CN1016538B - Energy saving two-stage drying technology process - Google Patents
Energy saving two-stage drying technology processInfo
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- CN1016538B CN1016538B CN 89101945 CN89101945A CN1016538B CN 1016538 B CN1016538 B CN 1016538B CN 89101945 CN89101945 CN 89101945 CN 89101945 A CN89101945 A CN 89101945A CN 1016538 B CN1016538 B CN 1016538B
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- drying
- hot blast
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Abstract
The present invention is energy-conservation two-stage drying technology process, the high-temperature tail gas that second level falling-rate periods of drying is discharged is all recycled, replenish the thermal source of part hot blast as first order constant rate of drying, its magnitude of recruitment is regulated with control valve, the dry moisture content of finished products of discharging in the control second level meets the requirements, general dry combustion gas temperature is low, high humidity, and it is many just to save heat energy.1.45 tons of 1 ton of moisture consumption steam are removed in the baking of working continuously as material, can save 30% for 2.1 tons than external average level.The present invention is applied to be divided into dry run the drier of one, 2 two dryer section, and the second level dried tail gas person more than 10 ℃ of heating up.
Description
The invention belongs to two-stage drying technology process
The present invention is than " drying equipment design " (Science and Technology of Shanghai publishing house)
[1]13 pages and " food collected translation "
[2]The 4th phase, 102 pages-105 pages heat exchanger recovery waste gas residual heats that utilize of going up introduction developed to some extent.
" drying equipment design " introduced: under the not too high situation of inlet temperature, the ratio that exhaust heat accounts for total amount of heat is very big to pneumatic conveyer dryer, and what have accounts for 40%.Adopt heat exchanger to reclaim the existing industrial implementation of heat that waste gas is taken away.For example, 10% air heat to 84.8 ℃, waste gas can drop to 70 ℃ from 150 ℃ by waste heat recovery heat exchanger, reclaims 25% of heat in the waste gas, and fuel savings 23% is recoverable to the used investment of waste heat recovery heat exchanger in two years." food collected translation " the 4th phase is introduced the conclusion of test of many times: when EGT is not less than 80 ℃ again; With the waste gas residual heat of heat exchanger recovery drier, be rational economically.Because it can be preheating to 55-65 ℃ to fresh air from 25 ℃, at this moment can save 20% heat.But waste gas is supplied with before the heat exchanger, needs to purify through particular filter; Heat exchanger need be adorned the cleaning equipment of automatic operation.The total cost of equipment heat exchanger can all reclaim within 2-2.5.The 3rd, Deutsche Bundespatent DT2611353A1 recycles a part of high-temperature tail gas and enters predrying parts through heat-exchange surface heating wet feed, about 50 ℃ of temperature, discharge outdoor through discharge pipe 25, wet feed is gone into prebake cylinder 3 through conveying device, through heat-exchange surface heating carrying out prebake, carries the wet feed of carrying with conveyer 4 to be mixed into through conveyer 28 then and carries out drying in the drying roller 8, be characterized in entering extruder 26 after the prebake, will extrude juice and advance prebake cylinder 3 by return pipe 27.
Purpose of the present invention: the invention reside in and overcome the traditional drying process and emit the EGT height, and the many shortcomings of waste heat energy adopt energy saving two-stage drying technology process, reduce EGT, increase waste gas humidity, save thermal energy consumption.Recycle whole tail gas and replenish a part of hot blast and become and mix hot blast and be used for the one-level drying, the free moisture of whole wet feeds is removed in baking, without the heat exchanger heat exchange, saves the heat exchange loss, enlarges and utilizes the waste heat scope and improve the thermal efficiency.
Technology contents of the present invention: dry run is divided into the first and second two sections, is second level dryer section that the high-temperature tail gas that deceleration drying section is discharged is all recycled, replenish a part of hot blast and become the mixing hot blast, as the one-level dryer section is the thermal source of constant speed drying section, its supplemental heat air quantity distributes control valve to regulate with hot blast, the hot blast rate of control second level dryer section, finished product is reached under the condition of requirement water content, the temperature of mixing hot blast that becomes the one-level drying source behind the tail gas that reclaims second level dryer section and the additional hot blast, anhydrate under the precondition of branch 1/2-1/3 satisfying one-level dryer section baking, be reduced to 43 ℃ as far as possible, make one-level dry-heat air temperature a little more than dew-point temperature, the approaching sticking wall of material, but do not stop up mass transport, the combustion gas humidity dewfall that reaches capacity is the limit, to reach maximum purpose of energy saving.Feeder adds wet feed to first order dryer feed mouth, and first order drier discharge gate is arranged half-dried material, and conveyer send half-dried material to enter second level drier, and second level drier discharge gate goes out finished product.
