CN208660407U - A kind of concentrated acid crystallization apparatus - Google Patents
A kind of concentrated acid crystallization apparatus Download PDFInfo
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- CN208660407U CN208660407U CN201820930294.1U CN201820930294U CN208660407U CN 208660407 U CN208660407 U CN 208660407U CN 201820930294 U CN201820930294 U CN 201820930294U CN 208660407 U CN208660407 U CN 208660407U
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Abstract
The utility model discloses a kind of concentrated acid crystallization apparatus, including condenser, forecooler, crystallizer, enrichment device, seperator, degassing tank and receiving slit, it further include mother vat, return pipe and mother liquor pump, the leakage fluid dram of the mother vat is connected by the inlet of return pipe and degassing tank, the mother liquor pump is arranged on return pipe, the inlet of the mother vat and the liquid outlet of seperator connect, the high liquor outlet of mother vat is connect with receiving slit, effect of the utility model enhancing to the evaporation and concentration and cooling that enter forecooler acid bath, realizes the increase of production capacity.
Description
Technical field
The utility model relates to the de- saltcake technical fields in production process of viscose fiber, more particularly to raw in viscose rayon
The concentrated acid crystallization apparatus of sodium sulphate in production in spinning recycling coagulating bath.
Background technique
It is often used concentrated sulfuric acid absorption crystallizer in viscose rayon production industry (or other industry), which is mainly used for
The sodium sulphate in viscose rayon production in spinning recycling coagulating bath is precipitated, making its crystallization is Na2SO4·10H2O.Its working principle
It is: accelerates the evaporation of acid bath moisture by improving vacuum degree, the steam evaporated is absorbed by the concentrated sulfuric acid, and acid bath is made to reach cooling
And the effect crystallized, the sodium sulphate salt slurry of precipitation pass through seperator for the Na of crystallization again2SO4·10H2O is separated.To acid bath
In extra sodium sulphate separated, to stablize acid bath component, be control acid bath total amount, reduce the key equipment of sulfuric acid consumption.
Concentrated acid crystallizer is driven to cool to discharging time after each parking maintenance or production adjustment longer, generally wants 2-3 hours, shadow
Ring yield；This technology will carry out process route change into acid and K1 into acid to BK1-3 on the basis of existing equipment, in original production
Yield is improved on the basis of energy, guarantee is stable, and capital investment is minimum, and effect is long-acting.The capital investment of factory is reduced simultaneously.
The prior art is as shown in Figure 1, from about 50 DEG C of concentration acid baths of temperature that flash distillation comes, through into sour flowmeter into forecooler 2
(VK1~VK 3) passes through condenser 1(BK1- BK3) evaporation be cooled to 28-32 DEG C, enter back into crystallizer 3(K1~K 4)
In, continue continuous evaporation and cooled down, is concentrated to saturation state precipitation crystallization and (in order to guarantee the suspension of crystal, is set in K1~K 4
There is air stirrer).Salt slurry is got off from K4 to be driven into enrichment device 4 (E) by brine pump 8 (SP), the dense salt slurry after enrichment
Into saltcake is isolated in seperator 5(Z), the mother liquor after being separated enters acid bath receiving slit 7, and high-order overflow goes out in enrichment device
Dilute salt slurry passes through degassing tank 6(EG2) it is drawn into acid bath condenser 1(BK1- BK3 again) in, on the one hand cooled down in VK1-3 with it
On the other hand the steam evaporated is heated to 38 DEG C or so in itself and returns in acid bath receiving slit, makes full use of thermal energy.Existing skill
The cooling effect of precooler 2 is poor in art practical application, and production capacity is smaller.
