CN220259070U - Alkali ash treatment system - Google Patents
Alkali ash treatment system Download PDFInfo
- Publication number
- CN220259070U CN220259070U CN202321712536.7U CN202321712536U CN220259070U CN 220259070 U CN220259070 U CN 220259070U CN 202321712536 U CN202321712536 U CN 202321712536U CN 220259070 U CN220259070 U CN 220259070U
- Authority
- CN
- China
- Prior art keywords
- treatment system
- ash treatment
- crystallization tank
- heat exchanger
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000003513 alkali Substances 0.000 title claims abstract description 21
- 238000002425 crystallisation Methods 0.000 claims abstract description 43
- 230000008025 crystallization Effects 0.000 claims abstract description 43
- 150000003839 salts Chemical class 0.000 claims description 35
- 239000007788 liquid Substances 0.000 claims description 19
- 230000007704 transition Effects 0.000 claims description 19
- 238000007599 discharging Methods 0.000 claims description 13
- 238000011010 flushing procedure Methods 0.000 claims description 12
- 239000007921 spray Substances 0.000 claims description 10
- 239000011521 glass Substances 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims 14
- 229910000029 sodium carbonate Inorganic materials 0.000 claims 7
- 235000017550 sodium carbonate Nutrition 0.000 claims 7
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 abstract description 26
- 235000011164 potassium chloride Nutrition 0.000 abstract description 13
- 239000001103 potassium chloride Substances 0.000 abstract description 13
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 abstract description 11
- 239000010446 mirabilite Substances 0.000 abstract description 11
- 238000003756 stirring Methods 0.000 abstract description 6
- 239000002002 slurry Substances 0.000 description 24
- 239000013078 crystal Substances 0.000 description 10
- 238000001816 cooling Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 6
- 230000006872 improvement Effects 0.000 description 6
- 239000003595 mist Substances 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000004537 pulping Methods 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000001953 recrystallisation Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the field of alkali ash treatment, and discloses a device which comprises a stirring tank, a crystallization tank, a centrifugal machine and an evaporator which are sequentially connected, wherein a recirculation unit is arranged on the crystallization tank, the recirculation unit comprises a circulation pipeline, a steam pipeline and a heat exchanger, the circulation pipeline penetrates through the heat exchanger, the steam pipeline is communicated with the top of the crystallization tank and the heat exchanger, and the steam pipeline is communicated with the circulation pipeline in the heat exchanger. So as to respectively recycle the potassium chloride and the mirabilite in the alkali ash.
Description
Technical Field
The utility model relates to the field of alkali ash treatment, in particular to an alkali ash treatment system.
Background
In order to save cost and protect environment, a pulping factory usually recovers alkali generated in the pulping process, black liquor is changed into white liquor after passing through an evaporation workshop, an alkali furnace combustion and a collotype workshop, and the white liquor is reused in a cooking process.
Wherein, the alkali ash is one of the combustion products of black liquor in the alkali furnace, and the alkali ash is rich in recyclable potassium chloride and mirabilite, and the potassium chloride and the mirabilite in the alkali ash are not extracted and recycled in the prior art, so that a great amount of resource waste is caused.
Disclosure of Invention
The utility model aims to provide an alkali ash treatment system which is used for respectively recovering potassium chloride and mirabilite in alkali ash.
In order to achieve the above purpose, the utility model adopts the following technical scheme: the alkali ash treatment system comprises a stirring tank, a crystallization tank, a centrifugal machine and an evaporator which are sequentially connected, wherein a recycling unit is arranged on the crystallization tank and comprises a circulating pipeline, a steam pipeline and a heat exchanger, the circulating pipeline penetrates through the heat exchanger, the steam pipeline is communicated with the top of the crystallization tank and the heat exchanger, and the steam pipeline is communicated with the circulating pipeline in the heat exchanger.
The beneficial effect of this scheme is:
1. and (3) stirring the alkali ash and water in a stirring tank to form slurry, introducing the slurry into a crystallization tank, and continuously introducing the slurry into a heat exchanger through a circulating pipeline for heat exchange and cooling. Since mirabilite is easy to crystallize and separate out at high temperature, and potassium chloride is easier to crystallize and separate out at low temperature, the precipitated crystals in the crystallization tank are mainly potassium chloride, the residual solution after the residual slurry passes through the centrifugal machine contains a large amount of mirabilite, and the residual slurry after the residual slurry passes through the centrifugal machine may also contain potassium chloride, so that recrystallization is needed. The solution containing a large amount of mirabilite enters an evaporator for evaporation and crystallization, so that the purpose of respectively recovering potassium chloride and mirabilite in the alkali ash is achieved.
2. The higher steam of temperature rises to the crystallization tank top, and the thick liquid in rethread steam conduit and the circulation pipeline merges, then cools down through the heat exchanger, gets back to in the crystallization tank to improve the efficiency to the thick liquid cooling, and then accelerate crystallization speed, improve recovery efficiency.
Preferably, as an improvement, the crystallization tank sequentially comprises an upper conical part, a cylinder body, a lower conical part and salt legs from top to bottom, a demister is arranged in the upper conical part, a flushing pipe is horizontally arranged at the upper end of the cylinder body, one end of the flushing pipe is communicated with the outside of the cylinder body, the other end of the flushing pipe is located under the demister, a vertical upward spray head is arranged at the other end of the flushing pipe, and the spraying range of the spray head covers the demister. So set up, there is the following effect:
1. if particles such as mist carried by steam enter a steam pipeline and a heat exchanger to easily cause blockage, scaling or corrosion to equipment, the mist eliminator is arranged in the scheme, when the steam passes through the mist eliminator, due to the inertia impact effect of the steam, the mist collides with the corrugated plate, and the aggregated liquid drops are separated from the surface of the corrugated plate when the gravity generated by the mist exceeds the resultant force of the lifting force of gas and the surface tension of the liquid, so that the blockage, scaling or corrosion to equipment is avoided.
2. After long-term use, the phenomenon that the steam makes the defroster appear hanging thick liquid or crystallization, arouses the defroster easily and blocks up to reduce defroster gas-liquid separation's effect, and in this scheme, spray defroster below through the wash pipe, and then avoid the defroster to block up.
Preferably, as an improvement, one end of the circulating pipeline is connected with the cylinder, and the other end of the circulating pipeline is connected with the lower cone. So set up, the thick liquid in the circulation pipeline is after the heat exchanger cooling, get back to in the crystallization tank again, because the temperature is lower when just getting back to in the one-level crystallization pipe, the thick liquid after the cooling sinks in the barrel, gradually with originally in the thick liquid intensive mixing of crystallization tank, and then accelerated the cooling of thick liquid in the crystallization tank.
Preferably, as an improvement, the salt leg is provided with a discharging port, a discharging port and three feeding ports, wherein the three feeding ports are an upper feeding port, a middle feeding port and a lower feeding port respectively. If only a single feed port is arranged, the slurry enters the crystallization tank at a high speed, and the slurry is unevenly dispersed, so that the cooling efficiency is affected; in this scheme, the thick liquids get into in the salt leg simultaneously through a plurality of feed inlets, collide the back with salt leg lateral wall and form the vortex, and the vortex upwards extends, and then makes the thick liquids equipartition in the crystallizer.
Preferably, as an improvement, the lower end of the lower cone is provided with a transition part, the transition part is inserted into the upper end of the salt leg, the upper feed inlet is horizontally arranged between the outer wall of the transition part and the inner wall of the salt leg, and the middle feed inlet, the discharge outlet and the lower feed inlet are all positioned on the axis of the salt leg. So set up, there is the following effect:
1. the slurry entering the circulation pipeline is continuously cooled, potassium chloride crystals are separated out and slide down to salt legs along the side wall of the lower cone 213, however, the side wall of the lower cone 213 is an inclined plane, part of crystals expand at low temperature and are combined with the side wall of the lower cone 213 and do not slide into the salt legs, after a long time, the surface of the side wall of the lower cone 213 is rough, more crystals cannot slide into the salt legs, and the crystals are difficult to collect; in the scheme, the transition part is arranged, and the slurry entering the salt leg from the upper feed inlet cannot directly enter the lower cone 213 upwards and cannot exchange temperature with the slurry in the lower cone 213, so that the cooling speed of the slurry between the salt leg and the transition part is slower, the slurry horizontally sprays out from the upper feed inlet to impact the outer side of the transition part, and the temperature of the transition part is higher than that of the lower cone under the contact of the slurry of the transition part and the transition part, so that the expansion effect is smaller and the crystal slides into the salt leg more easily when passing through the transition part; the lower cone part is also connected with the lower end of the circulating pipe, and the part connected with the lower end of the circulating pipe has larger fluidity, so that the problem that crystals are not easy to slide into salt legs is also not needed to be considered.