Description of drawings: accompanying drawing 1 is taken out bulging drying technology process, accompanying drawing 2 forced air drying technological processes, accompanying drawing 3 exhausting drying technology process, accompanying drawing 4 parallel pipelines divide and locate, accompanying drawing 5 parallel pipeline meets, accompanying drawing 6 positive negative pressure two-stage airflow dryers: 1 air cleaner, 2 heaters, 3 blower fans, 4 one-level driers, 5 secondary drying devices, 6 auxiliary heat airducts, 7 control valves, 8 control valves, 9 feeders, 10 conveyers, 11 removal devices, 12 half-dried material cyclones, 13 finished product cyclones, 14 dedusters, the total control valve of 15 crotches, the total control valve of 16 meets.The new air of → air-flow symbol: a stream, b master's hot blast stream, c auxiliary heat are distinguished and admirable, d, secondary drying tail gas, e blower fan discharge air-flow, the dry waste gas of f, g total airflow, the h heat of mixing are distinguished and admirable.→ material flow symbol, l wet feed, the half-dried material of m, n finished product.
The theoretical foundation of this technological process: dry run is divided into two sections of constant rate of drying and falling-rate periods of drying, and the terminal point of constant rate of drying is critical point, and therewith corresponding, the former is the one-level drying, and the latter is secondary drying. Constant speed drying section, material surface are all the time wetting by moisture institute, and the unbound water in the material inner macropores is easy to the surface move, and enough replenish the moisture that the surface vaporization is lost. Therefore, no matter to which kind of material, all show as the characteristic of vaporizing on the common water surface, namely the vapour pressure on material surface equals synthermal water saturation vapour pressure, and the material surface remains the wet-bulb temperature (40 ℃) of air substantially. The one-level constant rate of drying needs high-speed Wind Volume fast from the material surface vaporization moisture like this Speed is removed. It is secondary drying that constant rate of drying changes deceleration drying section over to latter stage. Deceleration drying section, the moisture that moves to the surface from material inside have been not enough to replenish the moisture that the surface vaporization is lost. The rate of drying of deceleration drying section depends on material properties, belongs to be subjected to the material internal moisture to move the control stage. Therefore, improve hot blast temperature moisture is moved the prior effect that plays. Because the heat that air is passed to material is greater than the required heat of moisture vaporization, so material surface temperature progressively rises and moves closer to the temperature of air[3] Exhaust temperature rises to 60 ℃ to 90 ℃, its relative temperature 20-40%. Add hot blast and bring up to 100 ℃ to 110 ℃, as the one-level drying source, heat release cools to about 43 ℃ outside the discharge machine.
Implement of the present inventionly when exhaust temperature is big with constant rate of drying exhaust temperature phase difference when must condition to be that single-stage is dry finish, the recycling waste gas residual heat just has big economic benefit. Only contain more unbound water at the material that is dried, and require the finished product baking to go part in conjunction with water, thereby baking goes need to use high-temperature hot-air in conjunction with water, exhaust temperature is just high, and unbound water is removed in baking, can use the low temperature hot blast, and the benefit of recycling like this waste heat is just big. Single-stage airflow drying exhaust temperature is higher than 55-65 ℃, and utilizes the exhaust temperature of the two-stage oven dry of waste heat to drop to 43 ℃, can save heat energy 20-30%. If single-stage dried tail gas temperature is higher than 80 ℃, even reach 150 ℃, the effect of then saving heat energy is just more remarkable.
Implementing economic benefit of the present invention can represent with evaporability.
The main cause that positive negative pressure is saved heat energy in conjunction with the two-stage airflow dryer is the tail gas high humidity of discharging, and temperature is low, and it is few to take away used heat.Complicated heat and mass transport process such as is reduced at the theoretical drying that contains analyzes comparison.Therefore, suppose that the hot-air liberated heat all is used for water evaporates in drier, promptly complete sensible heat is used for water evaporates.So, hot-air contain sensible heat in the value use up with tail gas in the water-vapo(u)r saturation degree be two conditions of this dry run of constraint.Therefore, maximum water capacity in the cards when calculating sensible heat and use up with analytic approach is calculated tail gas relative humidity with it again, judges the possibility that this dry run realizes by relative humidity.Analysis is discussed below:
(1) hot-air heat content (It
△ 1) computing formula:
It
△1＝1.004×t
1+（2500+1.842×t
1）d
o/1000
（40）（1）
In the formula: I
T1-t
1The time air heat content, kJ (kilojoule)/kilogram dry gas;
t
1-hot blast temperature, ℃;
d
o-air moisture content, gram/kilogram dry gas.
(2) formula (1) transplant formula (2), be used for the tail gas water capacity of theory of computation drying when sensible heat is used up, its formula:
d
2l2＝（I
t1-1.004t
2）1000/（2500+1.842t
2） （2）
D in the formula
212-exhaust temperature reaches t
2The time total water capacity, gram/kilogram dry gas;
I
T1-hot-air t
1The time heat content, kJ (kilojoule)/kilogram dry gas;
t
2-exhaust temperature, ℃.
(2) the total water capacity (d of tail gas
212) deduct the former water capacity (d of air
o) promptly get flat evaporator ability (△ d
212) △ d
212=d
212-d
o(3)
If d
o=10 gram/kilogram dry gas add hot-air to 130,140 ℃, calculate heat content (I
T1), again t
2Substitution (2) gets tail gas moisture content (d
2), deduct d
oGet evaporability (△ d), calculate 43 ℃ of tail gas again and improve evaporability than all the other humidity tail gas, numerical value is listed table 1 in:
Table 1
Hot-air heat content I kJ (kilojoule)/kilogram dry gas t
1=130 ℃ of I
130=157.91
Exhaust temperature t
2℃ 43 55 60 70
Tail gas water capacity d
212Gram/kilogram dry gas 44.49 39.48 37.41 33.33
Evaporability △ d
2Gram/kilogram dry gas 34.49 29.48 27.41 23.33
43 ℃ of tail gas improve % 0 17.0 25.8 47.8
Show: it is 15.1-47.8% that positive negative pressure two-stage steam flow oven dry improves evaporability.
Check: by document
[5]I-d numerical value is looked into and is calculated, and 43 ℃ of saturated water capacities are 59.9 gram/kilogram dry gas, and its maximum relative humidity 48.45/59.9=80.9% is so may realize drying.
Continuous table 1
Hot-air heat content I kJ (kilojoule)/kilogram dry gas t
1=140 ℃ of I
140=168.14
Exhaust temperature t
2℃ 43 55 60 70
Tail gas water capacity d
212Gram/kilogram dry gas 48.45 43.41 41.33 37.22
Evaporability △ d
2Gram/kilogram dry gas 38.45 33.41 31.33 27.22
43 ℃ of tail gas improve % 0 15.1 22.7 41.3
Embodiment 1: with the two-stage drying machine such as the accompanying drawing 1 that the air blast combination utilizes waste heat of taking out of technical flow design of the present invention.New air stream a enters heater 2 heating through air cleaner 1, be divided into blast pipe and auxiliary heat airduct 6 that two tributary b in parallel and c enter the secondary drying device 5 of two parallel connections respectively, air-flow b is the thermal source of secondary drying, it is dry to carry out the second time with its double siccative m, its tail gas d is discharged by the blast pipe of secondary drying device 5, it and auxiliary hot blast tributary c are combined into the distinguished and admirable h of the heat of mixing at the blast pipe and auxiliary heat airduct 6 joints of secondary drying device 5, the assignment of traffic ratio of two parallel pipelines is regulated by control valve 7 and 8, air-flow h sucks blower fan 3, discharge air-flow e, blast one-level drier 4, be used for the dry wet feed 1 that adds by feeder 9 to half-dried material m, combustion gas f, half-dried material m send into secondary drying device 5 through conveyer 10 and carry out the drying second time, emit finished product n through discharger 11.
Embodiment 2: the two-stage drying machine such as the accompanying drawing 2 that utilize waste heat with the blowing-type of technical flow design of the present invention.New air a reenters heater 2 heating after air cleaner 1 is gone into blower fan 3 pressurizations, be divided into blast pipe and auxiliary heat airduct 6 that two tributary b in parallel and c enter the secondary drying device 5 of two parallel connections respectively, air-flow b is the thermal source of secondary drying, it is dry to carry out the second time with its double siccative m, its tail gas d is discharged by the blast pipe of secondary drying device 5, it and auxiliary hot blast tributary c are combined into the distinguished and admirable h of the heat of mixing at the blast pipe and the auxiliary heat airduct joint of secondary drying device 5, the wet feed l that blasts 9 addings of 4 pairs of feeders of one-level drier carries out being dried to the first time partial desiccation m, the assignment of traffic ratio of two parallel pipelines is regulated with control valve 7 and 8, and the waste gas f of one-level drier 4 is by the blast pipe emptying.Wet feed 1 adds one-level drier 4 by feeder 9, and the half-dried material m of discharge sends into secondary drying device 5 by conveyer 10, carries out the drying second time, and finished product n is discharged by removal device 11.
Embodiment 3: the two-stage drying machine such as the accompanying drawing 3 that utilize waste heat with the exhausting formula of technical flow design of the present invention.New air a enters heater 2 heating through air cleaner 1, be divided into two tributary b in parallel and c, air-flow b is the thermal source of secondary drying, it is dry to carry out the second time with its double siccative m, its tail gas d is discharged by the blast pipe of secondary drying device 5, it and auxiliary hot blast tributary c are combined into the distinguished and admirable h of the heat of mixing at auxiliary heat airduct 6 and secondary drying device 5 blast pipe joints, the wet feed 1 of going into 9 addings of 4 pairs of feeders of one-level drier carries out the drying first time, the assignment of traffic ratio of two parallel pipelines is regulated with control valve 7 and 8, primary drying is discharged tail gas g, suck blower fan 3, blast pipe combustion gas f, wet feed 1 adds one-level drier 4 by feeder 9, the half-dried material m that discharges, send into secondary drying device 5 by conveyer 10, carry out the drying second time, finished product n is discharged by removal device 11.
Embodiment 4: the two-stage pneumatic drier accompanying drawing 6 that utilizes waste heat with the system blowing-type of technical flow design of the present invention.New air a enters heater 2 heating through air cleaner 1, be divided into two tributary b in parallel and c, the half-dried material m that main hot blast tributary b sends into conveyer 10 carries out sending into after the drying second time finished product cyclone separator 13, finished product is discharged through removal device 11, tail gas stream d with carry secretly fly powder through control valve 7 be combined into the distinguished and admirable h of the heat of mixing through the additional hot blast tributary c of control valve 8, go into blower fan 3 behind the wet feed 1 that feeder 9 adds, blast one-level drier 4, carry out the drying first time, isolated half-dried material m goes into secondary drying device 5 through conveyer 10 by half-dried material cyclone, and overflow waste gas f is through wet dust catcher 4 emptyings
[6]
Range of application: as long as dry run and arid region are divided into the first and second two dryer section, just can realize utilizing the two-stage drying of waste gas residual heat, this two-stage drying technology process is applicable to a formula (fluid bed and ebullated bed), tunnel type, conveyor type, chain-plate type, have that mobile flatcar is box, cell-type and tower.
Technical economic benefit:
If dry run is divided into two dryer section of the first order and the second level, the net of keeping watch is transformed into first order drier air channel, drier air channel, the second level and auxiliary heat airduct, and secondary drying device air channel is in parallel with the auxiliary heat airduct, adorns control valve etc. in the parallel pipeline.The two-stage drying artistic skill reduces EGT, improves humidity, and improving the hot-air evaporation can 15.1-47.8%.
The techno-economic effect example:
Positive negative pressure shows in conjunction with the mill trial results of two-stage airflow dryer: dried starch per ton consumes quantity of steam (vapour pressure is 0.6 MPa): working continuously is 0.767 ton, 0.88 ton of order of classes or grades at school average out to; Evaporate 1 ton of water consumption quantity of steam; Working continuously is 1.45 tons, 1.66 tons of order of classes or grades at school average out to.1.45 tons of consumption vapour indexs and 1.66 tons are with 2.3 tons of domestic average levels
[7]Compare with external average level 2.1 tons [notes], save steam 28-37% and 21-31% respectively.Recyclable equipment investment in 1 year.
Annotate: the West Germany expert says when China Academy of Agriculture Mechanization's exchange of technology: a ton water consumption 2.0-2.2 ton steam is removed in international average level baking.
List of references
1, " drying equipment design " compiled by Chemical Equipment Design pandect editorial board, and the Shanghai science and technology is published 1986.
2, Li Chunqi translates " drier waste gas heat utilization ".Be stated from " food collected translation " 1986 the 4th phase 102-105 pages or leaves.
3, Guo Yihu, Wang Xien work " spray-drying ", Chemical Industry Press, nineteen eighty-three.
4, Gao Kuiyuan translates " food drying principle technical foundation ", light industry publishing house,, 141 pages in 1986.
5, " grain drying " write group and compiled " grain drying ", China Financial ﹠ Economic Publishing, 1987.
6, Yu Jiyun " starch " powder " airflow dryer utility model patent ", the patent No. 19719.
7, Lou Xinjian work " also talking the design of starch pneumatic conveyer dryer " is stated from " starch and starch sugar " the 2nd phase in 1986.
Claims (4)
1, a kind of energy-conservation two-stage drying technology process, dry run is divided into the first and second two sections, second dryer section is that the high-temperature tail gas d that deceleration drying section 5 is discharged recycles, it is characterized in that all reclaiming the tail gas d that secondary drying section 5 is discharged, replenishing a part of hot blast c is the mixing hot blast h of the thermal source of constant speed drying section 4 as first order dryer section, supplemental heat air quantity c is with distributing control valve 7,8 regulate, the hot blast b of control second level dryer section 5, finished product n is reached under the condition of requirement water content, the temperature of mixing hot blast h that becomes the one-level drying source behind the tail gas d of the second level dryer section 5 that reclaims and the additional hot blast c, go under the prerequisite of 1/3-1/2 moisture satisfying first order dryer section 4 baking, be reduced to 43 ℃, make the one-level dry-heat air be higher than dew-point temperature, material l is approaching sticking wall in one-level drying 4, but do not stop up mass transport, with the combustion gas f humidity dewfall that reaches capacity is the limit, wet stock l is dried to half-dried material m by feeder 9 feeding first order driers 4, carry out drying second time through half-dried material conveyer 10 feeding second level driers 5, finished product n reaches after the requirement water content outside the discharge machine.
2, by the described energy-conservation two-stage drying technology process of claim 1, it is characterized in that: take out air blast in conjunction with the two-stage drying technology that utilizes waste heat, after air a process filter 1 and heater 2 heating, be divided into two gangs of hot blast b and c, hot blast b is inhaled into secondary drying device 5, its tail gas d with suck the adjustable auxiliary hot blast c of air quantity through auxiliary heat airduct 6 and merge into and mixes hot blast h, suction blower fan 3, discharge air-flow e, blast one-level drier 4 dryings.
3, by the described energy-conservation two-stage drying technology process of claim 1, it is characterized in that: blowing-type is utilized the two-stage drying technology of waste heat, and air a is inhaled into blower fan 3 through filter 1, bloats after gas flows into heater 2 heating, is divided into two gangs of hot blast b and c and is used for drying.
4, by the described energy-conservation two-stage drying technology process of claim 1, it is characterized in that: the exhausting formula is utilized the two-stage drying technology of waste heat, after air a process filter 1 and heater 2 heating, be divided into two gangs of hot blast b and c and be used for drying, the air-flow g that first order drier 4 flows out is inhaled into blower fan 3, blast pipe combustion gas f.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89101945 CN1016538B (en) | 1989-04-06 | 1989-04-06 | Energy saving two-stage drying technology process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89101945 CN1016538B (en) | 1989-04-06 | 1989-04-06 | Energy saving two-stage drying technology process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1036260A CN1036260A (en) | 1989-10-11 |
| CN1016538B true CN1016538B (en) | 1992-05-06 |
Family
ID=4854481
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 89101945 Expired CN1016538B (en) | 1989-04-06 | 1989-04-06 | Energy saving two-stage drying technology process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1016538B (en) |
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-
1989
- 1989-04-06 CN CN 89101945 patent/CN1016538B/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101881550A (en) * | 2010-06-30 | 2010-11-10 | 国家粮食局科学研究院 | Low-temperature high-efficiency fluidization combined drying process and equipment thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1036260A (en) | 1989-10-11 |
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