CN219652780U - High-salt wastewater recycling treatment system for PBO fiber production process - Google Patents
High-salt wastewater recycling treatment system for PBO fiber production process Download PDFInfo
- Publication number
- CN219652780U CN219652780U CN202321186301.9U CN202321186301U CN219652780U CN 219652780 U CN219652780 U CN 219652780U CN 202321186301 U CN202321186301 U CN 202321186301U CN 219652780 U CN219652780 U CN 219652780U
- Authority
- CN
- China
- Prior art keywords
- alkali liquor
- crystallization tank
- spray tower
- production process
- salt wastewater
- 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
- 239000002351 wastewater Substances 0.000 title claims abstract description 47
- 238000004064 recycling Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000011282 treatment Methods 0.000 title claims abstract description 26
- 230000008569 process Effects 0.000 title claims abstract description 24
- 238000007380 fibre production Methods 0.000 title claims abstract description 9
- 238000002425 crystallisation Methods 0.000 claims abstract description 66
- 230000008025 crystallization Effects 0.000 claims abstract description 65
- 239000003513 alkali Substances 0.000 claims abstract description 64
- 239000007921 spray Substances 0.000 claims abstract description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000003860 storage Methods 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims description 71
- 238000005406 washing Methods 0.000 claims description 66
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 239000000835 fiber Substances 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims description 8
- 150000003839 salts Chemical class 0.000 claims description 5
- 230000009467 reduction Effects 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 97
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 61
- 239000011780 sodium chloride Substances 0.000 description 48
- 239000013078 crystal Substances 0.000 description 23
- 230000000694 effects Effects 0.000 description 23
- 239000000243 solution Substances 0.000 description 19
- 239000007787 solid Substances 0.000 description 14
- 239000007789 gas Substances 0.000 description 11
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 9
- 238000010521 absorption reaction Methods 0.000 description 9
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 7
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 7
- 238000005507 spraying Methods 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- KKEYFWRCBNTPAC-UHFFFAOYSA-N terephthalic acid group Chemical group C(C1=CC=C(C(=O)O)C=C1)(=O)O KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- 238000004090 dissolution Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000006210 lotion Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910001415 sodium ion Inorganic materials 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- GAKFXHZPQGSWHQ-UHFFFAOYSA-N 4,6-diaminobenzene-1,3-diol;hydrochloride Chemical compound Cl.NC1=CC(N)=C(O)C=C1O GAKFXHZPQGSWHQ-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000011229 interlayer Substances 0.000 description 1
- 239000010410 layer Substances 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007785 strong electrolyte Substances 0.000 description 1
Abstract
The utility model discloses a high-salt wastewater circulation treatment system in a PBO fiber production process, which comprises an alkali liquor spray tower, a crystallization tank and an alkali liquor storage tank which are sequentially arranged and communicated from top to bottom, wherein a reversing valve is arranged at a water outlet at the lower end of the alkali liquor spray tower, two outlets of the reversing valve are respectively connected with the crystallization tank and the alkali liquor storage tank, and a water outlet of the alkali liquor storage tank is connected with a water inlet of the alkali liquor spray tower through a circulating pump. The utility model has simple structure, and utilizes the reversing valve to carry out diversion treatment and recycling on the high-salt wastewater with different concentrations generated in the alkali liquor spray tower, thereby playing the roles of energy conservation and emission reduction.
Description
Technical Field
The utility model relates to a high-salt wastewater recycling treatment system in a PBO fiber production process, in particular to a wastewater recycling treatment system, and belongs to the technical field of water treatment.
