CN214218200U - System for viscose fiber acid bath integrated production anhydrous sodium sulphate - Google Patents
System for viscose fiber acid bath integrated production anhydrous sodium sulphate Download PDFInfo
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- CN214218200U CN214218200U CN202120219581.3U CN202120219581U CN214218200U CN 214218200 U CN214218200 U CN 214218200U CN 202120219581 U CN202120219581 U CN 202120219581U CN 214218200 U CN214218200 U CN 214218200U
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Abstract
The utility model belongs to the technical field of anhydrous sodium sulphate production, in particular to a system for producing anhydrous sodium sulphate by viscose fiber acid bath integration, which comprises an acid bath pipeline, the acid bath pipeline passes through a mixing bottom groove, a multi-stage preheater device and a heater, the pre-evaporator and the multi-stage evaporator device enter the thickener, the thickener is communicated with a buffer tank through an overflow port, a last-stage evaporator in the multi-stage evaporator device is connected with the buffer tank, the buffer tank is connected with a mixing bottom tank, a discharge port of the thickener is connected with a vacuum filter, a washing liquor pipeline is arranged on the vacuum filter and is connected with a melting barrel, the melting barrel is connected with an alkali liquor pipeline, a discharge port of the melting barrel is connected with a hydrocyclone, a discharge port of the concentrated solution of the hydrocyclone is connected with a centrifugal machine, a discharge port of the centrifugal machine is connected with a drying device, a discharge port of the drying device is sequentially connected with a storage bin and a packaging machine, and a gas phase outlet of the drying device is sequentially connected with a dust remover and a spray tower. The utility model has the advantages of short process flow, simple operation and less investment.
Description
Technical Field
The utility model belongs to the technical field of anhydrous sodium sulphate production, concretely relates to viscose fiber acid bath integration production anhydrous sodium sulphate's system.
Background
The anhydrous sodium sulfate has bitter taste and hygroscopicity, and is colorless transparent, large crystal or granular small crystal, and can absorb water to generate sodium sulfate decahydrate (Na)2SO4·10H2O, aka mirabilite). The anhydrous sodium sulphate is mainly used for manufacturing water glass, porcelain glaze, paper pulp, refrigerating mixing agent, detergent, drying agent, fuel diluent and the like, and is a common inorganic industrial raw material.
The production process of obtaining mirabilite by cooling and crystallizing viscose acid bath and then obtaining anhydrous sodium sulphate by evaporation and crystallization has long been industrialized. The existing technological process for producing anhydrous sodium sulphate is as follows: 1. the acid bath is controlled by a flowmeter to enter an evaporation device at a certain flow rate, is preheated by a multi-stage preheater and then enters a heater to heat the acid bath to a designed temperature by using fresh steam, enters a pre-evaporator to be preliminarily evaporated by a pipeline, then enters the evaporator to be cooled step by step, and releases secondary steam to enter the preheater and to be preheated by the acid bath in the corresponding preheater. 2. The acid bath after temperature reduction and concentration enters a concentration bath trough through a pipeline, one part of the acid bath enters a bottom trough, and the other part of the acid bath is pumped into a crystallization device by a circulating pump (due to the characteristic of sodium sulfate, when the temperature is lower than 33 ℃, the sodium sulfate crystals carry crystal water). The acid bath is gradually cooled in the precooler and the crystallizer, after the temperature reaches the design temperature, the sodium sulfate particles in the acid bath are in a saturated state, the acid bath containing the sodium sulfate particles is pumped into the thickener equipment through a pump, the sodium sulfate particles in the thickener equipment are continuously polymerized, finally, the acid bath enters a centrifuge for solid-liquid separation through a pipeline, the sodium sulfate particles enter a roasting device, and the separated acid bath enters a bottom groove for continuous recycling. 3. The sodium sulfate particles enter a melting barrel with a stirring device of a roasting device to be dissolved by hot water at 75-80 ℃, and the dissolution of the hot water at the temperature is to dissolve the crystal water carried by the sodium sulfate particles and dissolve the sodium sulfate particles. Because sodium sulfate has crystal water during crystallization, the pH value in the melting barrel needs to be controlled for controlling the quality of a finished sodium sulfate product and the service life of later-stage equipment, NaOH needs to be added, and the pH value of the solution needs to be adjusted. To prevent particle deposition, the equipment agitation was turned on all the time. After the sodium sulfate with crystal water is fully dissolved, the solution is pumped into an evaporative crystallizer (VDK) device by a PV circulating pump, enters a circulating pump (UP) through a pipeline, is pumped into a heater (H) device by a pump and is heated by fresh steam, the heated salt slurry enters the evaporative crystallizer to be evaporated and thickened, and high-level overflow enters a melting barrel (S) through an overflow device for recycling. 4. The equipment starts to run, samples are periodically taken from the melting barrel, the concentration of the solution is tested, when the concentration reaches the design requirement, the PE circulating pump is started to pump the solution with solid particles into the cyclone device, after the solution is separated by the cyclone device, the concentrated solution enters a centrifugal machine for separation, the solid enters a drying device, and the separated dilute mother liquor returns to the melting barrel for continuous recycling. The dilute liquid separated by the cyclone also returns to the melting barrel through a pipeline for continuous recycling. 5. The sodium sulfate containing moisture enters a drying device, is heated by hot air in a drying system, evaporates the moisture carried by sodium sulfate particles, is conveyed to a dust remover through a pipeline, enters a storage bin after dust removal, enters a packaging bearing system in a certain amount through a vibrating screen, and leaves a factory after packaging.
