CN103768822B - A kind of processing method of unsaturated polyester (UP) steam - Google Patents
A kind of processing method of unsaturated polyester (UP) steam Download PDFInfo
- Publication number
- CN103768822B CN103768822B CN201210404075.7A CN201210404075A CN103768822B CN 103768822 B CN103768822 B CN 103768822B CN 201210404075 A CN201210404075 A CN 201210404075A CN 103768822 B CN103768822 B CN 103768822B
- Authority
- CN
- China
- Prior art keywords
- steam
- polyester
- treatment
- water
- waste water
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
The present invention relates to the processing method of a kind of unsaturated polyester (UP) steam。This method includes herein below: (1) one-level condenses, and makes polyester steam mid-boiling point transfer to liquid phase higher than the Organic substance of water from gas phase, reduces organic concentration in steam；(2) B-grade condensation, is condensed into low concentration polyester waste water by condensed for one-level steam；(3) anaerobic treatment, after B-grade condensation, waste water carries out anaerobic treatment；(4) Aerobic Process for Treatment, the waste water after anaerobic treatment carries out Aerobic Process for Treatment；(5) precipitation filters, the discharge after precipitation, filtration of the water outlet after Aerobic Process for Treatment。The method without being condensed into high concentrated organic wastewater by polyester steam, and the Organic substance response rate is high, and subsequent treatment energy consumption is low, flow process is short, equipment is simple, stable operation, and processing water outlet can qualified discharge。
Description
Technical field
The present invention relates to the processing method of a kind of polyester steam, particularly relate to the process of the polyester steam that the polycondensation reaction stage produces in a kind of unsaturated polyester resin (UPR) production process。
Background technology
Unsaturated polyester resin (UPR) is to be prepared through polycondensation reaction by binary acid, dihydroxylic alcohols, and polycondensation reaction is a reversible reaction generating condensation water, therefore makes generation water constantly be evaporated in course of reaction, so that reaction carries out to the direction generating product。Its polyester steam mainly contains reaction mass and the intermediate products such as ethylene glycol, propylene glycol, diglycol, low molecule polyester monocase, phthalic acid, maleic acid, and concentration is at 50～150g/m3Between。It is big that this kind of unsaturated polyester (UP) steam has vapour content, the feature that organic concentration is high, and directly condensation will form acid extremely strong high concentrated organic wastewater, and its biochemical treatment not only investment cost is high, and processing cost is also sufficiently expensive。
Production by Catalytic Combustion Process is to process a kind of effective ways of flammable organic exhaust gas, and CN02109675.9 and CN200610047791.9 all proposes to adopt the method for catalysis burning to process waste polyester gas。But, these methods are required for through complicated pretreatment, remove the water vapour in waste gas, dust and some there is corrosive Organic substance, it is to avoid affect the service life of catalyst and device。CN200510015163.8 discloses the purification method of a kind of waste polyester gas, and waste polyester gas removes most of moisture through gas-liquid separator, carries out catalysis burning after then preheated, and partial reaction tail gas mixes to recover energy with waste polyester gas directly as carrier gas。Although the method can make waste polyester gas qualified discharge, but containing substantial amounts of moisture in unsaturated polyester (UP) steam, after gas-liquid separation pretreatment, the organic pollution such as acetaldehyde, ethylene glycol that are wherein soluble in shipwreck volatilization can transfer to generation high concentrated organic wastewater in aqueous phase, and subsequent treatment difficulty is big。Additionally, organic concentration fluctuates relatively big with the change of polycondensation reaction degree in polyester steam, this makes catalysis burning be in the state that temperature fluctuation is bigger, and the performance of catalyst and the life-span of equipment are all had adverse effect。Therefore, the method for the less than optimal process unsaturated polyester (UP) steam of Production by Catalytic Combustion Process。
The method that polyester enterprise many employings hot Media Oven of early stage burns processes polyester steam, but adopts this method to process the relatively costly of polyester steam, and in steam, substantial amounts of useful resources can not be recycled, and causes the huge wasting of resources；Simultaneously because system pressure not easily balances, there is serious safety problem, the method not in use by。Domestic existing major part unsaturated polyester (UP) manufacturing enterprise all adopts cooling, rectification, biochemical process route, the unsaturated polyester (UP) steam of high concentration is directly condensed into waste water, then it being carried out rectification, recovery section material, distillate carries out anaerobism, aerobic treatment。CN201010602167.7 discloses a kind of method reclaiming ethylene glycol and acetaldehyde in polyester waste water, esterification waste water enters stripping tower and processes, overhead collection to organic gas and steam be directly entered Ethanal distillation column, after Ethanal distillation column processes, in overhead collection to high-purity acetaldehyde, waste water at the bottom of tower is collecting high-purity ethylene glycol solution after entering the process of ethylene glycol distillation column at the bottom of tower, steam and steam that tower top produces are again introduced into stripping tower circular treatment。In the method, every kind of Organic substance needs to condense respectively recovery, it is necessary to just forming low concentration wastewater after multiple condensation, and reclaim not thoroughly, energy consumption is big, and cost is high, does not meet cleaning and produces the theory with recycling economy。
Summary of the invention
For the feature of the deficiencies in the prior art and unsaturated polyester (UP) steam, the present invention provides the processing method of a kind of unsaturated polyester (UP) steam。The method without being condensed into high concentrated organic wastewater by polyester steam, and the Organic substance response rate is high, and subsequent treatment energy consumption is low, flow process is short, equipment is simple, stable operation, and processing water outlet can qualified discharge。