Background
The main process route adopted by the PBO fiber at present is terephthalic acid method: the method mainly comprises the step of carrying out polymerization reaction on monomer 4, 6-diaminoresorcinol hydrochloride and terephthalic acid, so that a large amount of byproduct hydrogen chloride gas is generated. Most of the hydrogen chloride gas is converted into high-concentration hydrochloric acid solution for recycling, and the small part of the hydrogen chloride tail gas is treated by means of alkali liquor spraying absorption and the like, in the process, the alkali washing liquid gradually forms high-concentration sodium chloride solution (namely high-salt wastewater refers to sodium chloride solution with concentration higher than 25 percent) after the alkali washing liquid circularly absorbs the hydrogen chloride; if the untreated high-concentration sodium chloride solution is recycled as alkaline washing liquid, not only is the tail gas treatment effect poor, but also sodium chloride crystals are separated out to block a pipeline in the using process, so that the alkaline washing spray absorption system cannot normally operate; if the high-concentration sodium chloride solution is directly discharged into a waste water treatment system of a company, the workload of waste water treatment can be greatly increased, and a large amount of water resources can be wasted. To solve the above-mentioned problem in the recycling of high concentration sodium chloride solution, generally, an evaporation crystallization mode is adopted, and condensed water formed by collecting water vapor for recycling is generally used, and the process generally includes: the steps of pretreatment, concentration, evaporation and crystallization are complex, and the solution is easy to cause high energy consumption and high cost in the evaporation and condensation processes.
In the prior art, high temperature is generally adopted to evaporate water serving as a solvent in high-salt wastewater so as to separate out salt. The utility model patent with publication number of CN115477431A discloses a low-cost high-salt wastewater reduction and resource utilization method, which is to convert chloride into a product required by production by electrochemical reaction; the utility model patent with publication number of CN207094646U discloses a novel quenching tower system capable of being cooled by high-salt wastewater, which is characterized in that high-salt wastewater is adopted to cool high-temperature flue gas so as to quickly evaporate water in the high-salt wastewater, and salt in the high-salt wastewater is analyzed; the utility model patent with publication number of CN211311181U discloses a high-salt wastewater recycling device containing sodium chloride and sodium sulfate, which utilizes a first crystallizer and a second crystallizer to separate and crystallize sodium chloride and sodium sulfate, a reaction box can be used for adding medicine to remove sulfate radical, and recycled water and sodium salt are recycled through multiple recycling treatments. In view of the above, the prior art does not provide a solution to the above-mentioned problems.
Disclosure of Invention
The utility model aims to provide a high-salt wastewater circulation treatment system in a PBO fiber production process, which is characterized in that high-salt wastewater with a pH value lower than a set value or a concentration higher than a set value is subjected to split treatment through a reversing valve, so that the high-salt wastewater discharged from an alkali liquor spray tower is conveyed to an external crystallization tank, sodium chloride crystals are separated out after the high-salt wastewater conveyed to the crystallization tank is mixed with added solid sodium hydroxide by utilizing the homoionic effect under a constant temperature state, alkaline washing liquid with a pH value of 14 at maximum is conveyed to an alkaline washing liquid storage tank, and then the alkaline washing liquid is conveyed to the alkali liquor spray tower again through a circulating pump for spraying, thereby realizing the purposes of separating out sodium chloride crystals while recycling the high-salt wastewater to prepare alkaline washing liquid, avoiding the waste of corresponding water resources, and solving the problem that the alkaline washing absorption system cannot normally operate due to the separation of sodium chloride crystals in the recycling process.
The utility model is realized by the following technical scheme:
a high-salt wastewater recycling treatment system in the production process of PBO fibers is characterized in that: the device comprises an alkali liquor spray tower, a crystallization tank and an alkali liquor storage tank which are sequentially arranged from top to bottom and are communicated, a reversing valve is arranged at a water outlet of the alkali liquor spray tower, two outlets of the reversing valve are respectively connected with the crystallization tank and the alkali liquor storage tank, and a water outlet of the alkali liquor storage tank is connected with a water inlet of the alkali liquor spray tower through a circulating pump.
And a stirring device is arranged in the crystallization tank.
The crystallization tank is provided with a constant temperature device.
The crystallization tank is provided with a feeding device.
And a stop valve is also arranged between the crystallization tank and the alkaline washing liquid storage tank.
And a pH value measuring device and a concentration detector are also arranged between the reversing valve and the alkali liquor spray tower.