The existing process has long flow, complex operation, difficult control, more matched equipment and large investment.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is: overcomes the defects of the prior art, provides a system for producing anhydrous sodium sulphate by integrating viscose fiber acid bath, and has short process flow and simple operation.
The utility model discloses an adopt following technical scheme to realize:
the viscose acid bath integrated anhydrous sodium sulphate production system comprises an acid bath pipeline, wherein the acid bath pipeline is connected with a mixed bottom tank, the bottom of the mixed bottom tank is sequentially connected with a multi-stage preheater device, a heater and a pre-evaporator, the pre-evaporator is connected with a multi-stage evaporator device, the bottoms of the last two stages of evaporators in the multi-stage evaporator device are connected with a thickener, the thickener is provided with an overflow port and communicated with a cache tank through the overflow port, the last stage evaporator in the multi-stage evaporator device is connected with the cache tank, the cache tank is connected with the mixed bottom tank, the tops of the last two stages of evaporators in the multi-stage evaporator device and the top of the mixed bottom tank are connected with a mixed condenser, the cache tank is connected with a concentrated acid tank, the discharge port of the thickener is connected with a vacuum filter, a washing liquid pipeline is arranged on the vacuum filter, the discharge port of the vacuum filter is connected with a melting barrel, the melting barrel is connected with an alkali liquor pipeline, a discharge port of the melting barrel is connected with a cyclone, a discharge port of a concentrated solution of the cyclone is connected with a centrifugal machine, a discharge port of the centrifugal machine is connected with a drying device, a discharge port of the drying device is sequentially connected with a storage bin and a packing machine, and a gas phase outlet of the drying device is sequentially connected with a dust remover and a spray tower.
Preferably, a flow meter is arranged at the outlet of the bottom of the mixing bottom tank.
Preferably, the multistage preheater device comprises at least 5 stages of preheaters which are sequentially connected through a pipeline, the multistage evaporator device comprises at least 5 stages of evaporators which are sequentially connected through a pipeline, a top steam outlet of each stage of evaporator except the last two stages of evaporators is connected with the corresponding preheater, and a steam outlet of each pre-evaporator is connected with the corresponding preheater.
Preferably, the bottom of each stage of evaporator except the last two stages in the multi-stage evaporator device is connected with the ground groove, and the bottom of the pre-evaporator is also connected with the ground groove.
Preferably, a dilute liquid outlet at the top of the cyclone is connected with the melting barrel.
Preferably, the dilute mother liquor outlet of the centrifuge is connected with the melting barrel.
The working principle and the process are as follows:
the acid bath is controlled by a flowmeter to enter an evaporation device at a certain flow rate, enters a heater to heat the acid bath to a designed temperature by using fresh steam after being preheated by a multi-stage preheater device, enters a pre-evaporator to be preliminarily evaporated by a pipeline, then enters the multi-stage evaporator device to be cooled step by step, releases secondary steam to enter the preheater, and is preheated by the acid bath corresponding to the acid bath in the corresponding preheater. The acid feeding amount is required to meet the requirements of meeting the operation condition of an evaporation device and reaching the supersaturated state of the acid bath after the concentrated acid is reached. And the secondary steam at the top of the last two stages of evaporators in the multi-stage preheater device enters a mixing condenser for condensation, the acid bath after evaporation and concentration is controlled at 48-50 ℃, and then enters thickener equipment with a stirring device from the bottoms of the last two stages of evaporators through pipelines for thickening, and stirring operation can ensure that particles in the thickener equipment are not condensed together and increase the granularity. The temperature of the acid bath is controlled to be 48-50 ℃, so that the acid bath can be recycled, and the sodium sulfate is prevented from carrying with crystal water when being crystallized due to too low temperature.