If Chinese patent notification number is CN202751833U, a kind of acid absorption crystallization dress was disclosed on 2 27th, 2013
It sets, including vacuum system, acid bath processing system, wherein further include having the sulfuric acid circulatory system, acid bath processing system includes successively
The forecooler group of connection, crystallization unit, enrichment device, centrifuge, waste heat condensation device group；The sulfuric acid circulatory system includes to be circularly set
Vapor absorber group, seal groove, sour tank, acid pump and heat exchanger；Crystallization unit top is connected to vapor absorber group；Vacuum
System includes the vacuum water spraying device for vacuumizing to vapor absorber group, and sulfuric acid circulatory system internal circulation flow has sulfuric acid molten
Liquid；Enrichment device lower part is connect with centrifuge, and the enrichment device top is connected with waste heat condensation device group, forecooler group top and waste heat
The connection of condenser group.It is above-mentioned practical newly to equally exist that cooling effect is poor, and production capacity is small.
Utility model content
In order to overcome the drawbacks of the prior art, the utility model provides a kind of concentrated acid crystallization apparatus, which can enhance
Effect to the evaporation and concentration and cooling that enter forecooler acid bath, realizes the increase of production capacity.
In order to solve the above-mentioned technical problem, the technical solution adopted in the utility model is:
A kind of concentrated acid crystallization apparatus, including condenser, forecooler, crystallizer, enrichment device, seperator, degassing tank and reception
Slot, the forecooler are connect with crystallizer, and crystallizer is connect by the first brine pump with enrichment device, and enrichment device and seperator connect
It connects, seperator is connect with receiving slit；The high-order overflow port of the enrichment device is connect with degassing tank, and degassing tank is connect with condenser,
Condenser is connect with receiving slit；Condenser is cooling to the acid bath in forecooler, it is characterised in that: further includes mother vat, return pipe
It is pumped with mother liquor, the leakage fluid dram of the mother vat is connected by the inlet of return pipe and degassing tank, and the mother liquor pump setting is being returned
In flow tube, the inlet of the mother vat and the liquid outlet of seperator are connected, and the high liquor outlet of mother vat is connect with receiving slit.
It further include circulation pipe and the second brine pump, one end of the circulation pipe and the liquid outlet of crystallizer connect, the other end
It is connect with the inlet of crystallizer, second brine pump is arranged on circulation pipe.
First brine pump is set side by side with the second brine pump, and the first brine pump is used to squeeze into acid bath to enrichment device；The
Two brine pumps are used to squeeze into acid bath to crystallizer.
The circulation pipe is equipped with the control valve for controlling flow.
The utility model has the advantage that
1, the utility model increases mother vat, return pipe and mother liquor pump, states the leakage fluid dram of mother vat by return pipe and takes off
The inlet of gas tank connects, and mother liquor pump is arranged on return pipe, and the inlet of mother vat and the liquid outlet of seperator connect, mother liquor
The high liquor outlet of bucket is connect with receiving slit.Dense salt slurry after enrichment, which enters, isolates saltcake in seperator, the mother after being separated
Liquid enters newly-increased mother vat, is pumped into degassing tank through mother liquor, and dilute salt slurry that high-order overflow goes out from enrichment device utilizes together
System negative pressure is pumped into acid bath condenser BK1-3, increases the flow of dilute salt slurry in acid bath condenser BK1-3, thus enhancing pair
Into the evaporation and concentration of VK acid bath and the effect of cooling, the increase of production capacity is realized.
2, the utility model includes circulation pipe and the second brine pump, and one end of circulation pipe and the liquid outlet of crystallizer connect,
The connection of the inlet of the other end and crystallizer, second brine pump are arranged on circulation pipe；Make from the part that crystallizer comes out
(flowmeter metering, self controllable) salt slurry is circulated back to system, since crystallizer drop temperature is lower than crystallizer feeding temperature, generally
The temperature difference can reach 8-10 DEG C, and system cooling is made to be rapidly reached technique requirement, reduces and drives to arrive discharging time；Utilize crystallizer salt slurry
In the saltcake crystal that contains crystal seed is added in advance to system front end, advantageous crystallization process is gone on smoothly, while also improving crystallization effect,
To improve crystallization production capacity.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the prior art.
Fig. 2 is the structural schematic diagram of the utility model.
It is marked in figure；1, condenser, 2, forecooler, 3, crystallizer, 4, enrichment device, 5, seperator, 6, degassing tank, 7, reception
Slot, the 8, first brine pump, 9, mother vat, 10, return pipe, 11, mother liquor pump, 12, circulation pipe, the 13, second brine pump.