Compared with the prior art, the utility model has the following advantages:
(1) According to the utility model, the reversing valve arranged at the water outlet of the alkali liquor spray tower is used for conveying the high-salt wastewater with the pH value lower than the set pH value or higher than the set concentration into the externally connected crystallization tank, and the same ion effect is generated between the high-salt wastewater and the added solid sodium hydroxide in the crystallization tank, so that sodium chloride crystals are separated out, alkali washing liquor with the pH value set (the highest pH value of 14) is prepared, and the alkali washing liquor enters the alkali washing spray absorption system again, thereby achieving the purposes of recycling the high-salt wastewater and reducing the circulating water, and simultaneously solving the problem that the alkali washing spray absorption system cannot normally operate due to the fact that sodium chloride crystals are separated out in the recycling process of the high-salt wastewater. In the process of recycling the high-salt wastewater, the purpose of preparing the alkaline washing liquid with the set pH value (highest pH value of 14) can be achieved without completely precipitating sodium chloride in the high-salt wastewater, so that the sodium chloride in the high-salt wastewater is not required to be completely precipitated in an evaporation crystallization mode, the waste of energy sources required by the high-salt wastewater treatment in the prior art is avoided, and the effects of energy conservation and emission reduction are achieved.
(2) The utility model sets a constant temperature device through the crystallization tank, and has the following functions: the method has the advantages that the problem that the solubility of sodium hydroxide and sodium chloride is increased due to the influence of heat generated in the dissolution process of sodium hydroxide solids to the homoionic effect is avoided, the quantity of precipitated sodium chloride crystals is reduced, the sodium ion content in the recycled alkaline washing liquid is increased, so that when the alkaline washing liquid reacts with hydrogen chloride gas in the subsequent use, the concentration of sodium chloride in the alkaline washing liquid is rapidly increased, the sodium chloride crystals cannot be timely discharged or diluted, and finally the precipitated sodium chloride crystals block a pipeline, so that the condition that the alkaline washing spray absorption system cannot normally operate occurs.
(3) According to the utility model, the stirring device is arranged in the crystallization tank, so that the homoionic effect can be enhanced, the effects of accelerating the dissolution of solid sodium hydroxide and the precipitation of sodium chloride crystals are achieved, the concentration of sodium chloride in the solution is reduced, and the alkaline cleaning solution required by the tail gas treatment generated in the production process of PBO fibers is rapidly prepared.
(4) According to the utility model, the charging device is arranged in the crystallization tank, so that enough sodium hydroxide can be used when homoionic effect occurs in the crystallization tank.
(5) According to the utility model, the stop valve is arranged between the crystallization tank and the alkaline washing liquid storage tank, so that the alkaline washing liquid is prevented from being discharged into the alkaline washing liquid storage tank before the pH value of the alkaline liquid prepared in the crystallization tank is less than 14, and the effects of improving the treatment efficiency of high-salt wastewater, reducing the treatment times and saving energy are achieved.
(6) According to the utility model, the pH value measuring device and the concentration detector are arranged between the reversing valve and the alkali liquor spray tower, so that the high-salt wastewater lower than the set pH value and higher than the set concentration can be timely conveyed to the externally connected crystallization tank, sodium chloride crystals are separated out through the homoionic effect with sodium hydroxide, and the purpose of recycling the alkali washing liquor with the set pH value is achieved, namely, the recycling and effective utilization of the high-salt wastewater is realized, and the recycling and absorbing effect of alkali liquor on the hydrogen chloride gas is ensured.
In summary, the utility model has simple structure, utilizes the reversing valve to carry out diversion treatment and recycling on the high-salt wastewater with different concentrations generated in the alkali liquor spray tower, and utilizes the homoionic effect to prepare the high-salt wastewater into the alkali liquor which can be used for tail gas treatment generated in the PBO fiber production process, thereby not only realizing the reutilization of the high-salt wastewater, but also solving the problem that the sodium chloride salt crystal is separated out in the recycling process of the high-salt wastewater in the prior art to block the pipeline, so that the alkali liquor spray absorption system cannot normally operate, avoiding the high energy consumption of treating the high-salt wastewater in a (high-temperature) evaporation crystallization mode, and playing the roles of energy conservation and emission reduction.