The solution of the acid bath after being thickened in the thickener enters a vacuum filter through a pipeline for spray washing and filtration, solid-liquid separation is carried out, solid particles enter a roasting melting barrel for dissolution, and the dissolution temperature is controlled to be 75-80 ℃. In order to control the quality of the finished sodium sulfate product and the service life of later equipment, the pH value in the melting barrel needs to be controlled, so that NaOH alkali liquor needs to be added to adjust the pH value of the solution. The diluted mother liquor precipitated in the thickener enters a buffer tank from an overflow port at the upper part of the thickener, the acid bath in the buffer tank enters a mixed bottom tank and is mixed with the fresh acid bath for recycling, and during intermittent production, the acid bath can be discharged into the buffer tank through a final-stage evaporator and is conveyed to a concentrated acid tank.
When the concentration in the melting barrel reaches the design requirement, a PE circulating pump is started to pump a solution with solid particles into a cyclone device, the solution is separated by the cyclone device, a concentrated solution enters a centrifugal machine for separation, the solid enters a drying device, and the separated dilute mother liquor returns to the melting barrel for continuous recycling. The dilute liquid separated by the cyclone also returns to the melting barrel through a pipeline for continuous recycling.
The sodium sulfate containing moisture enters a drying device, hot air is used for heating in a drying system, the moisture carried by sodium sulfate particles is evaporated, a gas phase is conveyed to a dust remover through a pipeline, the dust is removed and then is sprayed and absorbed by a spray tower, the emission is up to the standard, a product enters a storage bin, and then the product is packaged by a packaging machine and leaves the factory.
Compared with the prior art, the beneficial effects of the utility model are as follows:
1. compared with the prior art, the utility model process flow shortens, and the operation is more simple and convenient.
2. Because the flow shortens, the utility model discloses corollary equipment reduces, has reduced investment and equipment maintenance volume.
3. The utility model discloses equipment reduces newly-gone factory building area and reduces, has reduced the capital construction investment.
Drawings
Fig. 1 is a schematic structural view of the present invention;
in the figure: 1. an acid bath line; 2. a mixing bottom tank; 3. a mixing condenser; 4. a flow meter; 5. a multi-stage preheater unit; 6. a heater; 7. a pre-evaporator; 8. a multi-stage evaporator device; 9. a ground groove; 10. a concentrated acid tank; 11. a cache slot; 12. a thickener; 13. a vacuum filter; 14. a wash liquor line; 15. an alkali liquor pipeline; 16. a melting barrel; 17. a liquid cyclone; 18. a centrifuge; 19. a drying device; 20. a dust remover; 21. a spray tower; 22. a storage bin; 23. a packaging machine; A1-A11 is a preheater; V3-V13 is evaporator.
Detailed Description
The present invention will be further described with reference to the accompanying drawings.
As shown in figure 1, the viscose acid bath integrated anhydrous sodium sulphate production system comprises an acid bath pipeline 1, the acid bath pipeline 1 is connected with a mixed bottom tank 2, the bottom of the mixed bottom tank 2 is sequentially connected with a multi-stage preheater device 5, a heater 6 and a pre-evaporator 7, the pre-evaporator 7 is connected with a multi-stage evaporator device 8, the bottoms of the last two stages of evaporators in the multi-stage evaporator device 8 are respectively connected with a thickener 12, the thickener 12 is provided with an overflow port, the thickener 12 is communicated with a buffer tank 11 through the overflow port, the last stage evaporator in the multi-stage evaporator device 8 is connected with the buffer tank 11, the buffer tank 11 is connected with the mixed bottom tank 2, the top of the last two stages of evaporators in the multi-stage evaporator device 8 and the top of the mixed bottom tank 2 are respectively connected with a mixed condenser 3, the buffer tank 11 is connected with an acid concentration tank 10, the discharge port of the thickener 12 is connected with a vacuum filter 13, the vacuum filter 13 is provided with a washing liquid pipeline 14 for connection, a discharge port of the vacuum filter 13 is connected with a melting barrel 16, the melting barrel 16 is connected with an alkali liquid pipeline 15, a discharge port of the melting barrel 16 is connected with a cyclone 17, a discharge port of a concentrated solution of the cyclone 17 is connected with a centrifuge 18, a discharge port of the centrifuge 18 is connected with a drying device 19, a discharge port of the drying device 19 is sequentially connected with a storage bin 22 and a packing machine 23, and a gas phase outlet of the drying device 19 is sequentially connected with a dust remover 20 and a spray tower 21.
And a flow meter 4 is arranged at the outlet of the bottom of the mixing bottom tank 2.
The multistage preheater device 5 comprises 11 stages of preheaters A1-A11 which are connected in sequence through pipelines, the multistage evaporator device 8 comprises 11 stages of evaporators V3-V13 which are connected in sequence through pipelines, the top steam outlet of each stage of evaporator except the last two stages of evaporators V3-V11 is connected with a corresponding A3-A11 preheater, and the steam outlet of the pre-evaporator 7 is connected with a corresponding A1 preheater and a corresponding A2 preheater.
The bottom of each evaporator of V3-V11 except the last two stages in the multi-stage evaporator device 8 is connected with the ground groove 9, and the bottom of the pre-evaporator 7 is also connected with the ground groove 9.
The dilute liquid outlet at the top of the cyclone 17 is connected with the melting barrel 16.
The dilute mother liquor outlet of the centrifuge 18 is connected with the melting barrel 16.
When in work:
the acid bath enters a mixing bottom tank 2 from an acid bath pipeline 1, then enters an evaporation device at a certain flow rate under the control of a flow meter 4, enters a heater 6 after being preheated by a multistage preheater 5 device, heats the acid bath to a designed temperature by using fresh steam, enters a pre-evaporator 7 through a pipeline for preliminary evaporation, enters a multistage evaporator device 8 for gradual cooling, releases secondary steam to enter the preheater, and is preheated by corresponding acid bath in the preheater. The acid feeding amount is required to meet the requirements of meeting the operation condition of an evaporation device and reaching the supersaturated state of the acid bath after the concentrated acid is reached. The secondary steam at the top of the last two-stage evaporators V12 and V13 in the multi-stage preheater device 8 enters the mixing condenser 3 for condensation, the acid bath after evaporation and concentration is controlled at 48-50 ℃, and then enters the thickener 12 equipment with a stirring device from the bottom of the last two-stage evaporator through a pipeline for thickening, and stirring operation can ensure that particles in the thickener equipment are not condensed together and increase the granularity. The temperature of the acid bath is controlled to be 48-50 ℃, so that the acid bath can be recycled, and the sodium sulfate is prevented from carrying with crystal water when being crystallized due to too low temperature.
The solution of the acid bath after being thickened in the thickener 12 enters a vacuum filter 13 through a pipeline for spray washing and filtration, solid-liquid separation is carried out, solid particles enter a roasting melting barrel 16 for dissolution, and the dissolution temperature is controlled to be 75-80 ℃. In order to control the quality of the finished sodium sulfate product and the service life of later equipment, the pH value in the melting barrel 16 needs to be controlled, so that NaOH alkali liquor needs to be added to adjust the pH value of the solution. The dilute mother liquor precipitated in the thickener 12 enters the buffer tank 11 from an overflow port at the upper part of the thickener 12, the acid bath in the buffer tank 11 enters the mixed bottom tank 2 to be mixed with the fresh acid bath for recycling, and during intermittent production, the acid bath can be discharged into the buffer tank 11 through the last-stage evaporator V13 and conveyed to the concentrated acid tank 10.
When the concentration in the melting barrel 16 reaches the design requirement, a PE circulating pump is started to pump a solution with solid particles into a cyclone 17 device, after the solution is separated by the cyclone 17, a concentrated solution enters a centrifugal machine 18 for separation, the solid enters a drying device 19, and the separated dilute mother liquor returns to the melting barrel 16 for continuous recycling. The dilute liquid separated by the cyclone 17 is returned to the melting barrel 16 through a pipeline for continuous recycling.
The sodium sulfate containing moisture enters a drying device 19, hot air is used for heating in a drying system, the moisture carried by sodium sulfate particles is evaporated, gas phase is conveyed to a dust remover 20 through a pipeline, the dust is removed and then is sprayed and absorbed by a spray tower 21, the emission reaches the standard, a product enters a storage bin 22, and then the product is packaged by a packaging machine 23 and leaves the factory.