2. The slurry sprayed from the upper feed inlet collides with the transition part and flows in the annular space of the outer side wall of the transition part, so that the slurry in the salt legs is driven to form a vortex, and the middle feed inlet and the lower feed inlet are reversely and upwards flushed after downwards sprayed, and are accelerated to be flushed into the crystallization tank under the driving of rotation, so that the slurry is more uniformly distributed in the crystallization tank.
Preferably, as an improvement, the middle feed inlet is downward, and the middle feed inlet is positioned right above the discharge outlet. So set up, the thick liquids get into from the feed inlet and make constantly erode the discharge gate, prevent that the discharge gate from plugging up.
Preferably, as a modification, the discharging port is positioned at the bottom of the salt leg, the lower feed port is downward, and the lower feed port is positioned between the discharging port and the discharge port. So set up, the thick liquids gets into from lower feed inlet and makes and wash away the clean mouth of arranging constantly, prevents that the clean mouth from blocking up to take out the crystal that is located salt leg bottom.
Preferably, as an improvement, the crystallization tank is provided with a plurality of manholes, sight glass, liquid level gauge and pressure gauge. The manhole is arranged so as to enter the crystallization tank at any time for overhauling; the sight glass, level gauge and pressure gauge are set to monitor various parameters at all times to crystallize the slurry under optimal conditions.
Drawings
FIG. 1 is a schematic diagram of an embodiment;
FIG. 2 is a diagram showing the structure of a crystallization tank according to an embodiment.
Detailed Description
The following is a further detailed description of the embodiments:
reference numerals in the drawings of the specification include: stirred tank 1, crystallization tank 2, upper cone 211, cylinder 212, lower cone 213, transition 214, salt leg 215, mist eliminator 221, flush line 222, spray head 223, pressure gauge 231, level gauge 232, sight glass 233, vapor outlet 241, population 242, recycle inlet 243, recycle outlet 244, purge port 245, feed pipe 250, upper feed port 251, middle feed port 252, lower feed port 253, discharge line 260, discharge port 261, centrifuge 3, evaporator 4, recycle line 510, vapor line 520, heat exchanger 530.
Examples
An embodiment is substantially as shown in figure 1: the alkali ash treatment system comprises a stirring tank 1, a crystallization tank 2, a centrifugal machine 3 and an evaporator 4 which are connected in sequence.
As shown in fig. 2, the crystallization tank 2 sequentially comprises an upper cone 211, a cylinder 212, a lower cone 213 and salt legs 215 from top to bottom, a demister 221 is connected in the upper cone 211 in a bolt manner, a steam outlet 241 and two pressure gauges 231 are arranged on the upper left side of the upper cone 211, a population 242 and pressure gauges 231 are arranged on the upper right side of the upper cone 211, the demister 221 is a plate type demister, a flushing pipe 222 is welded horizontally on the upper inner end of the cylinder 212, the right end of the flushing pipe 222 is communicated with the outer side of the cylinder 212, the left end of the flushing pipe 222 is positioned right below the demister 221, a spray head 223 is integrally formed on the left end of the flushing pipe 222, the spray range of the spray head 223 covers the lower surface of a wave plate of the demister 221, a sight glass 233 and two liquid level gauges 232 are arranged on the left side of the cylinder 212, a recirculation inlet 243 is arranged on the upper right side of the cylinder 212, a recirculation outlet 244 is arranged on the lower right side of the lower cone 213, a vertically arranged cylindrical transition portion 214 is arranged on the lower end of the lower cone 213, the transition portion 214 is smaller than the diameter of the cylindrical salt legs 215, and the salt legs 215 are welded on the upper sides of the salt legs 215.