Drawings
FIG. 1 is a schematic illustration of a high salt wastewater recycling system in the PBO fiber production process;
wherein, 1-alkali liquor spray tower, 2-crystallization tank, 3-alkali washing liquid storage tank, 4-reversing valve, 5-circulating pump, 6-agitating unit, 7-feeding device, 8-stop valve, 9-pH value measuring device.
Detailed Description
The present utility model will be described in further detail with reference to examples, but embodiments of the present utility model are not limited thereto.
Examples:
as shown in fig. 1, this embodiment provides a high-salt wastewater recycling treatment system in PBO fiber production process, which is characterized in that: the device comprises an alkali liquor spray tower 1, a crystallization tank 2 and an alkali liquor storage tank 3 which are sequentially arranged and communicated from top to bottom, wherein a reversing valve 4 is arranged at a water outlet at the lower end of the alkali liquor spray tower 1, two outlets of the reversing valve 4 are respectively connected with the crystallization tank 2 and the alkali liquor storage tank 3, and a water outlet of the alkali liquor storage tank 3 is connected with a water inlet of the alkali liquor spray tower 1 through a conveying pipe provided with a circulating pump 5.
Before use, a sufficient amount of solid sodium hydroxide is required to be put into the crystallization tank 2, and in an initial state, the output direction of the reversing valve is from the alkali liquor spray tower 1 to the alkali liquor storage tank 3, and the circulating pump 5 is in a closed state; the pH of the alkaline washing solution in the alkaline washing solution storage tank 3 was 14.
When in use, the circulating pump 5 is started, the tail gas of hydrogen chloride conveyed into the alkali liquor spray tower 1 and the sprayed atomized alkali liquor undergo neutralization reaction, the alkali liquor (the pH value is reduced) after being used is discharged from the lower end of the alkali liquor spray tower 1 under the action of gravity, the output direction of the reversing valve 4 is switched according to the different pH values of the discharged alkali liquor, and the following use states are presented:
use state 1: when the pH value of the alkaline washing liquid discharged by the alkaline liquid spray tower 1 is detected to be higher than 9, the concentration of sodium chloride in the alkaline washing liquid is lower than 25%, the alkaline washing liquid is injected into the alkaline washing liquid storage tank 3 below the alkaline liquid spray tower 1 through the reversing valve 4 and then is conveyed to the water inlet of the alkaline liquid spray tower 1 for spraying again under the action of the circulating pump 5, so that the recycling of the alkaline washing liquid is realized. A first circulation path is available: alkali liquor spray tower 1-alkali washing liquid storage tank 3-alkali liquor spray tower 1. In the continuous recycling process, the concentration of sodium chloride in the alkaline washing liquid gradually rises until the recycling of the use state 1 is finished when the pH value of the sodium chloride in the alkaline washing liquid is lower than 9 or the concentration of the sodium chloride is higher than 25%.
Use state 2: when the pH value of the alkaline washing liquid discharged from the alkaline liquid spray tower 1 is detected to be lower than 9, when the concentration of sodium chloride in the alkaline washing liquid is lower than 25%, the alkaline washing liquid is conveyed into the crystallization tank 2 through the reversing valve 4, a proper amount of solid sodium hydroxide is added into the crystallization tank 2 to be gradually dissolved in the alkaline washing liquid until the pH value of the alkaline washing liquid reaches 14, no sodium chloride crystal is separated out or a very small amount of sodium chloride crystal is separated out during the period, a liquid discharge switch at the bottom of the crystallization tank 2 is opened, the prepared alkaline washing liquid flows into an alkaline washing liquid storage tank 3 arranged below the crystallization tank 2 under the action of gravity and is conveyed to a water inlet of the alkaline liquid spray tower 1 through the circulating pump 5 for spray use again, and thus the recycling of the alkaline washing liquid is realized.
Use state 3: when the concentration of sodium chloride in the alkaline washing liquid discharged from the alkaline liquid spray tower 1 is detected to be higher than 25%, the pH value of the alkaline washing liquid is lower than 14, the alkaline washing liquid is conveyed into the crystallization tank 2 through the reversing valve 4, a proper amount of solid sodium hydroxide is added into the crystallization tank 2, sodium chloride and sodium hydroxide are gradually separated out due to the homoionic effect, the pH value of the alkaline washing liquid in the tank is regulated to be 14, a liquid discharge switch at the bottom of the crystallization tank 2 is opened, the prepared alkaline washing liquid flows into the alkaline washing liquid storage tank 3 arranged below the crystallization tank 2 under the action of gravity and is conveyed to the water inlet of the alkaline liquid spray tower 1 through the circulating pump 5 for spray use again, and thus the recycling of the alkaline washing liquid is realized.
