CN103575081A - Fermented feed drying method - Google Patents
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- CN103575081A CN103575081A CN201310540144.1A CN201310540144A CN103575081A CN 103575081 A CN103575081 A CN 103575081A CN 201310540144 A CN201310540144 A CN 201310540144A CN 103575081 A CN103575081 A CN 103575081A
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Abstract
The invention relates to a fermented feed drying method. The method comprises steps as follows in sequence: fresh fermented feed enters a feeding machine from a main feed opening, is lifted, then enters a feed opening of a tube-type drying machine, advances from front to back in the horizontal direction in the tube-type drying machine, and is subjected to indirect heat exchange with steam simultaneously; hot and humid air is exhausted by an exhaust fan from an exhaust outlet of the tube-type drying machine; the preliminarily dried fermented feed enters sieving and conveying equipment for sieving after discharged from the tube-type drying machine; after sieving, a screen underflow is sent into a feed opening in the top of a tower-type drying machine, and a screen overflow is sent into an auxiliary feed opening of the feeding machine and mixed with the fresh fermented feed; and the fermented feed moves from top to bottom in the tower-type drying machine, air enters an air inlet in the lower part of the tower-type drying machine after heated by an air heater, and hot air flows from bottom to top to perform secondary drying on the fermented feed and is exhausted from an air outlet in the upper part of the tower-type drying machine. The fermented feed drying method is low in energy consumption and high in drying efficiency, and can maintain the activity of the fermented feed.
Description
Technical field
The present invention relates to a kind of drying means of feed, particularly a kind of fermented feed drying means.
Background technology
In prior art, dry fluid bed dryer, rower drier, pipe drier, the canal drier etc. of conventionally adopting of fermented feed.Wherein pipe drier adopts high-temperature steam as thermal source, and heating-up temperature is high, and rate of drying is fast; Rower drier adopts hot blast as thermal source, and heating-up temperature is low, and rate of drying is slow.For enhancing productivity, the dry field of fermented feed adopts pipe drier very general.
Owing to can producing large number of biological enzyme isoreactivity material after feed fermentation, in dry run, if temperature of charge is higher than 70 ℃ (different product material heatproof is different), fermented feed easily loses activity, and therefore, fermented feed belongs to heat sensitive material.
Because fresh fermented feed is moister, while adopting pipe drier to be dried, easily occur that material is bonded on tube wall to cause hot-spot, the inequality of being heated, whole poor thermal efficiency; And because the temperature of the heat source medium steam of pipe drier is higher, after fermented feed product drying, ubiquity activity is little, the problem of product sex change, as adopted Low Temperature Steam to have again the problem that production efficiency is low.
Rower drier adopts relatively gentle hot blast to dry, although can avoid fermented feed sex change, drying time is long, and production efficiency is low, and energy consumption is too high.
Summary of the invention
The object of the invention is to, overcome problems of the prior art, a kind of fermented feed drying means is provided, drying efficiency is high and can keep the activity of fermented feed.
For solving above technical problem, a kind of fermented feed drying means of the present invention, in turn include the following steps: fresh fermented feed enters from the main charging aperture of feeder lower end, material outlet from feeder upper end after promoting is discharged, then fermented feed enters the charging aperture of pipe drier, in pipe drier, fermented feed along continuous straight runs advances after by forward direction, when advancing and steam carry out indirect heat exchange, Hot wet air heating after heat exchange is extracted out by exhaust blower from the exhaust outlet of pipe drier, the fermented feed of preliminarily dried is discharged from the discharging opening of pipe drier, enter again the screening of screening conveying equipment, after screening, screenings is admitted to the charging aperture at rower drier top, the auxiliary charging aperture that oversize is admitted to described feeder mixes with fresh fermented feed, described auxiliary charging aperture is positioned at described main charging aperture top, in rower drier, fermented feed moves to the discharging opening discharge of bottom from the top down, air enters the air inlet of rower drier bottom after air heater heating, and hot blast flows from bottom to top fermented feed is carried out from the air outlet on rower drier top, discharging after redrying.
