CN201854649U - System for producing lysine sulphate - Google Patents
System for producing lysine sulphate Download PDFInfo
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- CN201854649U CN201854649U CN2010205596846U CN201020559684U CN201854649U CN 201854649 U CN201854649 U CN 201854649U CN 2010205596846 U CN2010205596846 U CN 2010205596846U CN 201020559684 U CN201020559684 U CN 201020559684U CN 201854649 U CN201854649 U CN 201854649U
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- heater
- gas
- supply device
- gas supply
- odor eliminator
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Abstract
The utility model discloses a system for producing lysine sulphate, wherein the system comprises a granulator (11), a first heater (12), a first gas supply device (17), a dryer (21), a second heater (22) and a second gas supply device (27). A first air inlet (14) and a first exhaust port (15) are arranged on the granulator, a gas inlet of the first heater is connected with the first gas supply device, and a gas outlet of the first heater is connected with the first air inlet. A second air inlet (24) and a second exhaust port (25) are arranged on the dryer, a gas inlet of the second heater is connected with the second gas supply device, and a gas outlet of the second heater is connected with the second air inlet. The system also comprises a third heater (3), a gas inlet of the third heater is connected with the second exhaust port, and a gas outlet of the third heater is connected with the first air inlet. The system can cyclically utilize tail gas, reduces the consumption of heat energy and improves the utilization rate of heat energy.
Description
Technical field
The utility model relates to lysine sulfate production field, particularly, relates to a kind of system that is used to produce lysine sulfate.
Background technology
Feed grade L-lysine sulfate is a kind of lysine of environment-friendly type.Aborning by adjusting the ratio of solid content and lysine in the zymotic fluid concentrate, with the concentrate mist projection granulating, formation comprises effective lysine at the compound lysine sulfate product of interior high protein, this product not only comprises the lysine greater than 51%, and contains other amino acid, vitamin and growth factor greater than 10%.The biological value of 65% lysine sulfate in swine rations is equal to or a little higher than 98.5% FE-5.It has broken through the production technology of traditional FE-5, and aspects such as efficiency of feed utilization, minimizing pollution are remarkably productive reducing production costs, improving.
Operations such as L-lysine sulfate production technology comprises neutralization, allotment, concentrates, granulation, drying, screening and packing.For a long time, as shown in Figure 1, the condensed water that the high-temperature steam of the steam heater of prilling granulator forms in the 65% lysine production technology is delivered directly to the workshop and utilizes once more, the temperature of the condensed water in the steam heater is higher, it has more heat energy, this part heat energy is not well utilized, and causes the waste of heat energy; The tail gas humidity that drying machine in the drying device produces is less relatively, and temperature is higher, reaches 90-100 ℃, and this part tail gas is directly drawn the back emptying by air-introduced machine, causes the waste of heat energy; The tail gas that comminutor in the prilling granulator produces only by behind the bag-type dust, just directly is discharged in the atmosphere, but influenced by the drying of high-temperature hot air, has heavier Jiao in the tail gas and sticks with paste peculiar smell, influences air quality, contaminated environment.
The utility model content
The purpose of this utility model provides a kind of system that is used to produce lysine sulfate, and this system can carry out recycling to tail gas, has reduced consumption of heat energy, has improved the heat energy utilization rate.
To achieve these goals, the utility model provides a kind of system that is used to produce lysine sulfate, and wherein, this system comprises: comminutor, primary heater, first gas supply device, drying machine, secondary heater and second gas supply device; Described comminutor is provided with first air inlet and first exhaust outlet, and the gas access of described primary heater is connected with described first gas supply device, and gas vent is connected with described first air inlet; Described drying machine is provided with second air inlet and second exhaust outlet, and the gas access of described secondary heater is connected with described second gas supply device, and gas vent is connected with described second air inlet; Described system also comprises the 3rd heater, and the gas access of described the 3rd heater is connected with described second exhaust outlet, and gas vent is connected with described first air inlet.
Preferably, this system also comprises the 4th heater, described primary heater and the 4th heater are shell-and-tube heat exchanger, the gas access of described primary heater is connected with described first gas supply device through described the 4th heater, the gas access of described the 4th heater is connected with described first gas supply device, gas vent is connected with the gas access of described primary heater, and the outlet of the heat transferring medium of described primary heater is connected to the heat transferring medium inlet of described the 4th heater.
Preferably, this system also comprises the 5th heater, described secondary heater and the 5th heater are shell-and-tube heat exchanger, the gas access of described secondary heater is connected with described second gas supply device through described the 5th heater, the gas access of described the 5th heater is connected with described second gas supply device, gas vent is connected with the gas access of described secondary heater, and the outlet of the heat transferring medium of described secondary heater is connected to the heat transferring medium inlet of described the 5th heater.