Homoionic effect of sodium chloride and sodium hydroxide:
because the solid sodium hydroxide is exothermic when dissolved, the temperature in the crystallization tank 2 should be kept at 20-30 ℃ in order to realize better effect of the homoionic effect and reproducibility of the high-salt wastewater circulation process, wherein the optimal temperature is 20 ℃. Under the constant temperature condition, when the concentration of sodium chloride in the crystallization tank 2 is higher than 25%, the pH value of the alkaline washing liquid is lower than 14, the alkaline washing liquid and solid sodium hydroxide in the added crystallization tank 2 have the same ion effect to separate sodium chloride crystals, and meanwhile, the sodium hydroxide is continuously dissolved to prepare alkaline washing liquid with a set pH value (highest pH value of 14), and the alkaline washing liquid is recycled. In the circulation control process, sodium chloride crystals are separated out to the greatest extent in the crystallization tank 2, so that sodium chloride in alkaline washing liquid for circulation spraying can not reach a saturated state all the time, and the condition that the alkaline washing liquid is separated out in the circulation use process to cause that the sodium chloride crystals block a pipeline, and the alkaline washing spraying absorption system cannot normally operate is avoided.
When not in use, the tail gas is stopped from being conveyed, and the circulating pump 5 is turned off.
Selection of crystallization tank 2 in this example: in order to avoid that sodium chloride crystals in the crystallization tank 2 are accumulated to influence the circulation preparation of alkaline washing liquid, the selected crystallization tank 2 is optimal to have a solid-liquid separation function, otherwise, a solid-liquid separation device such as a solid-liquid separator, a filter screen and the like is additionally arranged at a liquid outlet of the crystallization tank 2, and the situation that precipitated sodium chloride crystals are discharged along with the alkaline washing liquid to cause pipeline blockage can be avoided.
In the present embodiment, the reversing valve 4 is used, but in practical use, the reversing valve 4 is not essential. Only by the alkali lye spray column 1, crystallization tank 2 and the alkali wash liquid holding vessel 3 that set gradually from top to bottom and communicate, be connected the alkali lye spray column 1 water inlet with alkali wash liquid holding vessel 3 delivery port through circulating pump 5 again, can realize high salt waste water cyclic utilization, and can make the pH value of the alkali lotion of every turn circulation use be 14, also can play and avoid alkali lotion to precipitate sodium chloride crystal in the circulation use and stop up the pipeline, cause the unable normal operating condition emergence of alkali wash spray absorption system. But the embodiment has the advantages of higher operation efficiency and lower energy consumption, and is a better choice.
Further, in order to avoid that the quantity of sodium ions in the saturated solution increases due to the homoionic effect when the temperature is too high, the effect of the subsequent tail gas spraying treatment is affected, even if the alkali washing liquid is precipitated when not conveyed to the crystallization tank 2 due to temperature change, and the conveying pipeline is blocked, as shown in fig. 1, the crystallization tank 2 is provided with a constant temperature device, and the constant temperature device can adopt a constant temperature layer with chilled water or chilled water in an interlayer on the crystallization tank 2, and can also adopt a thermostat with a heating and refrigerating module, so long as the device capable of keeping the temperature in the crystallization tank 2 constant can be applied to the embodiment.
Further, in order to accelerate the dissolution of solid sodium hydroxide and enhance the homoionic effect, so that sodium chloride crystals are precipitated as much as possible, and the pH value of the alkaline washing liquid reaches 14 as soon as possible, as shown in FIG. 1, a stirring device 6 is arranged in the crystallization tank 2. There are various driving modes of the stirring device 6, and manual stirring and mechanical stirring can be adopted. In the actual production process, a stirrer driven by a servo motor is used, so that the condensation nuclei are more uniformly distributed in the solution, the growth speed of sodium chloride crystals precipitated in the crystallization tank 2 is increased, the purity and shape of the crystals are improved, the rotating speed of the stirrer is set to be 10-50 rpm, the optimal rotating speed is 20 rpm, and the stirring diameter is not smaller than half the inner diameter of the crystallization tank 2. In practical use, the device with stirring function can be applied to the embodiment.
Furthermore, in order to ensure sufficient solid sodium hydroxide required by the homoionic effect, a feeding device 7 is arranged on the crystallization tank 2, and a manual feeding device can be adopted, for example, one or more material boxes with movable drawing plates at the bottoms are arranged on the crystallization tank 2, the drawing plates at the bottoms of the material boxes need to be directly drawn outwards by adding the solid sodium hydroxide, and the feeding quantity can be determined by controlling the drawing distance of the drawing plates; mechanical feeding devices and automatic feeding devices can also be arranged. In practical use, the present embodiment can be applied as long as solid sodium hydroxide can be fed into the crystallization tank 2.
Further, in order to ensure that the pH of the alkaline washing liquid prepared in the crystallization tank 2 reaches 14 before being discharged into the alkaline washing liquid storage tank 3, a stop valve 8 is provided between the crystallization tank 2 and the alkaline washing liquid storage tank 3. The stop valve 8 of the present embodiment may be used in various types, such as a straight-through stop valve, an angle stop valve, a plunger stop valve, etc., and the stop valve used in the actual production process is a straight-through stop valve. Of course, valves that allow passage of alkaline wash solution when needed can be used in this embodiment.
Furthermore, in order to ensure that the sodium chloride solution with the concentration higher than 25% can be timely conveyed to the externally connected crystallization tank 2, a pH value measuring device 9 is further arranged between the reversing valve 4 and the alkali liquor spray tower 1. The device for measuring the pH value is various and can be manually controlled or automatically controlled. The pH measuring device 9 used in this embodiment is a pH measuring device, and the sensor, that is, the electrode portion, may be configured with different electrodes (e.g., high temperature, strong acid, strong base, sanitary) according to different application occasions, and in the actual production process, the sensor may be used in a strong base environment. The apparatus for measuring pH can be used in this embodiment as long as it can measure pH.
In addition, in the practical application process, in order to save manpower, an electric control reversing valve can be adopted to be matched with an automatically controlled pH value measuring device 9, the pH value measuring device 9 and the electric control reversing valve are controlled to be matched with each other to work through a control program, and the conveying direction of alkaline washing liquid discharged by the alkaline liquid spray tower 1 is automatically switched according to the measured pH value.
The embodiment not only can be used for the high-salt wastewater recycling treatment, but also can be used for other wastewater treatment and recycling by cooling crystallization or homoionic effect crystallization, and when the embodiment is used for other homoionic effects, only the solid sodium oxychloride added into the crystallization tank 2 is replaced by the required strong electrolyte.
In this embodiment, the switching of the conveying direction of the reversing valve is controlled by testing the pH value, and the switching of the conveying direction of the reversing valve is also controlled by testing the concentration of sodium chloride in the solution.
The high-concentration sodium chloride solution and the sodium chloride solution with the concentration higher than 25% in the embodiment, wherein the concentration of sodium chloride in the alkaline washing solution is higher than 25%, refer to high-salt wastewater.
The foregoing description is only a preferred embodiment of the present utility model, and is not intended to limit the present utility model in any way, and any simple modification, equivalent variation, etc. of the above embodiment according to the technical matter of the present utility model fall within the scope of the present utility model.
Claims (6)
1. A high-salt wastewater recycling treatment system in the production process of PBO fibers is characterized in that: the device comprises an alkali liquor spray tower (1), a crystallization tank (2) and an alkali liquor storage tank (3) which are sequentially arranged and communicated from top to bottom, wherein a reversing valve (4) is arranged at a water outlet at the lower end of the alkali liquor spray tower (1), two outlets of the reversing valve (4) are respectively connected with the crystallization tank (2) and an inlet of the alkali liquor storage tank (3), and a water outlet of the alkali liquor storage tank (3) is connected with a water inlet of the alkali liquor spray tower (1) through a circulating pump (5).
2. The high-salinity wastewater recycling treatment system for the production process of the PBO fiber according to claim 1, wherein: the crystallization tank (2) is provided with a constant temperature device.
3. The high-salinity wastewater recycling treatment system for the production process of the PBO fiber according to claim 1, wherein: the crystallization tank (2) is provided with a stirring device (6).
4. The high-salinity wastewater recycling treatment system for the production process of the PBO fiber according to claim 1, wherein: the crystallization tank (2) is provided with a feeding device (7).
5. The high-salinity wastewater recycling treatment system for the production process of the PBO fiber according to claim 1, wherein: a stop valve (8) is also arranged between the crystallization tank (2) and the alkaline washing liquid storage tank (3).
6. The PBO fiber production process high salt wastewater recycling treatment system according to any one of claims 1 to 5, wherein: a pH value measuring device (9) and a concentration detector are also arranged between the reversing valve (4) and the alkali liquor spray tower (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321186301.9U CN219652780U (en) | 2023-05-17 | 2023-05-17 | High-salt wastewater recycling treatment system for PBO fiber production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321186301.9U CN219652780U (en) | 2023-05-17 | 2023-05-17 | High-salt wastewater recycling treatment system for PBO fiber production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219652780U true CN219652780U (en) | 2023-09-08 |
Family
ID=87853728
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321186301.9U Active CN219652780U (en) | 2023-05-17 | 2023-05-17 | High-salt wastewater recycling treatment system for PBO fiber production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219652780U (en) |
-
2023
- 2023-05-17 CN CN202321186301.9U patent/CN219652780U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102030386B (en) | Efficient energy-saving coupling stripping deamination equipment and method | |
| CN101280476B (en) | Recovery method for NMMO solvent in fibre production by solvent method | |
| CN105671587B (en) | A kind of method and its device for preparing methionine and reclaiming accessory substance carbon dioxide | |
| WO2022198855A1 (en) | System and method for efficiently preparing taurine | |
| CN110304640A (en) | A kind of sodium bicarbonate production method | |
| CN205710248U (en) | A kind of zero-discharge treatment system of dyeing waste water | |
| CN206444229U (en) | MVR evaporation and crystallization systems and industrial alkali waste liquid treating system | |
| CN102275955B (en) | Method for preparing mirabilite by using sulfonated end gas absorption solution, and apparatus thereof | |
| CN103736383B (en) | Soda ash flue gas desulfurization technique and flue gas desulphurization system | |
| CN219652780U (en) | High-salt wastewater recycling treatment system for PBO fiber production process | |
| CN111111416A (en) | A novel gas washing system for landfill leachate handles | |
| CN102086159A (en) | Glutamic acid extraction method | |
| CN210751328U (en) | Aminoacetic acid by-product ammonium chloride recovery device | |
| CN216236063U (en) | Sodium bromide apparatus for producing | |
| CN111439814A (en) | Desulfurization wastewater concentration and reduction treatment system and method based on non-softening and directional driving electrodialysis technology | |
| CN110550609A (en) | Method for recovering sulfuric acid from concentrated acidic wastewater | |
| CN216513307U (en) | Ferric phosphate effluent disposal system | |
| CN216737932U (en) | Electrolytic waste residue and fluorine-containing wastewater treatment device for electrolytic fluorine production process | |
| CN209307138U (en) | A kind of Desulphurization for Coal-fired Power Plant Waste water concentrating sofening treatment device | |
| CN214270569U (en) | Zero-emission treatment system for evaporation mother liquor | |
| CN212246660U (en) | Device for extracting high-purity sodium acrylate or sodium methacrylate from UV monomer production wastewater | |
| CN211987966U (en) | A novel gas washing system for landfill leachate handles | |
| CN112250131A (en) | Ammonia nitrogen wastewater treatment method | |
| CN219792515U (en) | Green co-production device of battery level sodium carbonate and fused salt level sodium nitrate | |
| CN208166612U (en) | The device of wastewater minimisation processing is carried out using low-temperature flue gas waste heat |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |