CN1289725A - Process for pre-treating waste liquid of p-benzoic acid by complexing and extraction - Google Patents
Process for pre-treating waste liquid of p-benzoic acid by complexing and extraction Download PDFInfo
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Abstract
A process for pre-treating waste solution of benzoic acid includes such steps as preparing extractant from complexing agent, cosolvent and diluent, multi-stage extracting at ordinary-temp until its chemical oxygen consumption value conforms with discharge standard, and sampling analysis of COD cr, pH value and water-phase hydrogen ion concentration at each stage. It can be used to recover phenol, phenylamine and organic acid.
Description
The present invention relates to a kind of complexometric extraction para Toluic Acid pretreatment method for wastewater of using, belong to environmental technology field.
At present, phenylformic acid mainly adopts the production of toluene liquid-phase air oxidation.In the production technique, being catalyzer with cobalt salt or manganese salt, is 165 ℃ in temperature, and when pressure was 0.88Mpa, toluene generation oxidizing reaction generated phenylformic acid and by product.With acetate is under the condition of solvent, and by product mainly contains phenyl aldehyde, phenylcarbinol, methyl phenyl ketone, methyl benzoate, phenylmethyl acetate, biphenyl etc.The waste water that produces in this art production process, its outward appearance is little yellow, transparent, and the pH value is between 1.8～2.1, and hydrogen ion concentration is about 0.5～0.8molL in the water
-1, being stronger acidity, chemical oxygen demand is (hereinafter to be referred as COD
Cr) be about 20,000-100,000.Through gas chromatography-mass spectrometry analysis, the main component of waste water is eight kinds of organism such as phenylformic acid, acetate, toluene, phenyl aldehyde, phenylcarbinol, methyl phenyl ketone, methyl benzoate, phenylmethyl acetate, wherein based on phenylformic acid and acetate, six kinds of component contents such as toluene, phenyl aldehyde, phenylcarbinol, methyl phenyl ketone, methyl benzoate, phenylmethyl acetate seldom.According to the standard GB 8978-88 regulation that organic wastewater is handled, secondary discharge standard is COD
CrBe no more than 200mgL
-1Because this kind organic waste water belongs to the bio-refractory system, directly adopts the biochemical degradation method to handle, CODCr value and pH value are too high, and the waste water complicated component, must reduce solute concentration and COD earlier through pre-treatment
CrValue, and then carry out biochemical degradation or the terminal processing of other secondary, with qualified discharge.
The objective of the invention is to propose a kind of complexometric extraction para Toluic Acid pretreatment method for wastewater of using, reclaim the valuable product Sodium Benzoate, simultaneously, reduce the COD of waste water
CrValue and acidity make its requirement of satisfying biochemical processing process or other secondary method of edge treatment, realize utilization of wastewater resource and qualified discharge.
Typical process flow of the present invention is, waste water is after multi-stage counter current extraction purifies, main component such as phenylformic acid and acetic acid is in the solvent phase enrichment in the waste water, extraction agent recycles behind alkali liquid regeneration, the alkali lye load saturation is after condensing crystal can get the Sodium Benzoate head product, and every index of residual waste water satisfies the requirement of biochemical processing process or other secondary method of edge treatment.
Of the present invention with complexometric extraction para Toluic Acid pretreatment method for wastewater, comprise following each step:
1, preparation extraction agent, its composition is complexing agent+solubility promoter+thinner, and the volume proportion of extraction agent is that complexing agent accounts for 10%～100%, and solubility promoter accounts for 0～40%, and all the other are thinner, complexing agent wherein is tributyl phosphate, trialkyl (C
8～C
10) amine or trialkyl (C
8～C
10) any in the phosphine oxide, solubility promoter is a n-Octanol, thinner is a kerosene, and complexing agent, solubility promoter, thinner are mixed at normal temperatures by above-mentioned volume ratio, and is standby;
2, the mixed solvent with above-mentioned preparation is an extraction agent, at normal temperatures, para Toluic Acid's waste water carries out multi-stage solvent extraction, and in extracting operation, volume is in a ratio of: extraction agent: water=1～3: 1, when waste water is carried out multi-stage solvent extraction, extraction agent and waste water are compared mixing with above-mentioned, at normal temperatures, extracted 10～60 minutes, make two-phase reach extraction equilibrium, static at normal temperatures phase-splitting;
3. isolate the water in above-mentioned second step, carry out second stage extraction by compare identical again with the first step, wherein extraction phase is a lean solvent, reach phase-splitting after the balance, sampling analysis, the residue water carries out third stage extraction with lean solvent, so analogizes, till the chemical oxygen demand value of extraction raffinate reaches emission standard.
