CN1884144A - Method for treating waste water in production of para-hydroxyphenyl hydantoin - Google Patents
Method for treating waste water in production of para-hydroxyphenyl hydantoin Download PDFInfo
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- CN1884144A CN1884144A CN200610085746.2A CN200610085746A CN1884144A CN 1884144 A CN1884144 A CN 1884144A CN 200610085746 A CN200610085746 A CN 200610085746A CN 1884144 A CN1884144 A CN 1884144A
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- para hydroxybenzene
- wastewater treatment
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- water
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- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000002351 wastewater Substances 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- 229940091173 hydantoin Drugs 0.000 title abstract 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 59
- 229960003742 phenol Drugs 0.000 claims abstract description 29
- 239000011347 resin Substances 0.000 claims abstract description 24
- 229920005989 resin Polymers 0.000 claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 150000003839 salts Chemical class 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 7
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 40
- 238000003795 desorption Methods 0.000 claims description 35
- 238000010521 absorption reaction Methods 0.000 claims description 29
- NCLQYEZASHMIHD-UHFFFAOYSA-N C(CO)(=O)NC(=O)N.OC1=CC=CC=C1 Chemical compound C(CO)(=O)NC(=O)N.OC1=CC=CC=C1 NCLQYEZASHMIHD-UHFFFAOYSA-N 0.000 claims description 28
- 238000004065 wastewater treatment Methods 0.000 claims description 19
- 239000012452 mother liquor Substances 0.000 claims description 13
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 9
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 8
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 8
- 235000011152 sodium sulphate Nutrition 0.000 claims description 8
- 238000001179 sorption measurement Methods 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 7
- 239000012265 solid product Substances 0.000 claims description 6
- 238000004132 cross linking Methods 0.000 claims description 4
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 claims description 4
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 3
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 208000006558 Dental Calculus Diseases 0.000 claims description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 2
- 229910021653 sulphate ion Inorganic materials 0.000 claims description 2
- -1 hydroxybenzene glycolylureas Chemical class 0.000 claims 1
- FEPBITJSIHRMRT-UHFFFAOYSA-N 4-hydroxybenzenesulfonic acid Chemical compound OC1=CC=C(S(O)(=O)=O)C=C1 FEPBITJSIHRMRT-UHFFFAOYSA-N 0.000 abstract 1
- QIGBRXMKCJKVMJ-UHFFFAOYSA-N Hydroquinone Chemical compound OC1=CC=C(O)C=C1 QIGBRXMKCJKVMJ-UHFFFAOYSA-N 0.000 abstract 1
- 239000002131 composite material Substances 0.000 abstract 1
- WJRBRSLFGCUECM-UHFFFAOYSA-N hydantoin Chemical compound O=C1CNC(=O)N1 WJRBRSLFGCUECM-UHFFFAOYSA-N 0.000 abstract 1
- 238000009938 salting Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 13
- 238000000605 extraction Methods 0.000 description 11
- 230000008901 benefit Effects 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 6
- 238000010792 warming Methods 0.000 description 5
- 238000004821 distillation Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000012074 organic phase Substances 0.000 description 3
- 238000005185 salting out Methods 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000020477 pH reduction Effects 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 125000003368 amide group Chemical group 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- HHLFWLYXYJOTON-UHFFFAOYSA-N glyoxylic acid Chemical compound OC(=O)C=O HHLFWLYXYJOTON-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- ILRLTAZWFOQHRT-UHFFFAOYSA-N potassium;sulfuric acid Chemical compound [K].OS(O)(=O)=O ILRLTAZWFOQHRT-UHFFFAOYSA-N 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000000967 suction filtration Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
Landscapes
- Water Treatment By Sorption (AREA)
- Removal Of Specific Substances (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a disposing method of waste water in the p-hydroxybenzene hydantoin manufacturing course, which comprises the following steps: salting waste water with phenol mother liquid through soluble salt; stewing to divide water-phase; blending salted water phase and waste water according to 1:1-8; adsorbing the composite liquid in the resin adsorbing column under normal temperature at 0.1-2 BV per h flow; desorbing the adsorbed saturated resin; preparing for next adsorbing disposal. The invention removes p-phenolsulfonate by over 99 percent, which doesn't pollute environment.
Description
Technical field
The present invention relates to a kind of method of wastewater treatment, wastewater treatment method during specifically a kind of para hydroxybenzene glycolylurea is produced.
Background technology
The para hydroxybenzene glycolylurea is a kind of important chemical material and medicine intermediate, is mainly used in biological process and prepares the D-D-pHPG.Adopting oxoethanoic acid, urea, phenol is raw material, and in a certain amount of acidic medium, synthetic para hydroxybenzene glycolylurea can produce high-concentration phenolic wastewater, as effectively not administering directly discharging, certainly will cause long-term serious pollution to environment.
At present domestic: i.e. distillation-extraction-absorbing process about only there being following method to meet report in the treatment process of this factory effluent.
This method is to adopt earlier the mother liquor waste water underpressure distillation, distillate and the merging of material washes are carried out the two-stage extraction through special-purpose phenol extraction agent, water after will extracting then is through three posts series connection absorption (XD-303 resin), raffinate after wherein distilling returns synthesizing section and applies mechanically, organic phase after the extraction merges and lower floor's alkali lye is used to apply mechanically again after NaOH solution carries out back extraction, merge processing with desorption liquid after applying mechanically three times, upper organic phase is returned extraction, only select NaOH solution as desorbing agent during desorption, reclaimed phenol through the alkali lye merging of applying mechanically after three times through the method for underpressure distillation again after desorption liquid and the above-mentioned back extraction.
This shows that above-mentioned treatment process technology is tediously long, operation is loaded down with trivial details, and cost is higher, and following shortcoming is arranged specifically: 1. underpressure distillation energy consumption height, to the equipment requirements height, must carry out professional training to operator, and this can increase processing cost undoubtedly; 2. extraction is a kind of technology of Phenol-Containing Wastewater Treatment really, but selection of Extractant there is strict requirement, promptly must satisfy nontoxic, chemical stability is good, easily reclaim, requirement such as cheap grade, and this technology is better to lower concentration phenolic wastewater treatment effect, can only be when being used for high dense phenolic wastewater as preprocessing means, above-mentioned extraction is that the pretreating effect that reaches certain has adopted the two-stage extraction, complex process and increased processing cost, and the back extraction problem of extraction back organic phase also has to consider, therefore no matter still be cost from technology, aforesaid method all seems to have no advantage.That 3. polymeric adsorbent adopts is XD-303, it is a kind of macroporous adsorbent resin, modifies without any functional group, and the absorption of Pyrogentisinic Acid's molecule only depends on model ylid bloom action power to realize, guaranteeing to consume the more resin of volume under the same treatment effect prerequisite, three post tandem process have promptly been adopted; What 4. desorption liquid is adopted is underpressure distillation, cooling, crystallization, suction filtrations etc. reclaim phenol, though the phenol recovery rate near 100%, technology is loaded down with trivial details, processing cost is higher, is unacceptable to most of medium-sized and small enterprises.
Therefore aforesaid method complicated operation, cost is higher, is difficult to apply, so it is simple to be badly in need of developing a kind of flow process, cost is low, can realize that changing rejected material to useful resource and effective method of wastewater treatment are in the hope of realizing environmental benefit and economic benefit preferably.
Summary of the invention
The objective of the invention is to characteristics at para hydroxybenzene glycolylurea factory effluent, a kind of removal efficient height, simple, the non-secondary pollution of technology are provided, simultaneously can reclaim solid product, realize changing rejected material to useful resource, wastewater treatment method during a kind of para hydroxybenzene glycolylurea with good economic benefit and environmental benefit is produced.
Purpose of the present invention can reach by following measure:
The treatment process of being arranged in the production of a kind of para hydroxybenzene glycolylurea, its step is as follows:
(A) the phenol mother liquor waste water that contains that is discharged in the production of para hydroxybenzene glycolylurea is saltoutd with soluble salt, leave standstill and tell water;
(B) water after will saltouing and the material washing water in the para hydroxybenzene glycolylurea production process are that 1: 1～8 mixed obtains mixing solutions by volume;
(C) at normal temperatures, feed the resin absorption post with the flow of 0.1～2BV/h (promptly per hour the volume by solution is 0.1～2 times of a resin column volumetrical) and carry out adsorption treatment above-mentioned mixing solutions;
(D) carry out desorption and handle adsorbing adsorption column after saturated, for the adsorption treatment of mixing solutions is next time got ready.
The present invention utilizes the physics salting-out process that waste water in the production of para hydroxybenzene glycolylurea is particularly contained the phenol mother liquor waste water to carry out pre-treatment, contain high concentration phenol in the mother liquor waste water, pass through salting-out effect, make most of phenol enter oil phase, mix by adsorbing by certain volume ratio with the material washes again after telling water through amido modified superhigh cross-linking resin (being the NDA-99 resin), this resin not only adsorbs by model ylid bloom action power Pyrogentisinic Acid molecule, and also there is hydrogen bond action power in its functional group-amino with the phenol molecule, on above two kinds of coefficient bases of reactive force, the clearance of phenol reaches more than 99%, can also the recovery part solid product by the dense desorption liquid of height being carried out acidification, not only obtained treatment effect preferably, also reduced processing cost, it is a kind of simple to operate to can yet be regarded as, cost is low, non-secondary pollution, the method for wastewater treatment with good environment benefit and economic benefit.
The used soluble salt of saltouing in the step of the present invention (A) is soluble sulphate or hydrochloride, preferred solid sodium sulfate, vitriolate of tartar, sodium-chlor or Repone K, solid sodium sulfate most preferably, consumption is 30～60g/100mL, the salt eutectoid temperature is preferably 35～60 ℃, stir when saltouing, churning time is 30～50min.
Water after saltouing in the step (B) and the material washes in the para hydroxybenzene glycolylurea production process be 1: 2 by volume～4 mixed preferably.
The resin that uses in the step (C) is preferably NDA-99 superhigh cross-linking resin, adopt 2～4 resin column series connection, the placed in-line method of preferred 2 resin columns head and the tail is adsorbed, and absorption flow is preferably 0.1～1BV/h, the batch processing amount of absorption is 10～40BV, preferred 20BV.
NDA-99 superhigh cross-linking resin recited above is by Jiangsu Nanda Gede Environmental Protection Technology Co., Ltd's production and sales.
Water quality after the absorption is phenol content≤10mg/L, the cod codcr≤400mg/L that adopts potassium bichromate to determine as oxygenant.
Only first post is carried out desorption in the step (D), use 2～8%NaOH or the KOH solution of 2BV in the desorption process earlier, re-use 2～4BV water and carry out desorption; Desorption temperature is 40～80 ℃, is preferably 70～80 ℃; The desorption flow is 0.1～1BV/h, preferred 0.1～0.5BV/h.
Collect desorption liquid, the desorption liquid of the high density collected is transferred to about pH=2～4 with 30% hydrochloric acid, filter out solid product.
The inventive method is handled the existing relatively method of para hydroxybenzene glycolylurea factory effluent and is had the following advantages:
(1) only just realized by saltouing that technology is simple to containing the pre-treatment that phenol mother liquor waste water, particularly high density contain the phenol mother liquor waste water, cost is low, easy operation control;
(2) adopt twin columns series connection absorption, the circulation technology of single-column desorption can be realized continuous operation in the actual industrial application;
(3) desorbing agent adopts NaOH solution and water to make up, and has reduced the consumption of NaOH solution, has saved medicament expense usefulness;
(4) processing of high dense desorption liquid is simple, and can reclaim solid product.
Beneficial effect of the present invention is as follows:
1, provides wastewater treatment method in a kind of brand-new para hydroxybenzene glycolylurea production.
2, Pyrogentisinic Acid's clearance reaches more than 99%, sees the following form 1, thereby this invention has good benefits in environment.
Table 1
| Embodiment | Detect | Mother liquor waste water | The water of saltouing | Mixed solution | Absorption effluent | Clearance |
| Embodiment one | Phenol mg/L | 29684.63 | 4671.66 | 2756.74 | 3.92 | 99.86％ |
| CODcr mg/L | 75350.95 | 12997.98 | 13078.47 | 190.08 | 98.55％ | |
| Embodiment three | Phenol mg/L | 29684.63 | 4453.41 | 2769.77 | 5.17 | 99.81％ |
| CODcr mg/L | 75350.95 | 15365.96 | 12014.86 | 217.67 | 98.19％ |
3, the physics salting-out process that uses among the present invention, principle is simple, and medicament expense is used with working cost low, and pretreating effect is good.
4, water outlet is effective, and the overall operation cost is low, and saltout and resin absorption can not cause secondary pollution to environment.
Embodiment
Embodiment one
The amount that contains in the phenol mother liquor waste water by 54g/100mL (w/v) of at first being discharged in the production of para hydroxybenzene glycolylurea adds solid sodium sulfate, be warming up to 40 ℃, after stirring 35min, standing demix 1h, the back water of will saltouing is told, and 1: 3 by volume ratio is mixed with material washes in the para hydroxybenzene glycolylurea production process.Mixed solution is through two posts series connection absorption, and the control absorption flow is 1BV/h, when absorption batch processing amount reaches 20BV, stops absorption.The average phenol concentration of absorption effluent is 3.92mg/L, CODcr=190.08mg/L (chemical oxygen demand that adopts potassium bichromate to determine as oxygenant).Only first post being carried out desorption handles: at first dispose 6% NaOH solution as desorbing agent, in post, add the 6%NaOH solution of about 0.6BV then, being heated to 70 ℃ makes resin soak 0.5h, open peristaltic pump afterwards, dominant discharge is 0.5BV/h, and desorption liquid is collected in classification, promptly at first the desorption liquid of 0-0.5BV is collected, regather the desorption liquid of 0.5-1BV, the desorption liquid of 1-2BV is collected with the 3rd container.Divide the 6%NaOH solution that in post, adds 70 ℃ for 2～3 times to 2BV during the collection, guarantee that resin is immersed in the 6%NaOH solution all the time; Treating when desorption liquid soon can not the submergence resin 70 ℃ distilled water with 2BV is added in the post, resin washed that temperature and flow all remain unchanged.After treating that this post (being first post) washing finishes,, the adsorption column of desorption (being stern post) is not carried out the absorption of next batch as the first post of next batch with its stern post as next batch.The acidification of desorption liquid: in the desorption liquid of 0-0.5BV, drip 30% hydrochloric acid, its pH is transferred to about 2, filter, reclaim solid product.
Embodiment two:
At first the amount by 40g/100mL (w/v) adds solid sodium sulfate in the mother liquor waste water that is discharged in the production of para hydroxybenzene glycolylurea, be warming up to 60 ℃, behind the stirring 45min, standing demix 1h, the back water of will saltouing is told, and 1: 1 by volume ratio is mixed with washes.The control absorption flow is 0.1BV/h.When absorption batch processing amount reaches 10BV, stop absorption, temperature is 60 ℃ during desorption, and flow is 0.1BV/h, and desorbing agent is selected 4% NaOH for use.Adding hydrochloric acid transfers to desorption liquid pH about 4.Other conditions are with embodiment one.The average phenol content of absorption effluent is 5.56mg/L, CODcr=261.23mg/L.
Show in the enforcement: solid sulphuric acid potassium has close effect, but cost is higher, and uses sodium-chlor or Repone K that close effect is also arranged.
Embodiment three:
At first the amount that contains in the phenol mother liquor waste water by 42g/100mL (w/v) in high density adds solid sodium sulfate, is warming up to 50 ℃, stir 50min after, standing demix 1h, the back water of will saltouing is told, 1: 3 by volume ratio is mixed with washes.Other conditions are with embodiment one.The average phenol content of absorption effluent is 5.17mg/L, CODcr=217.67mg/L (chemical oxygen demand that adopts potassium bichromate to determine as oxygenant).
Embodiment four:
At first the amount that contains in the phenol mother liquor waste water by 50g/100mL (w/v) in high density adds solid sodium sulfate, is warming up to 45 ℃, stir 30min after, standing demix 1h, the back water of will saltouing is told, 1: 2 by volume ratio is mixed with washes.The control absorption flow is 0.5BV/h, when absorption batch processing amount reaches 30BV, stops absorption.Other conditions are with embodiment two.The average phenol content of absorption effluent is 6.39mg/L, CODcr=285.48mg/L.
Embodiment five:
At first the amount that contains in the phenol mother liquor waste water by 60g/100mL (w/v) in high density adds solid sodium sulfate, be warming up to 35 ℃, after stirring 50min, standing demix 1h, the back water of will saltouing is told, 1: 8 by volume ratio is mixed with washes, absorption flow is 2BV/h, and temperature is 80 ℃ during desorption, and flow is 1BV/h, desorbing agent is selected 8% NaOH for use, and desorption liquid is transferred about pH to 3 after adding hydrochloric acid.Other conditions are with embodiment one.The average phenol content of absorption effluent is 8.24mg/L, CODcr=335.31mg/L.
Claims (10)
1, wastewater treatment method during a kind of para hydroxybenzene glycolylurea is produced is characterized in that:
(A) adopt soluble salt to saltout the phenol mother liquor waste water that contains that is discharged in the production of para hydroxybenzene glycolylurea, leave standstill and tell water;
(B) water after will saltouing and the material washes in the para hydroxybenzene glycolylurea production process are that 1: 1～8 mixed obtains mixing solutions by volume;
(C) at normal temperatures, the flow feeding resin absorption post with 0.1～2BV/h carries out adsorption treatment with above-mentioned mixing solutions;
(D) carry out desorption and handle adsorbing adsorption column after saturated, for the adsorption treatment of mixing solutions is next time got ready.
2, wastewater treatment method during para hydroxybenzene glycolylurea according to claim 1 is produced, the used soluble salt that it is characterized in that saltouing in the step (A) is soluble sulphate or hydrochloride, consumption is 30～60g/100mL.
3, wastewater treatment method during para hydroxybenzene glycolylurea according to claim 1 and 2 is produced, the used soluble salt that it is characterized in that saltouing is solid sodium sulfate, vitriolate of tartar, sodium-chlor or Repone K, the salt eutectoid temperature is 35～60 ℃, stirs when saltouing, and churning time is 30～50min.
4, wastewater treatment method during para hydroxybenzene glycolylurea according to claim 1 is produced, the water after it is characterized in that saltouing in the step (B) and the mixed of the material washing water 1: 2 by volume～4 in the para hydroxybenzene glycolylurea production process.
5, wastewater treatment method during para hydroxybenzene glycolylurea according to claim 1 is produced is characterized in that the resin that uses in the step (C) is NDA-99 superhigh cross-linking resin, adopts the placed in-line method of 2～4 resin columns to adsorb.
6, wastewater treatment method during the para hydroxybenzene glycolylurea is produced according to claim 1 or 5 is characterized in that absorption flow is 0.1～1BV/h, and the batch processing amount of absorption is 10～40BV.
7, wastewater treatment method during para hydroxybenzene glycolylurea according to claim 1 is produced, the water quality after it is characterized in that adsorbing is phenol content≤10mg/L, the cod codcr≤400mg/L that adopts potassium bichromate to determine as oxygenant.
8, wastewater treatment method during para hydroxybenzene glycolylurea according to claim 1 is produced, it is characterized in that only first post being carried out desorption in the step (D), using the massfraction of 2BV earlier in the desorption process is 2～8%NaOH or KOH solution, re-uses 2～4BV water and carries out desorption.
9, according to wastewater treatment method in claim 1 or the 8 described para hydroxybenzene glycolylureas productions, it is characterized in that desorption temperature is 40～80 ℃, flow is 0.1～1BV/h, collects desorption liquid.
10, wastewater treatment method during para hydroxybenzene glycolylurea according to claim 9 is produced is characterized in that the desorption liquid of the high density that will collect transfers to about pH=2～4 with 30% hydrochloric acid, filters out solid product.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2006100857462A CN100513333C (en) | 2006-06-29 | 2006-06-29 | Method for treating waste water in production of para-hydroxyphenyl hydantoin |
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| CNB2006100857462A CN100513333C (en) | 2006-06-29 | 2006-06-29 | Method for treating waste water in production of para-hydroxyphenyl hydantoin |
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| CN100513333C CN100513333C (en) | 2009-07-15 |
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| CN101230123B (en) * | 2007-12-28 | 2010-06-09 | 天津市职业大学 | Comprehensive utilization method for byproduct of p-hydroxybenzene hydantoin production |
| CN107445414A (en) * | 2017-09-26 | 2017-12-08 | 南京大学 | A kind of process for cleanly preparing of gallic acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101230123B (en) * | 2007-12-28 | 2010-06-09 | 天津市职业大学 | Comprehensive utilization method for byproduct of p-hydroxybenzene hydantoin production |
| CN107445414A (en) * | 2017-09-26 | 2017-12-08 | 南京大学 | A kind of process for cleanly preparing of gallic acid |
| CN107445349A (en) * | 2017-09-26 | 2017-12-08 | 南京大学 | A kind of recycling processing method of gallic acid production wastewater |
| CN109867391A (en) * | 2017-12-03 | 2019-06-11 | 天津市职业大学 | The preprocess method of 4-Hydroxyphenyl hydantoin production high concentration highly acid phenolic waste liquor |
| CN109867391B (en) * | 2017-12-03 | 2021-12-24 | 天津市职业大学 | Pretreatment method for high-concentration strong-acid phenol-containing waste liquid in production of p-hydroxy-phenyl-hydantoin |
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