Preferably, this system also comprises first deduster, and described first deduster is connected with described first exhaust outlet.
Preferably, this system also comprises the tail gas odor eliminator, and described tail gas odor eliminator is connected with described first deduster.
Preferably, described tail gas odor eliminator comprises the wet type odor eliminator and the dry type odor eliminator of connecting successively by gas flow direction.
Preferably, described wet type odor eliminator is the buck odor eliminator.
Preferably, described dry type odor eliminator is the plain odor eliminator of plant extract.
Preferably, this system also comprises second deduster, and described second deduster is connected with described second exhaust outlet.
In the production process of lysine sulfate, operations such as production and processing comprises neutralization, allotment, concentrates, granulation, drying, screening and packing.By technique scheme, comminutor carries out granulation to the zymotic fluid concentrate, forms the lysine sulphate particle, then, discharges by the discharging opening of comminutor, and the charging aperture by drying machine enters and carries out drying processing in the drying machine again.
Zymotic fluid carries out mist projection granulating in comminutor; first gas supply device is supplied with primary heater with cold air; and carry out becoming hot-air after the exchange heat with heat transferring medium wherein; and enter comminutor inside by first air inlet on the comminutor; blowing zymotic fluid spraying, to make fluid separation applications be drop; take away the part moisture in the drop simultaneously, make it form graininess lysine sulfate.The tail gas that produces in the granulation process is discharged by first exhaust outlet on the comminutor.
Owing to also contain more water in the graininess lysine sulfate that the comminutor granulation forms; and then it enters and carries out drying in the drying machine and handle; second gas supply device is supplied with secondary heater with cold air; and carry out becoming hot-air after the exchange heat with heat transferring medium wherein; and enter dryer inner by second air inlet on the drying machine; by the heat that has in the hot-air lysine sulphate particle is evaporated and to dewater; flowing of hot-air can also be carried out air-dry to the lysine sulphate particle simultaneously; the excessive moisture that the lysine sulphate particle has is removed, made it become the dried granules product.The tail gas that produces in the dry run is discharged by second exhaust outlet on the drying machine.
Through the tail gas that second exhaust outlet of drying machine is discharged, its humidity is less relatively, and temperature is higher, reaches 90-100 ℃, after heating by the 3rd heater, enters comminutor inside as hot-air by first air inlet.Because tail gas itself has more heat transfer, in heating process, only need less heat just can be heated the design temperature of hot-air.Thereby comminutor reduces by the consumption of the hot-air that the primary heater heat exchange forms, and further the heat transferring medium consumption of primary heater also reduces, and has saved thermal source, has reduced consumption of heat energy.Simultaneously, this system has carried out recycling to tail gas, effectively utilized the heat that has in the tail gas, has avoided the waste of heat energy, has improved the heat energy utilization rate.In addition, this system has reduced the discharge capacity of tail gas, helps environmental protection.
Other features and advantages of the utility model will partly be described in detail in the specific embodiment subsequently.
Description of drawings
Accompanying drawing is to be used to provide further understanding of the present utility model, and constitutes the part of specification, is used from explanation the utility model with the following specific embodiment one, but does not constitute restriction of the present utility model.In the accompanying drawings:
Fig. 1 is the schematic diagram that the system of lysine sulfate is produced in traditional being used to;
Fig. 2 is the schematic diagram of system that is used to produce lysine sulfate according to the specific embodiment of the present invention.
Description of reference numerals
3 the 3rd heaters, 11 comminutors
12 primary heaters, 13 first dedusters
14 first air inlets, 15 first exhaust outlets
16 the 4th heaters, 17 first gas supply devices
18 tail gas odor eliminators, 18 ' wet type odor eliminator
18 " dry type odor eliminator 21 drying machines
22 secondary heaters, 23 second dedusters
24 second air inlets, 25 second exhaust outlets
26 the 5th heaters, 27 second gas supply devices
The specific embodiment
Below in conjunction with accompanying drawing the specific embodiment of the present utility model is elaborated.Should be understood that the specific embodiment described herein only is used for description and interpretation the utility model, is not limited to the utility model.
As shown in Figure 2, the system that is used to produce lysine sulfate according to the specific embodiment of the present utility model, wherein, this system comprises: comminutor 11, primary heater 12, first gas supply device 17, drying machine 21, secondary heater 22 and second gas supply device 27; Comminutor 11 is provided with first air inlet 14 and first exhaust outlet 15, and the gas access of primary heater 12 is connected with first gas supply device 17, and gas vent is connected with first air inlet 14; Drying machine 21 is provided with second air inlet 24 and second exhaust outlet 25, and the gas access of secondary heater 22 is connected with second gas supply device 27, and gas vent is connected with second air inlet 24; Described system comprises that also the gas access of the 3rd heater 3, the three heaters 3 is connected with second exhaust outlet 25, and gas vent is connected with first air inlet 14.
In the production process of lysine sulfate, operation such as production and processing comprises neutralization, is mixed, concentrates, granulation, drying, screening and packing.11 pairs of zymotic fluid concentrates of comminutor carry out granulation, form the lysine sulphate particle, then, discharge by the discharging opening of comminutor 11, and the charging aperture by drying machine 21 enters and carries out drying processing in the drying machine 21 again.
Zymotic fluid carries out mist projection granulating in comminutor 11; first gas supply device 17 is supplied with primary heater 12 with cold air; and carry out becoming hot-air after the exchange heat with heat transferring medium wherein; and enter comminutor 11 inside by first air inlet 14 on the comminutor 11; blowing zymotic fluid spraying, to make fluid separation applications be drop; take away the part moisture in the drop simultaneously, make it form graininess lysine sulfate.The tail gas that produces in the granulation process is discharged by first exhaust outlet 15 on the comminutor 11.
Owing to also contain more water in the graininess lysine sulfate that comminutor 11 granulations form; and then it enters and carries out drying in the drying machine 21 and handle; second gas supply device 27 is supplied with secondary heater 22 with cold air; and carry out becoming hot-air after the exchange heat with heat transferring medium wherein; and enter drying machine 21 inside by second air inlet 24 on the drying machine; by the heat that has in the hot-air lysine sulphate particle is evaporated and to dewater; flowing of hot-air can also be carried out air-dry to the lysine sulphate particle simultaneously; the excessive moisture that the lysine sulphate particle has is removed, made it become the dried granules product.The tail gas that produces in the dry run is discharged by second exhaust outlet 25 on the drying machine 21.
Through the tail gas that second exhaust outlet 25 of drying machine 21 is discharged, its humidity is less relatively, and temperature is higher, reaches 90-100 ℃, after heating by the 3rd heater 3, enters comminutor 11 inside as hot-air by first air inlet 14.Because tail gas itself has more heat transfer, in heating process, only need less heat just can be heated about 90 ℃ of the design temperatures of hot-air, make about 60 ℃ of the temperature raisings in air source of comminutor 11.Thereby comminutor 11 reduces by the consumption of the hot-air that primary heater 12 heat exchange form, and further the heat transferring medium consumption of primary heater 12 also reduces, and has saved thermal source, has reduced consumption of heat energy.Simultaneously, this system has carried out recycling to tail gas, effectively utilized the heat that has in the tail gas, has avoided the waste of heat energy, has improved the heat energy utilization rate, has reduced production cost, has saved the energy.In addition, this system has reduced the discharge capacity of tail gas, helps environmental protection.
Preferably, this system also comprises the 4th heater 16, primary heater 12 and the 4th heater 16 are shell-and-tube heat exchanger, the gas access of primary heater 12 is connected with first gas supply device 17 through the 4th heater 16, the gas access of the 4th heater 16 is connected with first gas supply device 17, gas vent is connected with the gas access of primary heater 12, and the outlet of the heat transferring medium of primary heater 12 is connected to the heat transferring medium inlet of the 4th heater 16.Primary heater 12 and the 4th heater 16 all adopt shell-and-tube heat exchanger, make can not mix between the medium that carries out exchange heat, and whole diabatic process are continuous, stable, and the heat exchange efficiency height heats effective simultaneously.The cold air of first gas supply device, 17 supply primary heaters 12 enters in the primary heater 12 by the gas access of primary heater 12, carry out exchange heat with the heat transferring medium in the primary heater 12, thereby cold air becomes hot-air, heat transferring medium is that the vapours cooling forms about 150 ℃ high-temperature condensation water, heat transferring medium outlet by primary heater 12 is discharged, and the heat transferring medium inlet by the 4th heater 16 enters in the 4th heater 16 and becomes new heat transferring medium.It is that the heat of high-temperature condensation water carries out preheating that the cold air that enters by first gas supply device 17 at first enters the heat transferring medium that utilizes in the 4th heater 16 wherein, make cold air reach certain temperature, obtain certain heat, and then to enter in the primary heater 12 with heat transferring medium be that vapours is carried out exchange heat, reaches the hot air temperature of predetermined system requirements.The setting of the 4th heater 16 makes that the consumption of heat transferring medium reduces in the primary heater 12, has saved system heat sources, has reduced production cost.Simultaneously, the high-temperature condensation water that cooling forms after this internal system heat exchanging medium and cold air heat exchange carries out cycling and reutilization, become new heat transferring medium, made full use of the heat energy that wherein has, reduced system energy consumption, avoid the waste of heat energy, realized the economy and the feature of environmental protection that lysine sulfate is produced.