The salt leg 215 lower extreme is equipped with and arranges clean mouth 245, and salt leg 215 right side is equipped with discharging pipe 260, and discharging pipe 260 left end is discharge gate 261, and discharge gate 261 leans upward left, discharge gate 261 and centrifuge 3 intercommunication, salt leg 215 left side level are equipped with three inlet pipe 250, all are equipped with the branch pipe that is used for washing on discharging pipe 260 and the three inlet pipe 250, and the contained angle of the inlet pipe 250 of top and salt leg 215 lateral wall is less than 90, and three inlet pipe 250 right-hand member is from last to following in proper order: an upper inlet 251, a middle inlet 252 and a lower inlet 253, the upper inlet being located on the side wall of the salt leg 215, horizontally to the right and between the outer wall of the transition 214 and the inner wall of the salt leg 215; the middle and lower feed ports 252, 253 are all downward, and the middle, discharge, and lower feed ports 252, 261, 253 and purge ports 245 are vertically aligned from top to bottom and are all located on the center axis of the salt leg 215.
As shown in fig. 1, a recirculation unit is arranged on the crystallization tank 2, the recirculation unit comprises a circulation pipeline 510, a steam pipeline 520 and a heat exchanger 530, one end of the circulation pipeline 510 is connected with a recirculation inlet 243, the other end of the circulation pipeline 510 is connected with a recirculation outlet 244, the circulation pipeline 510 passes through the heat exchanger 530, the steam pipeline 520 is communicated with the steam outlet 241 and the heat exchanger 530, the steam pipeline 520 is communicated with the circulation pipeline 510 in the heat exchanger 530, and the solution separated by the centrifuge 3 is communicated with the circulation pipeline 510. The number of the crystallization tanks 2 can be adjusted according to actual demands, and the quantity of potassium chloride crystals can be increased by connecting a plurality of crystallization tanks 2 in series for multiple crystallization.
The specific implementation steps are as follows:
1. the alkali ash and water are stirred in the stirring tank 1 to form slurry, the slurry is introduced into the crystallization tank 2, and the slurry continuously enters the heat exchanger 530 through the circulating pipeline 510 for heat exchange and temperature reduction. The crystals precipitated in the crystallization tank 2 are mainly potassium chloride, the residual solution after the residual slurry passes through the centrifuge 3 contains a large amount of mirabilite, and the residual slurry after the residual slurry passes through the centrifuge 3 may also contain potassium chloride and returns to the crystallization tank 2 through the circulation pipeline 510 for recrystallization. The solution containing a large amount of mirabilite enters an evaporator 4 for evaporation and crystallization, so that the purpose of respectively recovering potassium chloride and mirabilite in the alkali ash is achieved.
2. The higher steam of temperature rises to crystallization tank 2 top, and rethread steam pipe 520 and circulation pipeline 510 interior thick liquid meet, then through heat exchanger 530 cooling, get back to in the crystallization tank 2 to improve the efficiency to the thick liquid cooling, and then accelerate crystallization speed, improve recovery efficiency.
The foregoing is merely exemplary of the present utility model, and specific technical solutions and/or features that are well known in the art have not been described in detail herein. It should be noted that, for those skilled in the art, several variations and modifications can be made without departing from the technical solution of the present utility model, and these should also be regarded as the protection scope of the present utility model, which does not affect the effect of the implementation of the present utility model and the practical applicability of the patent. The protection scope of the present application shall be subject to the content of the claims, and the description of the specific embodiments and the like in the specification can be used for explaining the content of the claims.
Claims (8)
1. The alkali ash treatment system is characterized in that: including agitator tank, crystallization tank, centrifuge and the evaporimeter that connect gradually, be equipped with the recycle unit on the crystallization tank, the recycle unit includes circulation pipeline, steam pipeline and heat exchanger, and circulation pipeline passes the heat exchanger, steam pipeline intercommunication crystallization tank top and heat exchanger, and steam pipeline and circulation pipeline communicate in the heat exchanger.
2. The soda ash treatment system of claim 1, wherein: the crystallization tank sequentially comprises an upper conical part, a cylinder body, a lower conical part and salt legs from top to bottom, a demister is arranged in the upper conical part, a flushing pipe is horizontally arranged at the upper end of the cylinder body, one end of the flushing pipe is communicated with the outside of the cylinder body, the other end of the flushing pipe is located under the demister, a vertical upward spray head is arranged at the other end of the flushing pipe, and the spraying range of the spray head covers the demister.
3. The soda ash treatment system of claim 2, wherein: one end of the circulating pipeline is connected with the cylinder body, and the other end of the circulating pipeline is connected with the lower cone part.
4. The soda ash treatment system of claim 3, wherein: the salt leg is provided with a clean discharging port, a discharging port and three feeding ports, wherein the three feeding ports are an upper feeding port, a middle feeding port and a lower feeding port respectively.
5. The soda ash treatment system of claim 4, wherein: the lower end of the lower cone is provided with a transition part, the transition part is inserted into the upper end of the salt leg, the upper feed inlet is horizontally arranged between the outer wall of the transition part and the inner wall of the salt leg, and the middle feed inlet, the discharge outlet and the lower feed inlet are all positioned on the axis of the salt leg.
6. The soda ash treatment system of claim 5, wherein: the middle feeding hole faces downwards, and the middle feeding hole is positioned right above the discharging hole.
7. The soda ash treatment system of claim 6, wherein: the discharging port is positioned at the bottom of the salt leg, the lower feeding port is downward, and the lower feeding port is positioned between the discharging port and the discharging port.
8. The soda ash treatment system of claim 1, wherein: the crystallization tank is provided with a plurality of manholes, sight glass, liquid level gauge and pressure gauge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321712536.7U CN220259070U (en) | 2023-06-30 | 2023-06-30 | Alkali ash treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321712536.7U CN220259070U (en) | 2023-06-30 | 2023-06-30 | Alkali ash treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220259070U true CN220259070U (en) | 2023-12-29 |
Family
ID=89318519
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321712536.7U Active CN220259070U (en) | 2023-06-30 | 2023-06-30 | Alkali ash treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220259070U (en) |
-
2023
- 2023-06-30 CN CN202321712536.7U patent/CN220259070U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN220259070U (en) | Alkali ash treatment system | |
| CN116637923A (en) | Alkali ash treatment system | |
| CN210385238U (en) | Foam type pollution prevention and control equipment | |
| CN106397104A (en) | Carbon tetrafluoride purification system with nitrogen recycling function | |
| CN101766942B (en) | Trichlorosilane de-dusting device and de-dusting process | |
| CN208799809U (en) | A kind of mechanization tar ammonia clarification slot device | |
| CN211420081U (en) | Condensate tank capable of removing impurities and separating water | |
| US6287415B1 (en) | Arrangement in soda recovery boiler for removing melts for maintenance | |
| CN207738708U (en) | A kind of coal gas refrigerated separation device | |
| CN207294234U (en) | A kind of crystallization treatment device recycled based on trade effluent | |
| CN209128047U (en) | A kind of saltcake hot melting recycling utilizes system | |
| CN202876423U (en) | Acid bath flash evaporation and crystallization device | |
| CN201817277U (en) | Carclazyte bed sewage disposal waste liquor recovery equipment | |
| CN201598320U (en) | Gold-containing copper pyrite reaction device | |
| CN216703880U (en) | Evaporation secondary steam washing device | |
| CN105126577A (en) | Acetylene gas purifying device for purifying acetylene and desorbing waste sodium hypochlorite | |
| CN201620063U (en) | Reactor treating cyanate waste water or ore slurry containing cyanogen and/or sulfur | |
| CN107744791A (en) | A kind of spiral agitating type tail gas desulfurization reactor | |
| CN219111287U (en) | Desulfurizing tower | |
| CN218501285U (en) | Gravity type heat exchange and concentration integrated machine | |
| CN216799315U (en) | Online slag discharging device of tail gas washing tower | |
| CN212854744U (en) | R134a finished product alkali washing separator | |
| CN210393780U (en) | Gas-liquid separator for evaporative crystallization system | |
| CN211801665U (en) | Automatic water pumping, water supplementing and flushing flotation machine | |
| CN211112228U (en) | Copper sulfate crystal recycling machine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |