater G151 by pipeline, it is air preheat by temperature remaining in feed liquid, carrying out energy-conservation further, the flocculation albumen feed liquid after air heater heat exchange enters horizontal spiral centrifuge and carries out solid-liquid separation. isolated liquid enters subsequent evaporation upgrading unit, is finally fabricated to liquid fertilizer. isolated solid material 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 be dried. Albumen is entered the hothouse of flash dryer G11 by feed screw (auger G17); hot-air is entered stirring pulverizing hothouse with suitable spout velocity by inlet tube bottom flash dryer G11; albumen produced strong shearing, blow floating, turning effort; albumen is centrifuged, is sheared, is collided, is rubbed and by micronized, enhancing mass and heat transfer.Bottom flash dryer G11, relatively big relatively wet granule protein group is by mechanical activation comminution under the effect of rabbling mechanism, and the protein body that moisture content is relatively low, granularity is less is carried secretly rising by swirling eddy, is further dried in uphill process. Owing to gas-particle two-phase makes rotational flow, solid phase inertia is more than gas phase, and the relative velocity that solid and gas two is alternate is relatively big, the mass-and heat-transfer that strengthening two is alternate, so this machine produces intensity height. The dried albumen water content of drying unit G1 is about about 10��12%, subsequently enters screening packaging unit.

Detailed scheme such as Fig. 7, shown in 8, the bottom of flash dryer G11 is provided with sloped footing G111 and rabbling mechanism, rabbling mechanism includes the shaft G101 that vertical shape is arranged, one end traverse sloped footing G111 of shaft G101 extends in flash dryer G11 and is arranged to the stirrer gear G103 of comminuting matter at this end, the other end of shaft G101 is undertaken rotating by the bearing block that flash dryer G11 bottom outside is arranged to be installed, stirrer gear G103 is provided with for striking off the scraper plate G104 of adhesion protein on flash dryer G11 inwall away from one end of shaft, the top of flash dryer G11 arranges spinning disk. the blade G102 of the layered arrangement arranged on shaft 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, improve heat and mass efficiency, and play certain pulverization. being provided with inner cone structure bottom drying machine, make hot-air flow area constantly expand from bottom to top, gas speed in bottom is big, and top gas speed is little so that the little granule of bottom bulky grain and top is in good fluidized state. it addition, sloped footing G111 can shorten shaft G101 jib-length, increasing operational reliability, bearing block is located at outside machine, it is to avoid bearing, in high-temperature region long-term work, extends the service life of bearing. while wet stock is stirred tooth pulverizing, part is thrown toward wall, is bonded on wall, as scraped not in time, can affect product quality, by arranging scraper plate G104 on stirrer gear G103 top, it is prevented that thermal denaturation crossed by the viscous wall of material. the spinning disk that hothouse top is arranged, is effectively ensured material moisture content and fineness. it addition, cold wind protection can be provided with at cone hot-wind inlet place, the end, it is prevented that material contacts with high temperature air and produced thermal metamorphism. owing to flash dryer G11 inlet temperature is higher, therefore bearing block also can arrange hydrologic cycle cooling system, the outer wall of flash dryer G11 adopts carbon steel to make, and is incubated, and insulation material is high-quality aluminium silicate, arranges the foreskin that A3 steel is made outside insulation material. first cyclone separator G13 is centrifugal cyclone separator, so that the separated collection of material of more than 85%, the first cyclone separator G13 bottom adopts star airlock to carry out discharging. second cyclone separator G14 is dust arrester, it is therefore an objective to collect superfine material, makes exhaust emissions reach the discharge standard of country.

Dried albumen enters packaging feed bin, according to customer demand screening, packaging, finally delivers to warehouse storage. Long-time storage and long-distance transportation is realized owing to dried albumen water content is low.

Additionally this system is also configured with the cleaning unit Q1 of full-automatic on-line cleaning, cleaning unit Q1 includes alkali liquor storage tank Q12 and fresh water (FW) storage tank Q13, solution in alkali liquor storage tank Q12 is prepared by the sodium hydroxide in sodium hydroxide storage tank Q11 and fresh water (FW) and is obtained, sodium hydroxide solution and fresh water (FW) are pumped to each unit by flushing water pump Q14 and each equipment are carried out, it is only necessary to 1 operator can be operated.The non-soluble protein extraction ratio of this system is up to 90%, and energy consumption is low, it is possible to need to produce feed grade albumen and food-grade albumen according to client.

The above is only preferred implementation of the present utility model; should be understood that; for those skilled in the art; in knowing this utility model after contents; under the premise without departing from this utility model principle; it can also being made some equal conversion and replacement, these convert on an equal basis and substitute and also should be regarded as belonging to protection domain of the present utility model.

Claims (1)

1. the air-heating unit produced for Rhizoma Solani tuber osi protein, it is characterized in that: include the first air heater, the air outlet of flash dryer and the first air heater is connected, first air heater includes 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 air heater and the first blower fan are connected.