With respect to prior art, the present invention has obtained following beneficial effect: (1) the fermented feed of fresh humidity enters feeder jointly with the preliminary fermented feed of drying of process from screening conveying equipment, at feeder, promote in course of conveying and mixed and stirred, the fermented feed overall humidity that enters pipe drier is declined, avoid occurring collophore phenomenon at pipe drier, fermented feed is heated evenly, hot-spot can not occur, fermented feed particle can be fully and thermal source carry out heat exchange, the thermal efficiency is high; (2) in pipe drier, although vapor (steam) temperature is very high, because the humidity of fermented feed is now very large, moisture can absorb a large amount of heats when evaporation, as long as still retain certain humidity while making pipe drier discharging, needn't reach the low moisture levels of finished product, can make the temperature of fermented feed self below safe temperature, can loss of activity; (3) the fermented feed of preliminarily dried is discharged from pipe drier, enter the screening of screening conveying equipment, drier particle becomes screenings and enters the continuation oven dry of lower road, reduced the oven dry load of rower drier, more sluggish in the time of relatively moist fermented feed motion, become oversize and be back in feeder and fresh fermented feed blending; (4) the fermented feed that enters rower drier moves from the top down, and hot blast flows from bottom to top, and both move toward one another make to flow through hot blast relative velocity of fermented feed is higher, is conducive to the evaporation of residual moisture in fermented feed; The hot blast temperature on rower drier top reduces, and the fermented feed temperature that has now just entered rower drier is also minimum, and both can keep good drying effect; The fermented feed temperature that arrives tower drying motor spindle raises, and what now contact with it is just to have entered the highest hot blast of rower drier temperature, and both still can keep good drying effect; When fermented feed temperature is very low, humidity is very high time, adopts high-temperature medium to its indirect heating, drying, is conducive to shorten drying time, improves drying efficiency; When fermented feed temperature raises, residual humidity is lower time, adopts gentle hot blast to carry out direct convection stoving, both guaranteed that fermented feed can Yin Gaowen loss of activity, improved again rate of drying, overall energy consumption is low.
As improvement of the present invention, described air heater is included in mid temperature heat exchanger and the high-temperature heat-exchanging being connected in series successively in air direction of advance, and air is entered the air inlet of described rower drier successively after mid temperature heat exchanger and high-temperature heat-exchanging heating; High-temperature steam enters to discharge in described high-temperature heat-exchanging to be become high-temperature condensation water after latent heat and discharges, high-temperature condensation water enters flash tank flash distillation becomes flash-off steam, flash-off steam enters after mid temperature heat exchanger continues to discharge latent heat becomes middle temperature condensed water discharge, middle temperature condensed water by warm condensate pump through in warm condensed water stop valve send into recycling condensing water pipe, described recycling condensing water pipe is connected with recycling condensing water system by the first stop valve.Air is first heated by mid temperature heat exchanger, temperature is heated by high-temperature heat-exchanging after raising again, high-temperature steam enters to discharge in high-temperature heat-exchanging to be become high-temperature condensation water after latent heat and discharges, high-temperature condensation water enters flash tank flash distillation becomes flash-off steam, flash-off steam enters mid temperature heat exchanger and continue to discharge and to become middle temperature condensed water after latent heat and discharge, middle temperature condensed water by warm condensate pump send into recycling condensing water system, so realized the cascade utilization of steam energy, reduce steam consumption quantity, the thermal efficiency is high.
As a further improvement on the present invention, the Hot wet air heating of discharging from described pipe drier is sent into the air inlet on used heat absorption tower by described exhaust blower, in used heat absorption tower, recirculated water is carried out after heat release from the air outlet at top, used heat absorption tower to airborne release, the water inlet on used heat absorption tower is flowed back in the heat release rear flank that the recirculated water flowing out from the delivery port on used heat absorption tower is sent into hot water heat exchanger by circulating pump; Hot water carries out indirect preheating to air in low-temperature pre-heater, air after preheating enters mid temperature heat exchanger to be continued to be heated, the water outlet of low-temperature pre-heater is flowed through and by heat-exchanger pump, is sent back to the water inlet of low-temperature pre-heater after the heat absorbing side of described hot water heat exchanger, in hot water heat exchanger, the recirculated water on used heat absorption tower carries out indirect heat release to the hot water of low-temperature pre-heater.In pipe drier, humidity of materials is higher, the dust of discharge seldom with the wind, and air draft has higher temperature, by exhaust blower, sent into used heat absorption tower recirculated water is carried out to heat release, recirculated water enters hot water heat exchanger after absorbing heat again, carry out indirect heat exchange with the hot water of low-temperature pre-heater, the hot water of low-temperature pre-heater is realized preheating to air, and the air after preheating enters mid temperature heat exchanger to be continued to be heated; Not only realized the UTILIZATION OF VESIDUAL HEAT IN of pipe drier air draft, reduced the consumption of air heater steam, and utilized hot water heat exchanger to carry out indirect heat exchange, can guarantee that hot water is not affected by the dust in material air draft, can fouling in low-temperature pre-heater.