Each grade extraction process is carried out sampling analysis COD
Cr, pH value, water hydrogen ion concentration so that judge the processed degree of waste water.
In order to recycle extraction agent, reclaim the benzoate product, can also advance～go on foot to adopt sodium hydroxide, potassium hydroxide, sodium hydrogen carbonate solution that the extraction agent of load solute is carried out back extraction regeneration (separating out or concentrating of solute).In the back extraction operation, it is alkali lye/extraction agent=1:1 ~ 3 that operational volume is compared scope.Acid in the waste water obtains enrichment in alkali lye, finally realize the recovery of benzoate.In the solvent reclamation process, be back extraction alkali lye with sodium hydroxide, potassium hydroxide and sodium hydrogen carbonate solution respectively, rich solvent is carried out the back extraction simulated experiment.When making each rich solvent, adopt fresh extraction agent with 1: after compare and the waste water of l reaches extraction equilibrium, the hydrogen ion concentration of acid in the titration extraction agent.The rich solvent of getting 10ml then joins in the 50ml tool plug Erlenmeyer flask, adds isopyknic alkali lye again, places the full warm air of HzQ-F type to bathe vibrator, at normal temperatures with 220min
-1Velocity fluctuation 30 minutes, reach the back extraction balance, hydrionic concentration in the titration organic phase.
The phenylformic acid wastewater preprocessing process of this invention is the method that adopts complexometric extraction, select tributyl phosphate, trialkylphosphine oxide, trialkylamine as extraction agent, most of acid organism and generate the organic by-products that is soluble in organic phase aborning and come together in the waste water into organic phase, extraction agent can be recycled after the alkali lye back extraction, can realize the benzoic utilization of valuable material in the waste water after the alkali lye enrichment acid, the waste water of treated mistake can meet the requirement of biochemical degradation or other secondary method of edge treatment.Therefore the complexometric extraction para Toluic Acid pretreatment method for wastewater of using of the present invention owing to the highly selective in polarity organic water solution system and efficient hollow, has been successfully used to phenol, aniline, organic acid extraction recovery.
Introduce embodiments of the invention below.
EXAMPLE l: adopt four kinds of different extraction agents, 1. volumetric concentration 10% tributyl phosphate+90% kerosene, 2. volumetric concentration 30% tributyl phosphate+70% kerosene, 3. volumetric concentration 100% tributyl phosphate, 4. volumetric concentration 20% trialkylphosphine oxide+80% kerosene, waste water is carried out multi-stage solvent extraction, and join with certain comparing in the separating funnel of 300ml, the pairing volume of each extraction agent is compared (extraction phase/waste water) and was respectively 3: 1,2: 1,1: 1,2: l, the volume total amount is 240ml, cover bottle stopper, at normal temperatures, acutely shake, extracted 15 minutes, and made two-phase reach extraction equilibrium; The solution after the balance is left standstill at normal temperatures, phase-splitting separates organic phase and water after 10 minutes, measure water COD again
CrValue, pH value, and titration aqueous phase hydrogen ion concentration are obtained in the organic phase by the hydrogen ion concentration of collection acid according to material balance.Surplus water adds according to compare identical with the first step equally mutually and carries out second stage extraction in the separating funnel, and wherein extraction phase is a lean solvent, reaches phase-splitting after the balance, sampling analysis, and the residue water carries out third stage extraction with lean solvent, so analogizes.It the results are shown in Table 1.1. 10% tributyl phosphate, one kerosene system is carried out six grades of cross current solvent extractions to waste water under 3: 1 the condition of comparing result in the table 1,2. be 30% tributyl phosphate, one kerosene system 2: the result who under the condition of comparing of l waste water is carried out eight grades of cross current solvent extractions, 3. being 100% tributyl phosphate system is carried out the level Four cross current solvent extraction to waste water under 1: 1 the condition of comparing result, 4. is 20% trialkylphosphine oxide, one kerosene system is carried out six grades of cross current solvent extractions to waste water under 2: 1 the condition of comparing result.Experiment shows that after the multistage cross flow extraction treatment, the acid solute rate of recovery is higher, the COD of waste water
CrValue greatly reduces.