Preferably, this system also comprises the 5th heater 26, secondary heater 22 and the 5th heater 26 are shell-and-tube heat exchanger, the gas access of secondary heater 22 is connected with second gas supply device 27 through the 5th heater 26, the gas access of the 5th heater 26 is connected with second gas supply device 27, gas vent is connected with the gas access of secondary heater 22, and the outlet of the heat transferring medium of secondary heater 22 is connected to the heat transferring medium inlet of the 5th heater 26.As mentioned above, the structure of the 5th heater 26, purposes and function are similar to the 4th heater 16, therefore, are not repeated at this.
Preferably, this system comprises that also first deduster, 13, the first dedusters 13 are connected with first exhaust outlet 15.The tail gas that produces in comminutor 11 granulation process is discharged by first exhaust outlet 15, enters first deduster 13 and carries out dust removal process.Because comminutor 11 medium powers are bigger, media flow is also bigger, therefore can produce more dust, needs 13 pairs of tail gas of first deduster to handle, and makes that dust content is less in the tail gas, reduces the pollution and the destruction of environment to external world.Thereby, also make things convenient for next step tail gas taste removal to handle.
Preferably, this system also comprises tail gas odor eliminator 18, and tail gas odor eliminator 18 is connected with first deduster 13.Owing to be subjected to the drying influence of high-temperature hot air; the tail gas that comminutor 11 produces has heavier Jiao and sticks with paste peculiar smell; this tail gas enters the processing that eliminates the unusual smell in the tail gas odor eliminator 18 by the air outlet of first deduster 13; remove the burnt burning that wherein has; avoiding tail gas to discharge the back pollutes air; improve the surrounding environment quality, helped environmental protection.
Preferably, tail gas odor eliminator 18 comprises the wet type odor eliminator 18 ' and the dry type odor eliminator 18 of connecting successively by gas flow direction ".By two-stage tail gas odor eliminator, i.e. wet type odor eliminator 18 ' and dry type odor eliminator 18 ", the tail gas that comminutor 11 produces is further handled, it is more thorough to make peculiar smell in the tail gas remove, so the environment protecting of system is better.
Preferably, wet type odor eliminator 18 ' is the buck odor eliminator.The buck odor eliminator is the wet method taste removal, and the tail gas after first deduster 13 is handled can be removed about 80% peculiar smell through the washing of buck, and the taste removal ability of buck odor eliminator is stronger, and effect is preferable, and simple, and cost is lower.
Preferably, the dry type odor eliminator 18 " be the plain odor eliminator of plant extract.The plain odor eliminator of plant extract is the dry method taste removal, also residual in the tail gas of handling through the 18 ' taste removal of wet type odor eliminator have a less peculiar smell, the plain odor eliminator of plant extract carries out further dry method neutralization by the plant extract element to it, thoroughly remove the burnt burning that has in the tail gas, make that the taste removal effect is thorough, reach environmental protection requirement.
Preferably, this system comprises that also second deduster, 23, the second dedusters 23 are connected with second exhaust outlet 25.The tail gas that produces in drying machine 21 dry runs is discharged by second exhaust outlet 25, enters second deduster 23 and carries out dust removal process.Because drying machine 21 medium powers are bigger, media flow is also bigger, and simultaneous temperature is higher, humidity is less, therefore can produce more dust, needs 23 pairs of tail gas of second deduster to handle, make that dust content is less in the tail gas, reduce the pollution and the destruction of environment to external world.Thereby this tail gas can enter in the 3rd heater 3 and carry out heat treated, and is recycling for next step.
Below describe preferred implementation of the present utility model in conjunction with the accompanying drawings in detail; but; the utility model is not limited to the detail in the above-mentioned embodiment; in technical conceive scope of the present utility model; can carry out multiple simple variant to the technical solution of the utility model, these simple variant all belong to protection domain of the present utility model.
Need to prove in addition, each concrete technical characterictic described in the above-mentioned specific embodiment under reconcilable situation, can make up by any suitable manner, for fear of unnecessary repetition, the utility model is to the explanation no longer separately of various possible compound modes.
In addition, also can make up arbitrarily between the various embodiment of the present utility model, as long as it is without prejudice to thought of the present utility model, it should be considered as content disclosed in the utility model equally.
Claims (9)
1. system that is used to produce lysine sulfate, it is characterized in that this system comprises: comminutor (11), primary heater (12), first gas supply device (17), drying machine (21), secondary heater (22) and second gas supply device (27); Described comminutor (11) is provided with first air inlet (14) and first exhaust outlet (15), and the gas access of described primary heater (12) is connected with described first gas supply device (17), and gas vent is connected with described first air inlet (14); Described drying machine (21) is provided with second air inlet (24) and second exhaust outlet (25), and the gas access of described secondary heater (22) is connected with described second gas supply device (27), and gas vent is connected with described second air inlet (24); Described system also comprises the 3rd heater (3), and the gas access of described the 3rd heater (3) is connected with described second exhaust outlet (25), and gas vent is connected with described first air inlet (14).
2. system according to claim 1, it is characterized in that, this system also comprises the 4th heater (16), described primary heater (12) and the 4th heater (16) are shell-and-tube heat exchanger, the gas access of described primary heater (12) is connected with described first gas supply device (17) through described the 4th heater (16), the gas access of described the 4th heater (16) is connected with described first gas supply device (17), gas vent is connected with the gas access of described primary heater (12), and the outlet of the heat transferring medium of described primary heater (12) is connected to the heat transferring medium inlet of described the 4th heater (16).
3. system according to claim 1, it is characterized in that, this system also comprises the 5th heater (26), described secondary heater (22) and the 5th heater (26) are shell-and-tube heat exchanger, the gas access of described secondary heater (22) is connected with described second gas supply device (27) through described the 5th heater (26), the gas access of described the 5th heater (26) is connected with described second gas supply device (27), gas vent is connected with the gas access of described secondary heater (22), and the outlet of the heat transferring medium of described secondary heater (22) is connected to the heat transferring medium inlet of described the 5th heater (26).
4. according to any described system among the claim 1-3, it is characterized in that this system also comprises first deduster (13), described first deduster (13) is connected with described first exhaust outlet (15).
5. system according to claim 4 is characterized in that, this system also comprises tail gas odor eliminator (18), and described tail gas odor eliminator (18) is connected with described first deduster (13).
6. system according to claim 5 is characterized in that, described tail gas odor eliminator (18) comprises the wet type odor eliminator (18 ') of connecting successively by gas flow direction and dry type odor eliminator (18 ").
7. system according to claim 6 is characterized in that, described wet type odor eliminator (18 ') is the buck odor eliminator.
8. system according to claim 6 is characterized in that, and described dry type odor eliminator (18 ") be the plain odor eliminator of plant extract.
9. according to any described system among the claim 1-3, it is characterized in that this system also comprises second deduster (23), described second deduster (23) is connected with described second exhaust outlet (25).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205596846U CN201854649U (en) | 2010-10-12 | 2010-10-12 | System for producing lysine sulphate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205596846U CN201854649U (en) | 2010-10-12 | 2010-10-12 | System for producing lysine sulphate |
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| Publication Number | Publication Date |
|---|---|
| CN201854649U true CN201854649U (en) | 2011-06-08 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010205596846U Expired - Lifetime CN201854649U (en) | 2010-10-12 | 2010-10-12 | System for producing lysine sulphate |
Country Status (1)
| Country | Link |
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| CN (1) | CN201854649U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104399262A (en) * | 2014-10-16 | 2015-03-11 | 浙江索纳克生物科技有限公司 | Porcine blood protein powder drying and recycling apparatus |
-
2010
- 2010-10-12 CN CN2010205596846U patent/CN201854649U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104399262A (en) * | 2014-10-16 | 2015-03-11 | 浙江索纳克生物科技有限公司 | Porcine blood protein powder drying and recycling apparatus |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: COFCO BIOCHEMICAL (ANHUI) CO., LTD. Free format text: FORMER NAME: FENGYUAN BIOLOGICAL CHEMISTRY CO., LTD., ANHUI PROV. |
|
| CP03 | Change of name, title or address |
Address after: 233010 No. 1 COFCO Avenue, Anhui, Bengbu Patentee after: COFCO Biochemical (Anhui) Co., Ltd. Address before: 233010 No. 73, Daqing Road, Bengbu, Anhui Patentee before: Fengyuan Biological Chemistry Co., Ltd., Anhui Prov. |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20110608 |