Of course, the above description is only a preferred embodiment of the present invention, and should not be taken as limiting the scope of the embodiments of the present invention. The present invention is not limited to the above examples, and the technical field of the present invention is equivalent to the changes and improvements made in the actual range of the present invention, which should be attributed to the patent coverage of the present invention.
Claims (6)
1. The utility model provides a viscose fiber acid bath integration production anhydrous sodium sulphate's system, includes acid bath pipeline (1), its characterized in that: the acid bath pipeline (1) is connected with the mixing bottom tank (2), the bottom of the mixing bottom tank (2) is sequentially connected with a multi-stage preheater device (5), a heater (6) and a pre-evaporator (7), the pre-evaporator (7) is connected with a multi-stage evaporator device (8), the bottom of the last two-stage evaporator in the multi-stage evaporator device (8) is connected with a thickener (12), an overflow port is arranged on the thickener (12), the thickener (12) is communicated with a cache tank (11) through the overflow port, the last-stage evaporator in the multi-stage evaporator device (8) is connected with the cache tank (11), the cache tank (11) is connected with the mixing bottom tank (2), the top of the last two-stage evaporator in the multi-stage evaporator device (8) and the top of the mixing bottom tank (2) are connected with a mixing condenser (3), the cache tank (11) is connected with a concentrated acid tank (10), the discharge port of the thickener (12) is connected with a vacuum filter (13), a washing liquid pipeline (14) is arranged on the vacuum filter (13) to be connected, a discharge hole of the vacuum filter (13) is connected with a melting barrel (16), the melting barrel (16) is connected with an alkali liquid pipeline (15), a discharge hole of the melting barrel (16) is connected with a cyclone (17), a discharge hole of a concentrated solution of the cyclone (17) is connected with a centrifugal machine (18), a discharge hole of the centrifugal machine (18) is connected with a drying device (19), a discharge hole of the drying device (19) is sequentially connected with a storage bin (22) and a packing machine (23), and a gas phase outlet of the drying device (19) is sequentially connected with a dust remover (20) and a spray tower (21).
2. The system for integrated production of anhydrous sodium sulphate by viscose fiber acid bath according to claim 1, wherein: a flowmeter (4) is arranged at the outlet of the bottom of the mixing bottom tank (2).
3. The system for integrated production of anhydrous sodium sulphate by viscose fiber acid bath according to claim 1, wherein: the multistage preheater device (5) comprises at least 5 stages of preheaters which are sequentially connected through pipelines, the multistage evaporator device (8) comprises at least 5 stages of evaporators which are sequentially connected through pipelines, a top steam outlet of each stage of evaporator except the last two stages of evaporators is connected with the corresponding preheater, and a steam outlet of the pre-evaporator (7) is connected with the corresponding preheater.
4. The system for integrated production of anhydrous sodium sulphate by viscose fiber acid bath according to claim 1, wherein: the bottom of each stage of evaporator except the last two stages in the multi-stage evaporator device (8) is connected with a ground groove (9), and the bottom of the pre-evaporator (7) is also connected with the ground groove (9).
5. The system for integrated production of anhydrous sodium sulphate by viscose fiber acid bath according to claim 1, wherein: the dilute liquid outlet at the top of the cyclone (17) is connected with the melting barrel (16).
6. The system for integrated production of anhydrous sodium sulphate by viscose fiber acid bath according to claim 1, wherein: the dilute mother liquor outlet of the centrifuge (18) is connected with the melting barrel (16).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120219581.3U CN214218200U (en) | 2021-01-26 | 2021-01-26 | System for viscose fiber acid bath integrated production anhydrous sodium sulphate |
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| CN202120219581.3U CN214218200U (en) | 2021-01-26 | 2021-01-26 | System for viscose fiber acid bath integrated production anhydrous sodium sulphate |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253545A (en) * | 2022-07-26 | 2022-11-01 | 唐山三友集团兴达化纤有限公司 | Method and system for recycling dust removal water in viscose staple fiber production process |
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2021
- 2021-01-26 CN CN202120219581.3U patent/CN214218200U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253545A (en) * | 2022-07-26 | 2022-11-01 | 唐山三友集团兴达化纤有限公司 | Method and system for recycling dust removal water in viscose staple fiber production process |
| CN115253545B (en) * | 2022-07-26 | 2023-10-10 | 唐山三友集团兴达化纤有限公司 | Method and system for recycling dedusting water in viscose staple fiber production process |
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