Table l extraction agent is handled the cross-flow experimental result of waste water
| Extraction agent | Project | Raw wastewater | One-level | Secondary | Three grades | Level Four | Pyatyi | Six grades | Seven grades | Eight grades |
| ① | COD Cr(mg／L) | 23270 | ?15230 | ?12450 | ?10010 | ?7050 | ?6285 | ?5024 | ?4252 | |
| ?PH | ?2．03 | ?2．16 | ?2．15 | ?2．26 | ?2．34 | ?2．48 | ?2．64 | ?3．09 |
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.381 | ?0.268 | ?0.185 | ?0.124 | ?0.083 | ?0.056 | ?0.036 | ||
| ② | ?????COD Cr????(mg/L) | ?23270 | ?10938 | ?7738 | ?5068 | ?4063 | ?3468 | ?2654 | ?2693 | ?2659 |
| ??????PH | ?2.03 | ?2.11 | ?2.55 | ?2.82 | ?3.19 | ?3.65 | ?4.30 | ?4.69 | ?5.10 | |
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.273 | ?0.136 | ?0.065 | ?0.034 | ?0.018 | ?0.009 | ?0.006 | ?0.005 | |
| ③ | ?????COD Cr????(mg/L) | ?23270 | ?8800 | ?4633 | ?4210 | ?3245 | ||||
| ??????PH | ?2.03 | ?2.40 | ?2.81 | ?2.35 | ?4.64 | |||||
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.169 | ?0.050 | ?0.015 | ?0.006 | |||||
| ④ | ?????COD Cr????(mg/L) | ?23270 | ?8042 | ?4354 | ?2782 | ?2180 | ?2055 | ?1933 | ||
| ??????PH | ?2.03 | ?2.45 | ?3.06 | ?3.63 | ?3.95 | ?4.09 | ?4.56 | |||
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.167 | ?0.031 | ?0.009 | ?0.004 | ?0.003 | ?0.002 |
Embodiment 2: adopt four kinds of different extraction agents, 1. volumetric concentration 20% tributyl phosphate+80% kerosene, 2. volumetric concentration 40% tributyl phosphate+60% kerosene, 3. volumetric concentration 50% tributyl phosphate+50% kerosene, 4. volumetric concentration 20% trialkylamine+30% n-Octanol+50% kerosene, waste water is carried out multi-stage solvent extraction, and join with certain comparing in the separating funnel of 300ml, the pairing volume of each extraction agent is compared (extraction phase/waste water) and was respectively 2: 1,2: 1,2: 1,1: 2, the volume total amount is 240ml, cover bottle stopper, at normal temperatures, acutely shake, extracted 30 minutes, and made two-phase reach extraction equilibrium; The solution after the balance is left standstill at normal temperatures, phase-splitting separates organic phase and water after 10 minutes, measure water COD again
CrValue, pH value, and titration aqueous phase hydrogen ion concentration are obtained in the organic phase by the hydrogen ion concentration of collection acid according to material balance.Surplus water adds according to compare identical with the first step equally mutually and carries out second stage extraction in the separating funnel, and wherein extraction phase is a lean solvent, reaches phase-splitting after the balance, sampling analysis, and the residue water carries out third stage extraction with lean solvent, so analogizes.It the results are shown in Table 2.1. 20% tributyl phosphate-kerosene system is carried out six grades of cross current solvent extractions to waste water under 2: 1 the condition of comparing result in the table 2,2. be 40% tributyl phosphate-kerosene system is carried out three grades of cross current solvent extractions to waste water under 2: 1 the condition of comparing result, 3. being 50% tributyl phosphate-kerosene system is carried out the level Four cross current solvent extraction to waste water under 2: 1 the condition of comparing result, 4. is 20% trialkylamine-30% n-Octanol-kerosene system is carried out six grades of cross current solvent extractions to waste water under 1: 2 the condition of comparing result.Experiment shows that after the multistage cross flow extraction treatment, the acid solute rate of recovery is higher, the COD of waste water
CrValue greatly reduces.
Table 2 extraction agent is handled the cross-flow experimental result of waste water
| Extraction agent | Project | Raw wastewater | One-level | Secondary | Three grades | Level Four | Pyatyi | Six grades | Seven grades | Eight grades |
| ??① | ?COD Cr?(mg/L) | ?23270 | ?17023 | ?11818 | ?9080 | ?6940 | ?5805 | ?3473 | ||
| ?PH | ?2.03 | ?2.24 | ?2.34 | ?2.50 | ?2.60 | ?2.77 | ?3.69 | |||
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.334 | ?0.204 | ?0.125 | ?0.074 | ?0.049 | ?0.020 | |||
| ??② | ?COD Cr?(mg/L) | ?23270 | ?10564 | ?6772 | ?3576 | |||||
| ?PH | ?2.03 | ?2.36 | ?2.62 | ?2.97 |
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.2616 | ?0.086 | ?0.033 | ||||||
| ?③ | ?COD Cr?(mg/L) | ?23270 | ?8430 | ?5273 | ?4180 | ?3140 | ||||
| ?PH | ?2.03 | ?2.50 | ?2.77 | ?3.13 | ?4.32 | |||||
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.188 | ?0.064 | ?0.022 | ?0.007 | |||||
| ?④ | ?COD Cr?(mg/L) | ?23270 | ?9219 | ?5998 | ?4643 | ?4650 | ||||
| ?PH | ?2.03 | ?2.44 | ?3.09 | ?3.58 | ?4.02 | |||||
| Hydrogen ion concentration (mol/L) | ?0.564 | ?0.302 | ?0.169 | ?0.089 | ?0.044 |
Embodiment 3: being respectively 20% tributyl phosphate+80% kerosene, 50% tributyl phosphate+50% kerosene, 20% trialkylphosphine oxide+80% kerosene with volumetric concentration is extraction agent, be back extraction alkali lye with sodium hydroxide, potassium hydroxide and sodium hydrogen carbonate solution respectively, waste water is carried out the back extraction simulated experiment.After adopting fresh extraction agent to reach extraction equilibrium with waste water with 1: 1 compare, the hydrogen ion concentration of acid in the titration extraction agent.The extraction agent of getting then after the 10ml load joins in the 50ml tool plug Erlenmeyer flask, adds isopyknic alkali lye again, places the full warm air of HZQ-F type to bathe vibrator, at normal temperatures with 220min
-1Velocity fluctuation 30 minutes, reach the back extraction balance, hydrionic concentration in the titration organic phase, after the definition back extraction balance in the organic phase in hydrogen ion concentration and the initial organic phase ratio of hydrogen ion concentration be back extraction ratio.The result of back extraction shows that sodium hydroxide, potassium hydroxide, sodium bicarbonate all have back extraction effect preferably to the load extraction agent, when the equivalent concentration of alkali in the alkali lye can realize 100% back extraction during the load hydrogen ionic concn in greater than extraction agent.
Embodiment 4: the employing volumetric concentration is that 50% tributyl phosphate-kerosene is extraction agent, carries out the experiment of multistage cross flow extracting-back extraction.Get the fresh extraction agent of 200ml and place the 400ml separating funnel, compare adding waste water by organic phase/waste water of 2: 1, acutely shake at normal temperatures and reached balance in 15 minutes, the water parameter is measured in phase-splitting.Load organic phases is taken out and is mixed with 10% NaOH solution and carries out back extraction, and step is identical with embodiment 2, reach the back extraction balance after, leave standstill phase-splitting.Regenerated solvent continues to carry out second stage extraction with 2: 1 compare with first step extraction raffinate water, reaches phase-splitting after the balance, regenerated solvent, enters the next stage extraction.It the results are shown in Table 3.As can be seen from the table, adopting regenerating extracting agent to carry out wastewater treatment also can reach the solute recovery and reduce COD
CrEffect, stripping method is feasible.
Table 3 50% tributyl phosphate-kerosene is handled the cross-flow experimental result of waste water
| Extraction progression | COD Cr(mg／L) | pH | Hydrogen ion concentration (mol/L) | Hydrogen ion in the extraction agent (mol/L) | Hydrogen is from degree (mol/L) in the regenerating extracting agent |
| Original waste water | 23270 | ?2．03 | ?0．564 | - | - |
| One-level | 8430 | ?2．50 | ?0．188 | ?0．184 | ?0 |
| Secondary | 5273 | ?2．77 | ?0．064 | ?0．061 | ?0 |
| Three grades | 4180 | ?3．13 | ?0．022 | ?0．021 | ?0 |
| Level Four | 3140 | ?4．32 | ?0．007 | ?0．008 | - |
Embodiment 5: the employing volumetric concentration is 40% tributyl phosphate-kerosene extraction agent, carry out the fatigue experiment of extraction agent, experimental technique is as follows: getting fresh 40% tributyl phosphate-kerosene is extraction agent, mix with waste water with 1: 1 compare and to reach extraction equilibrium, phase-splitting, difference titration organic phase and aqueous phase hydrogen ion concentration, getting organic phase mixes with 10% NaOH solution with 1: 1 compare and reaches the back extraction balance, phase-splitting, get organic phase, titration is the concentration of acid wherein, obtains back extraction ratio, get this organic phase and extract next time, wherein water is the original liquid of waste water.Through eight fatigue experiments, find that extraction agent has fatigue strength preferably, extracting power remains unchanged, and the back extraction phase-splitting is rapid, and extractant regeneration is simple.Table 4 is eight fatigue experiment results of extraction agent.
Table 4 40% tributyl phosphate-kerosene fatigue experiment result
| Experiment number | Extraction raffinate hydrogen ion (mol/L) | Back extraction ratio | Experiment number | Extraction raffinate hydrogen ion (mol/L) | Back extraction ratio |
| 1 | ?0．219 | ?100％ | 5 | ?0．217 | ?100％ |
| 2 | ?0．219 | ?100％ | 6 | ?0．216 | ?100％ |
| 3 | ?0．212 | ?100％ | 7 | ?0．217 | ?100％ |
| 4 | ?0．216 | ?100％ | 8 | ?0．213 | ?100％ |
Claims (1)
1, a kind of with complexometric extraction para Toluic Acid pretreatment method for wastewater, it is characterized in that this method comprises following each step:
(1) preparation extraction agent, its composition is complexing agent+solubility promoter+thinner, and the volume proportion of extraction agent is that complexing agent accounts for 10%～100%, and solubility promoter accounts for 0～40%, and all the other are thinner, complexing agent wherein is tributyl phosphate, trialkyl (C
8～C
10) amine or trialkyl (C
8～C
10) any in the phosphine oxide, solubility promoter is a n-Octanol, thinner is a kerosene, and complexing agent, solubility promoter, thinner are mixed at normal temperatures by above-mentioned volume ratio, and is standby;
(2) mixed solvent with above-mentioned preparation is an extraction agent, at normal temperatures, para Toluic Acid's waste water carries out multi-stage solvent extraction, and in extracting operation, volume is in a ratio of: extraction agent: water=1～3: 1, when waste water is carried out multi-stage solvent extraction, extraction agent and waste water are compared mixing with above-mentioned, at normal temperatures, extracted 10～60 minutes, make two-phase reach extraction equilibrium, static at normal temperatures phase-splitting;
(3) isolate above-mentioned second water that goes on foot, carry out second stage extraction by compare identical again with the first step, wherein extraction phase is a lean solvent, reach phase-splitting after the balance, sampling analysis, the residue water carries out third stage extraction with lean solvent, so analogizes, till the chemical oxygen demand value of extraction raffinate reaches emission standard.
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| CN110857233A (en) * | 2018-08-22 | 2020-03-03 | 沈阳化工研究院设计工程有限公司 | Device and method for treating high-salinity wastewater containing phenol and aniline |
| CN109850976A (en) * | 2018-12-31 | 2019-06-07 | 江苏尚莱特医药化工材料有限公司 | The recovery and treatment method of p-aminobenzoic acid in p-aminobenzoic acid technique waste water |
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