Specific embodiment
The utility model is further elaborated with reference to the accompanying drawing, but the utility model is not limited to following embodiment,
The method is conventional method unless otherwise instructed, and the material can be gotten from open business unless otherwise instructed.
Embodiment 1
A kind of concentrated acid crystallization apparatus, including condenser 1, forecooler 2, crystallizer 3, enrichment device 4, seperator 5, degassing tank 6
With receiving slit 7, the forecooler 2 is connect with crystallizer 3, and crystallizer 3 is connect by the first brine pump 8 with enrichment device 4, enrichment device
4 connect with seperator 5, and seperator 5 is connect with receiving slit 7；The high-order liquid outlet of the enrichment device 4 is connect with degassing tank 6, degassing
Tank 6 is connect with condenser 1, and condenser 1 is connect with receiving slit 7；Condenser 1 is cooling to the acid bath in forecooler 2.(such as Fig. 1 institute
Show).
The improvement of the utility model is: further including mother vat 9, return pipe 10 and mother liquor pump 11, the row of the mother vat 9
Liquid mouth is connect by return pipe 10 with the inlet of degassing tank 6, and the mother liquor pump 11 is arranged on return pipe 10, the mother vat
9 inlet is connect with the liquid outlet of seperator 5, and the high liquor outlet of mother vat 9 connect (as shown in Figure 2) with receiving slit 7.
About 50 DEG C of concentration acid baths of temperature come from flash distillation, through into sour flowmeter into forecooler 2(VK1~VK 3), by cold
Condenser 1(BK1- BK3) evaporation be cooled to 28-32 DEG C, the dense salt slurry after enrichment, which enters, isolates saltcake in seperator, separated
Mother liquor afterwards enters newly-increased mother vat, is pumped into degassing tank through mother liquor, and dilute salt slurry one that high-order overflow goes out from enrichment device
It rises and is pumped into acid bath condenser BK1-3 using system negative pressure, increase the flow of dilute salt slurry in acid bath condenser BK1-3, thus
Enhance the effect to the evaporation and concentration and cooling for entering VK acid bath, realizes the increase of production capacity.
Embodiment 2
A kind of concentrated acid crystallization apparatus, including condenser 1, forecooler 2, crystallizer 3, enrichment device 4, seperator 5, degassing tank 6
With receiving slit 7, the forecooler 2 is connect with crystallizer 3, and crystallizer 3 is connect by the first brine pump 8 with enrichment device 4, enrichment device
4 connect with seperator 5, and seperator 5 is connect with receiving slit 7；The high-order liquid outlet of the enrichment device 4 is connect with degassing tank 6, degassing
Tank 6 is connect with condenser 1, and condenser 1 is connect with receiving slit 7；Condenser 1 is cooling to the acid bath in forecooler 2.(such as Fig. 1 institute
Show).
The improvement of the utility model is: further including mother vat 9, return pipe 10 and mother liquor pump 11, the row of the mother vat 9
Liquid mouth is connect by return pipe 10 with the inlet of degassing tank 6, and the mother liquor pump 11 is arranged on return pipe 10, the mother vat
9 inlet is connect with the liquid outlet of seperator 5, and the high liquor outlet of mother vat 9 connect (as shown in Figure 2) with receiving slit 7.
Further improve also resides in, and further includes circulation pipe 12 and the second brine pump 13, one end of the circulation pipe 12 with
The liquid outlet of crystallizer 3 connects, and the other end is connect with the inlet of crystallizer 3, and second brine pump 13 is arranged in circulation pipe
On 12.First brine pump 8 is set side by side with the second brine pump 13, and the first brine pump 8 is used to squeeze into acid bath to enrichment device 4；
Second brine pump 13 is used to squeeze into acid bath to crystallizer 3.Circulation pipe 12 is equipped with control valve (such as Fig. 2 for controlling flow
It is shown).
Salt slurry pump discharge is drawn on the FRPP pipeline to the pipeline of forecooler 2 of a DN50, with valve regulated flow.It is opening
Control valve is opened when vehicle and in production process, is made from the part that crystallizer 3 comes out (flowmeter metering, self controllable) salt slurry circulation
System is returned to, since 3 drop temperature of crystallizer is lower than 3 feeding temperature of crystallizer, the general temperature difference can reach 8-10 DEG C, drop system
Temperature is rapidly reached technique requirement, reduces and drives to arrive discharging time；System front end is shifted to an earlier date using the saltcake crystal contained in K4 salt slurry
Crystal seed is added, advantageous crystallization process is gone on smoothly, while also improving crystallization effect, to improve crystallization production capacity.
Due to the change of process route, the acid intake amount of device forecooler can increase the utility model, and the flow of brine pump will
Increase (by taking the device of 6T/h as an example: 22 sides of acid intake amount/h of forecooler, 20 sides of salt slurry flow/h, forecooler after transformation before being transformed
26 sides of acid intake amount/h, 28 sides of salt slurry flow/h are recycled back to 5 sides of dosage/h, and production capacity increases by 20% or so).Other techniques are constant.
Claims (4)
1. a kind of concentrated acid crystallization apparatus, including condenser (1), forecooler (2), crystallizer (3), enrichment device (4), seperator (5),
Degassing tank (6) and receiving slit (7), the forecooler (2) connect with crystallizer (3), and crystallizer (3) passes through the first brine pump (8)
It is connect with enrichment device (4), enrichment device (4) is connect with seperator (5), and seperator (5) is connect with receiving slit (7)；The enrichment device
(4) high-order liquid outlet is connect with degassing tank (6), and degassing tank (6) is connect with condenser (1), condenser (1) and receiving slit (7)
Connection；Condenser (1) is cooling to the acid bath in forecooler (2), it is characterised in that: further include mother vat (9), return pipe (10) and
Mother liquor pumps (11), and the leakage fluid dram of the mother vat (9) is connect by return pipe (10) with the inlet of degassing tank (6), the mother
Liquid pump (11) is arranged on return pipe (10), and the inlet of the mother vat (9) is connect with the liquid outlet of seperator (5), mother liquor
The high liquor outlet of bucket (9) is connect with receiving slit (7).
2. a kind of concentrated acid crystallization apparatus according to claim 1, it is characterised in that: further include circulation pipe (12) and the second salt
One end of stock pump (13), the circulation pipe (12) is connect with the liquid outlet of crystallizer (3), the feed liquor of the other end and crystallizer (3)
Mouth connection, second brine pump (13) are arranged on circulation pipe (12).
3. a kind of concentrated acid crystallization apparatus according to claim 2, it is characterised in that: first brine pump (8) and second
Brine pump (13) is set side by side, and the first brine pump (8) is used to squeeze into acid bath to enrichment device (4)；Second brine pump (13) be used for
Crystallizer (3) squeezes into acid bath.
4. a kind of concentrated acid crystallization apparatus according to claim 2, it is characterised in that: the circulation pipe (12) is equipped with and is used for
Control the control valve of flow.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820930294.1U CN208660407U (en) | 2018-06-15 | 2018-06-15 | A kind of concentrated acid crystallization apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820930294.1U CN208660407U (en) | 2018-06-15 | 2018-06-15 | A kind of concentrated acid crystallization apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208660407U true CN208660407U (en) | 2019-03-29 |
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ID=65824341
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820930294.1U Expired - Fee Related CN208660407U (en) | 2018-06-15 | 2018-06-15 | A kind of concentrated acid crystallization apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208660407U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108579118A (en) * | 2018-06-15 | 2018-09-28 | 成都丽雅纤维股份有限公司 | A kind of concentrated acid crystallization apparatus |
-
2018
- 2018-06-15 CN CN201820930294.1U patent/CN208660407U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108579118A (en) * | 2018-06-15 | 2018-09-28 | 成都丽雅纤维股份有限公司 | A kind of concentrated acid crystallization apparatus |
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| Date | Code | Title | Description |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20190329 Termination date: 20200615 |