As another step of the present invention, improve, described air heater also comprises the cryogenic heat exchanger being serially connected with between described low-temperature pre-heater and described mid temperature heat exchanger, described recycling condensing water pipe is connected with the water inlet of described cryogenic heat exchanger by the second stop valve, middle temperature condensed water becomes cryogenic condensation water discharge sensible heat in cryogenic heat exchanger after, then flows into described recycling condensing water system.Between low-temperature pre-heater and mid temperature heat exchanger, be connected in series cryogenic heat exchanger, make air along low-temperature pre-heater, cryogenic heat exchanger, mid temperature heat exchanger and high-temperature heat-exchanging successively cascade raising temperature, can again utilize the middle temperature condensed water producing after flash-off steam heat release, further reduce steam consumption and improve efficiency of energy utilization.
As improvement of the present invention, the condensation-water drain of described pipe drier also accesses the condensing water inlet of described flash tank; The bottom of described flash tank is connected with flash tank condensate pump, and described flash tank condensed water delivery side of pump is connected with described recycling condensing water pipe by flash tank condensed water stop valve.The condensed water of pipe drier discharge also enters flash tank and carries out secondary flash distillation utilization, improves efficiency of energy utilization; The condensed water of flash tank bottom can be sent into recycling condensing water pipe by flash tank condensate pump, both can directly enter recycling condensing water system, enters recycling condensing water system after can entering again cryogenic heat exchanger heat release again, guarantees that waste heat is fully utilized.
As another improvement of the present invention, the tail gas of discharging from described rower drier top air outlet enters cyclone separator to carry out centrifugation, from the air outlet of described cyclone separator, through exhaust fan, be discharged into atmosphere, the fermented feed of separating flows back to described screening conveying equipment by feed back pipe from the discharge gate of described cyclone separator.Because the discharging of rower drier is to meet the dry fermented feed requiring; therefore in air draft, contain more dust and fermented feed chip, install cyclone separator additional and on the one hand tail gas is carried out discharging after dedusting, protection of the environment; can reclaim fermented feed chip on the other hand, cut the waste.
As preferred version of the present invention, enter the oversize of the auxiliary charging aperture of described feeder and the mass ratio of fresh fermented feed for (1-3): 8, the fermented feed moisture content of described pipe drier discharging opening is 20%-25%, and the fermented feed moisture content of described rower drier discharging opening is 8%-12%.Oversize and fresh fermented feed, under this mixed proportion, make fermented feed in pipe drier, can avoid occurring collophore phenomenon, fermented feed is heated evenly, can there is not hot-spot, fermented feed particle can be fully and thermal source carry out heat exchange, the thermal efficiency is high; Fermented feed is divided into two sections and heats, moist in the situation that, adopt pipe drier to force hot indirect drying, in the situation that moisture content is lower, adopting rower drier to carry out weak heating directly dries, pipe drier outlet keeps the moisture content of 20%-25%, both can make the temperature of fermented feed self below 70 ℃, can loss of activity, guaranteed again drying efficiency, overall energy consumption level is low.
As preferred version of the present invention, the steam inlet temperature of described pipe drier is 135 ℃-140 ℃, and the temperature of described pipe drier condensation-water drain is 110 ℃-115 ℃, and the fermented feed outlet temperature of described pipe drier is 45 ℃-55 ℃; The hot blast inlet temperature of described rower drier is 80 ℃-90 ℃, and the temperature of outgoing air of described rower drier is 50 ℃-55 ℃, and the fermented feed outlet temperature of described rower drier is 60 ℃-70 ℃.At pipe drier, adopt the high-temperature steam of 135 ℃-140 ℃ to comprise drying efficiency, in rower drier, adopt the hot blast of 80 ℃-90 ℃ to guarantee drying effect, the temperature of fermented feed self is all the time below 70 ℃, can loss of activity, guaranteed again drying efficiency.
As preferred version of the present invention, the temperature of outgoing air of described pipe drier is 75 ℃-80 ℃, the temperature of outgoing air on described used heat absorption tower is 55 ℃-60 ℃, and the inflow temperature of described low-temperature pre-heater is 65 ℃-70 ℃, and the leaving water temperature of described low-temperature pre-heater is 50 ℃-55 ℃.Waste heat in pipe drier air draft is further utilized, tentatively improve the temperature of air, reduce the steam consumption quantity of air heater.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation, and accompanying drawing only provides reference and explanation use, non-in order to limit the present invention.
Fig. 1 is the structural representation of fermented feed drying means of the present invention.
In figure: 1. feeder; 1a. material loading owner charging aperture; The auxiliary charging aperture of 1b. feeder; 1c. feeder discharging opening;
2. pipe drier; 2a. tube type drying machine inlet capable; 2a '. pipe drier discharging opening; 2b. pipe drier steam inlet; 2b '. pipe drier condensation-water drain;
3. sieve conveying equipment; 3a. screening conveying equipment charging aperture; The outlet of 3b. screenings; The outlet of 3c. oversize; 3d. feed back entrance;
4. rower drier; 4a. tower drying machine inlet capable; 4a '. rower drier discharging opening; 4b. rower drier air inlet; 4b '. rower drier air outlet;
5. air heater; 5a. low-temperature pre-heater; 5b. cryogenic heat exchanger; 5c. mid temperature heat exchanger; 5d. high-temperature heat-exchanging;
6. flash tank; 6a. flash tank condensing water inlet; The outlet of 6b. flash tank flash steam; 6c. flash tank condensation-water drain;
7. exhaust blower;
8. used heat absorption tower; 8a. used heat absorption tower air inlet; 8a '. used heat absorption tower air outlet; 8b. used heat absorption tower water inlet; 8b '. used heat absorption tower delivery port; 8.2. circulating pump; 8.3. hot water heat exchanger;
9. cyclone separator; 9a. cyclone separator air inlet; 9b. cyclone separator air outlet; 9c. cyclone separator discharging opening;
10. exhaust fan;
Warm condensate pump in 11.; 11a. the first stop valve; 11b. the second stop valve; Warm condensed water stop valve in 11c.; 12. flash tank condensate pumps; 12a. flash tank condensed water stop valve;
13. heat-exchanger pumps; 14. main steam pipes; 15. recycling condensing water systems.
The specific embodiment
As shown in Figure 1, fermented feed drying means of the present invention comprises feeder 1, the pipe drier 2 that the steam of take is thermal source, screening conveying equipment 3, the rower drier 4 that the hot blast of take is thermal source, air heater 5, cyclone separator 9, used heat absorption tower 8 and hot water heat exchanger 8.3, fresh fermented feed enters from the material loading owner charging aperture 1a of feeder lower end, feeder discharging opening 1c is connected with the tube type drying machine inlet capable 2a of pipe drier, main steam pipe 14 is connected with the pipe drier steam inlet 2b of pipe drier, the exhaust outlet of pipe drier 2 is provided with exhaust blower 7.
The top of rower drier 4 is provided with tower drying machine inlet capable 4a and rower drier air outlet 4b ', and the bottom of rower drier 4 is provided with rower drier discharging opening 4a ' and rower drier air inlet 4b.
Pipe drier discharging opening 2a ' is connected with the screening conveying equipment charging aperture 3a of screening conveying equipment 3, the screenings outlet 3b of screening conveying equipment 3 is connected with tower drying machine inlet capable 4a, the oversize outlet 3c of screening conveying equipment 3 is connected with the auxiliary charging aperture 1b of feeder, and the auxiliary charging aperture 1b of feeder is positioned at material loading owner charging aperture 1a top.Hot blast is by the rear access of air heater 5 heating rower drier air inlet 4b.
Air heater 5 is included in low-temperature pre-heater 5a, cryogenic heat exchanger 5b, mid temperature heat exchanger 5c and the high-temperature heat-exchanging 5d being connected in series successively in air direction of advance.The hot-blast outlet of high-temperature heat-exchanging 5d is connected with rower drier air inlet 4b, the steam inlet of high-temperature heat-exchanging is connected with main steam pipe 14, the flash tank condensing water inlet 6a of the condensation-water drain access flash tank 6 of high-temperature heat-exchanging, the flash tank flash steam outlet 6b of flash tank is connected with the steam inlet of mid temperature heat exchanger 5c, the condensation-water drain of mid temperature heat exchanger 5c is connected with the entrance of middle temperature condensate pump 11, and in the outlet warp of middle temperature condensate pump 11, warm condensed water stop valve 11c is connected with recycling condensing water pipe.Recycling condensing water pipe is connected with recycling condensing water system 15 by the first stop valve 11a, by the second stop valve 11b, is connected with the water inlet of cryogenic heat exchanger 5b, and the delivery port of cryogenic heat exchanger 5b is connected with recycling condensing water system 15.The water inlet of low-temperature pre-heater 5a is connected with the outlet of heat-exchanger pump 13, and the water outlet of low-temperature pre-heater 5a is flowed through after the heat absorbing side of hot water heat exchanger 8.3 and is connected with the water inlet of heat-exchanger pump 13.
The pipe drier condensation-water drain 2b ' of pipe drier 2 also accesses the flash tank condensing water inlet 6a of flash tank, the flash tank condensation-water drain 6c of flash tank bottom is connected with flash tank condensate pump 12, and the outlet of flash tank condensate pump 12 is connected with recycling condensing water pipe by flash tank condensed water stop valve 12a.Open flash tank condensate pump 12 and flash tank condensed water stop valve 12a, the condensed water of flash tank bottom can be sent into recycling condensing water pipe by flash tank condensate pump 12, both can directly enter recycling condensing water system 15, enter again recycling condensing water system 15 after can entering again cryogenic heat exchanger 5b heat release.
The top on used heat absorption tower 8 is provided with used heat absorption tower water inlet 8b and used heat absorption tower air outlet 8a ', and the bottom on used heat absorption tower is provided with used heat absorption tower delivery port 8b ' and used heat absorption tower air inlet 8a.The outlet of exhaust blower 7 is connected with used heat absorption tower air inlet 8a, used heat absorption tower air outlet 8a ' is to airborne release, used heat absorption tower delivery port 8b ' is provided with circulating pump 8.2, and the flow through heat release rear flank of hot water heat exchanger 8.3 of the water outlet of circulating pump 8.2 is connected with used heat absorption tower water inlet 8b.
The cyclone separator air inlet 9a of cyclone separator 9 is connected with rower drier air outlet 4b ', cyclone separator air outlet 9b is discharged into atmosphere by exhaust fan 10, and cyclone separator discharging opening 9c is connected with the feed back entrance 3d of screening conveying equipment 3 by feed back pipe.
Dry run in turn includes the following steps: fresh fermented feed enters feeder from the material loading owner charging aperture 1a of lower end, from the preliminary fermented feed of drying of process of screening conveying equipment, from the auxiliary charging aperture 1b of feeder, enter feeder, the auxiliary charging aperture 1b of feeder is above material loading owner charging aperture 1a, feeder can be conveying worm, at feeder, promote in course of conveying that fermented feed is mixed and stirred and evenly, then from the feeder discharging opening 1c of feeder upper end, discharge, enter the tube type drying machine inlet capable 2a of pipe drier, in pipe drier, fermented feed along continuous straight runs advances after by forward direction, when advancing and steam carry out indirect heat exchange, Hot wet air heating after heat exchange is extracted out by exhaust blower 7 from the exhaust outlet of pipe drier.
The fermented feed of preliminarily dried is discharged from pipe drier discharging opening 2a ', enter again 3 screenings of screening conveying equipment, after screening, screenings is admitted to the tower drying machine inlet capable 4a at rower drier top, and oversize is admitted to the auxiliary charging aperture 1b of feeder to be mixed with fresh fermented feed.
In rower drier 4, fermented feed moves to the rower drier discharging opening 4a ' discharge of bottom from the top down, air enters the rower drier air inlet 4b of rower drier 4 bottoms after air heater 5 heating, and hot blast flows from bottom to top fermented feed is carried out from the rower drier air outlet 4b ' on rower drier top, discharging after redrying.
In air heater, air flow through successively low-temperature pre-heater, cryogenic heat exchanger, mid temperature heat exchanger and high-temperature heat-exchanging, be constantly heated raising temperature.Hot blast after heating enters the rower drier air inlet 4b of rower drier.High-temperature steam enters to discharge in high-temperature heat-exchanging to be become high-temperature condensation water after latent heat and discharges, high-temperature condensation water enters flash tank flash distillation becomes flash-off steam, flash-off steam enters after mid temperature heat exchanger continues to discharge latent heat becomes middle temperature condensed water discharge, middle temperature condensed water by warm condensate pump through in warm condensed water stop valve 11c send into recycling condensing water pipe, open the first stop valve 11a, close the second stop valve 11b, middle temperature condensed water can directly enter recycling condensing water system.Also can close the first stop valve 11a, open the second stop valve 11b, middle temperature condensed water becomes cryogenic condensation water after can entering and discharging sensible heat in cryogenic heat exchanger, then flows into recycling condensing water system.Hot water carries out indirect preheating to air in low-temperature pre-heater, and the water outlet of low-temperature pre-heater is flowed through after the heat absorbing side of hot water heat exchanger 8.3 and sent into by heat-exchanger pump 13 water inlet that flows back to low-temperature pre-heater.
The Hot wet air heating of discharging from pipe drier is sent into used heat absorption tower air inlet 8a by exhaust blower, in used heat absorption tower, recirculated water is carried out after heat release from the used heat absorption tower air outlet 8a ' at top, used heat absorption tower to airborne release, used heat absorption tower water inlet 8b is flowed back in the heat release rear flank that the recirculated water flowing out from used heat absorption tower delivery port 8b ' is sent into hot water heat exchanger 8.3 by circulating pump 8.2.In hot water heat exchanger 8.3, the recirculated water of heat release side carries out indirect to the hot water of heat absorbing side.
The tail gas of discharging from rower drier air outlet 4b ' enters cyclone separator air inlet 9a, in cyclone separator, carry out after centrifugation, from cyclone separator air outlet 9b, discharge, through exhaust fan, be discharged into atmosphere again, the fermented feed of separating flows back to screening conveying equipment 3 by feed back pipe from cyclone separator discharging opening 9c.
The technological parameter embodiment at each position is as follows:
Embodiment mono-
Enter the oversize of the auxiliary charging aperture 1b of feeder and the mass ratio of fresh fermented feed is 1:8, the fermented feed moisture content of pipe drier discharging opening 2a ' is 20%, and the fermented feed moisture content of rower drier discharging opening 4a ' is 8%.
The vapor (steam) temperature that enters pipe drier steam inlet 2b is 135 ℃, and the condensate temperature of pipe drier condensation-water drain 2b ' is 110 ℃, and the fermented feed outlet temperature of pipe drier discharging opening 2a ' is 45 ℃; The hot blast inlet temperature of rower drier air inlet 4b is 80 ℃, and the temperature of outgoing air of rower drier air outlet 4b ' is 50 ℃, and the fermented feed outlet temperature of rower drier discharging opening 4a ' is 60 ℃.
The temperature of outgoing air of pipe drier 2 is 75 ℃, and the temperature of outgoing air of used heat absorption tower air outlet 8a ' is 55 ℃, and the inflow temperature of low-temperature pre-heater 5a is 65 ℃, and the leaving water temperature of low-temperature pre-heater 5a is 50 ℃.
Embodiment bis-
Enter the oversize of the auxiliary charging aperture 1b of feeder and the mass ratio of fresh fermented feed is 1:4, the fermented feed moisture content of pipe drier discharging opening 2a ' is 22%, and the fermented feed moisture content of rower drier discharging opening 4a ' is 10%.
The vapor (steam) temperature that enters pipe drier steam inlet 2b is 138 ℃, and the condensate temperature of pipe drier condensation-water drain 2b ' is 112 ℃, and the fermented feed outlet temperature of pipe drier discharging opening 2a ' is 50 ℃; The hot blast inlet temperature of rower drier air inlet 4b is 85 ℃, and the temperature of outgoing air of rower drier air outlet 4b ' is 52 ℃, and the fermented feed outlet temperature of rower drier discharging opening 4a ' is 65 ℃.
The temperature of outgoing air of pipe drier 2 is 78 ℃, and the temperature of outgoing air of used heat absorption tower air outlet 8a ' is 57 ℃, and the inflow temperature of low-temperature pre-heater 5a is 68 ℃, and the leaving water temperature of low-temperature pre-heater 5a is 52 ℃.
Embodiment tri-
Enter the oversize of the auxiliary charging aperture 1b of feeder and the mass ratio of fresh fermented feed is 3:8, the fermented feed moisture content of pipe drier discharging opening 2a ' is 25%, and the fermented feed moisture content of rower drier discharging opening 4a ' is 12%.
The vapor (steam) temperature that enters pipe drier steam inlet 2b is 140 ℃, and the condensate temperature of pipe drier condensation-water drain 2b ' is 115 ℃, and the fermented feed outlet temperature of pipe drier discharging opening 2a ' is 55 ℃; The hot blast inlet temperature of rower drier air inlet 4b is 90 ℃, and the temperature of outgoing air of rower drier air outlet 4b ' is 55 ℃, and the fermented feed outlet temperature of rower drier discharging opening 4a ' is 70 ℃.
The temperature of outgoing air of pipe drier 2 is 80 ℃, and the temperature of outgoing air of used heat absorption tower air outlet 8a ' is 60 ℃, and the inflow temperature of low-temperature pre-heater 5a is 70 ℃, and the leaving water temperature of low-temperature pre-heater 5a is 55 ℃.
The foregoing is only the present invention's better possible embodiments, non-so limit to scope of patent protection of the present invention.In addition to the implementation, the present invention can also have other embodiments, according to the difference of fermented feed kind, can select whether come into operation low-temperature heater or low-temperature pre-heater, also the hot water of low-temperature pre-heater directly can be introduced to used heat absorption tower and carry out heat exchange, for abortion amount fermented feed factory, in view of investment, consider, also can not reclaim used heat of tube bundle drying machine tail gas etc.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop in the protection domain of requirement of the present invention.The present invention can pass through or adopt existing techniques in realizing without the technical characterictic of describing, and does not repeat them here.
Claims (9)
1. a fermented feed drying means, it is characterized in that, in turn include the following steps: fresh fermented feed enters from the main charging aperture of feeder lower end, material outlet from feeder upper end after promoting is discharged, then fermented feed enters the charging aperture of pipe drier, in pipe drier, fermented feed along continuous straight runs advances after by forward direction, when advancing and steam carry out indirect heat exchange, Hot wet air heating after heat exchange is extracted out by exhaust blower from the exhaust outlet of pipe drier, the fermented feed of preliminarily dried is discharged from the discharging opening of pipe drier, enter again the screening of screening conveying equipment, after screening, screenings is admitted to the charging aperture at rower drier top, the auxiliary charging aperture that oversize is admitted to described feeder mixes with fresh fermented feed, described auxiliary charging aperture is positioned at described main charging aperture top, in rower drier, fermented feed moves to the discharging opening discharge of bottom from the top down, air enters the air inlet of rower drier bottom after air heater heating, and hot blast flows from bottom to top fermented feed is carried out from the air outlet on rower drier top, discharging after redrying.
2. fermented feed drying means according to claim 1, it is characterized in that: described air heater is included in mid temperature heat exchanger and the high-temperature heat-exchanging being connected in series successively in air direction of advance, air is entered the air inlet of described rower drier successively after mid temperature heat exchanger and high-temperature heat-exchanging heating; High-temperature steam enters to discharge in described high-temperature heat-exchanging to be become high-temperature condensation water after latent heat and discharges, high-temperature condensation water enters flash tank flash distillation becomes flash-off steam, flash-off steam enters after mid temperature heat exchanger continues to discharge latent heat becomes middle temperature condensed water discharge, middle temperature condensed water by warm condensate pump through in warm condensed water stop valve send into recycling condensing water pipe, described recycling condensing water pipe is connected with recycling condensing water system by the first stop valve.
3. fermented feed drying means according to claim 2, it is characterized in that: the Hot wet air heating of discharging from described pipe drier is sent into the air inlet on used heat absorption tower by described exhaust blower, in used heat absorption tower, recirculated water is carried out after heat release from the air outlet at top, used heat absorption tower to airborne release, the water inlet on used heat absorption tower is flowed back in the heat release rear flank that the recirculated water flowing out from the delivery port on used heat absorption tower is sent into hot water heat exchanger by circulating pump; Hot water carries out indirect preheating to air in low-temperature pre-heater, air after preheating enters mid temperature heat exchanger to be continued to be heated, the water outlet of low-temperature pre-heater is flowed through and by heat-exchanger pump, is sent back to the water inlet of low-temperature pre-heater after the heat absorbing side of described hot water heat exchanger, in hot water heat exchanger, the recirculated water on used heat absorption tower carries out indirect heat release to the hot water of low-temperature pre-heater.
4. fermented feed drying means according to claim 3, it is characterized in that: described air heater also comprises the cryogenic heat exchanger being serially connected with between described low-temperature pre-heater and described mid temperature heat exchanger, described recycling condensing water pipe is connected with the water inlet of described cryogenic heat exchanger by the second stop valve, middle temperature condensed water becomes cryogenic condensation water discharge sensible heat in cryogenic heat exchanger after, then flows into described recycling condensing water system.
5. fermented feed drying means according to claim 2, is characterized in that: the condensation-water drain of described pipe drier also accesses the condensing water inlet of described flash tank; The bottom of described flash tank is connected with flash tank condensate pump, and described flash tank condensed water delivery side of pump is connected with described recycling condensing water pipe by flash tank condensed water stop valve.
6. fermented feed drying means according to claim 1, it is characterized in that: the tail gas of discharging from described rower drier top air outlet enters cyclone separator to carry out centrifugation, from the air outlet of described cyclone separator, through exhaust fan, be discharged into atmosphere, the fermented feed of separating flows back to described screening conveying equipment by feed back pipe from the discharge gate of described cyclone separator.
7. fermented feed drying means according to claim 1, it is characterized in that: enter the oversize of the auxiliary charging aperture of described feeder and the mass ratio of fresh fermented feed for (1-3): 8, the fermented feed moisture content of described pipe drier discharging opening is 20%-25%, and the fermented feed moisture content of described rower drier discharging opening is 8%-12%.
8. fermented feed drying means according to claim 1, it is characterized in that: the steam inlet temperature of described pipe drier is 135 ℃-140 ℃, the temperature of described pipe drier condensation-water drain is 110 ℃-115 ℃, and the fermented feed outlet temperature of described pipe drier is 45 ℃-55 ℃; The hot blast inlet temperature of described rower drier is 80 ℃-90 ℃, and the temperature of outgoing air of described rower drier is 50 ℃-55 ℃, and the fermented feed outlet temperature of described rower drier is 60 ℃-70 ℃.
9. fermented feed drying means according to claim 3, it is characterized in that: the temperature of outgoing air of described pipe drier is 75 ℃-80 ℃, the temperature of outgoing air on described used heat absorption tower is 55 ℃-60 ℃, the inflow temperature of described low-temperature pre-heater is 65 ℃-70 ℃, and the leaving water temperature of described low-temperature pre-heater is 50 ℃-55 ℃.
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Address after: 225127 Ji'an Road, Hanjiang Industrial Park, Jiangsu, China, No. 198, No. Applicant after: Mayande Group Co., Ltd. Address before: 225127 Ji'an Road, Hanjiang Industrial Park, Jiangsu, China, No. 198, No. Applicant before: Jiangsu Myande Food Machinery Co., Ltd. |
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