The processing method of unsaturated polyester (UP) steam of the present invention, including herein below:
(1) one-level condensation, makes polyester steam mid-boiling point transfer to liquid phase higher than the Organic substance of water from gas phase, reduces organic concentration in steam；
(2) B-grade condensation, is condensed into low concentration polyester waste water by condensed for one-level steam；
(3) anaerobic treatment, after B-grade condensation, waste water carries out anaerobic treatment；
(4) Aerobic Process for Treatment, the waste water after anaerobic treatment carries out Aerobic Process for Treatment；
(5) precipitation filters, the discharge after precipitation, filtration of the water outlet after Aerobic Process for Treatment。
In the inventive method, described unsaturated polyester (UP) steam is from the polycondensation reaction stage in unsaturated polyester resin production process, organic concentration is high and fluctuation is big, mainly contains the organic pollution of the difficult volatilization such as ethylene glycol, propylene glycol, diglycol, low molecule polyester monocase, phthalic acid, maleic acid。
In the inventive method, the one-level condensation described in step (1) adopts condensing tower, and tower top arranges condensate pans, and tower body adopts the form of column plate and filler combination, more than polyester steam inlet is combined column plate, and theoretical cam curve is 3～15 pieces；Being packing section below polyester steam inlet, filler is stainless steel helices, ceramic ring filler or plastic filler etc.。Condensing tower entrance polyester vapor (steam) temperature is 190～220 DEG C, and tower top temperature is 105～120 DEG C, to ensure that steam steams from tower top；Column bottom temperature is 140～170 DEG C, can reduce condensed liquid phase and again evaporate, and is 5:1～50:1 by its gas/liquid weight ratio of steam inlet flow-control。In the present invention, condensed liquid phase Organic substance is back to tower top through packing section, and liquid-phase reflux ratio is 1～50。Polyester steam mid-boiling point condenses through layer by layer higher than Organic substances such as the ethylene glycol of water, propylene glycol and transfers to liquid phase from gas phase, is 90wt%～100wt% by organic content in liquid phase at the bottom of the tower that above-mentioned process is formed, and better value is 95wt%～100wt%。
In the inventive method, the B-grade condensation described in step (2) adopts common condenser, and inlet temperature is 105～120 DEG C, and outlet temperature is 40～60 DEG C, and heat exchange area is 15～25dm2。Condensed waste water COD is 10000～20000mg/L, BOD5Being 4000～5600mg/L, subsequent treatment can adopt biochemical treatment。
In the inventive method, the anaerobic treatment described in step (3) adopts anaerobic UASB reactor, and the water inlet volumetric loading of reactor is 4～10kgCOD/ (m3?D), retention time of sewage is 20～60h, and inflow temperature is 30～40 DEG C, and the methane gas content of collection is 55v%～70v%。
In the inventive method, the Aerobic Process for Treatment described in step (4) adopts contact-oxidation pool, and water inlet volumetric loading is 0.3～1.2kgCOD/ (m3?D), retention time of sewage is 6～12h, and gas-water ratio is 3:1～7:1。
Compared with the prior art, the polyester steam treatment method that the inventive method provides is without being condensed into high-concentration waste water by polyester steam, but by high boiling point difficulty volatile organic compounds such as the ethylene glycol in one-level condensation high efficiente callback polyester steam, propylene glycol, phthalic acid, maleic acids, there is not second-order phase transition in this process, the response rate is high, energy expenditure is low, and reduces subsequent treatment energy consumption。Remaining steam forms low concentration wastewater by B-grade condensation and carries out anaerobism, Aerobic Process for Treatment, and flow process is short, equipment is simple, stable operation, and after process, water outlet can qualified discharge。The method can reclaim substantial amounts of useful resources from polyester steam, turns waste into wealth, can realize again the qualified discharge of polyester steam, and the response rate is high, energy consumption is low, has good economic benefit and environmental benefit。
Accompanying drawing explanation
Fig. 1 is a kind of concrete unsaturated polyester (UP) steam treatment technique schematic flow sheet of the present invention。
Wherein: 10, first-stage condenser, 11, material storage tank, 12, secondary condenser, 13, effluent storage tank, 14, regulating reservoir, 15, anaerobic UASB, 16, air accumulator, 17, contact-oxidation pool, 18, sedimentation tank, 19, filter。
Fig. 2 is the concrete structure schematic diagram of first-stage condenser in the present invention。
Wherein: 1, steam inlet, 2, condensate pans, 3, steam (vapor) outlet, 4, refluxing opening, 5, liquid re-distributor, 6, column plate, 7, packing layer, 8, seal pot, 9, discharging opening。
Detailed description of the invention
Fig. 1 is a kind of concrete technological process of the present invention: the unsaturated polyester (UP) steam that polycondensation phase produces is introduced into first-stage condenser 10, Organic substance in steam is mainly the reaction masses such as ethylene glycol, propylene glycol, diethylene glycol, phthalic acid, maleic acid, these organic boiling points are all high than the boiling point of water, liquid phase oily Organic substance is formed in the bottom of first-stage condenser, recycling after material storage tank 11 is collected。All the other uncondensed vapor form low concentration polyester waste water by secondary condenser 12 and enter effluent storage tank 13, enter anaerobic UASB reactor 15 after mixed with the process water outlet of sedimentation tank in regulating reservoir 14, and the biogas of generation enters air accumulator 16。Anaerobic treatment water outlet enters in contact-oxidation pool 17 and carries out Aerobic Process for Treatment, and the degree of depth removes the Organic substance in waste water。Water outlet after aerobic treatment can qualified discharge after processing through sedimentation tank 18, filter 19。
Fig. 2 is the concrete structure schematic diagram of condenser of the present invention, detailed process is as follows: unsaturated polyester (UP) steam enters from condenser import department, the temperature of steam inlet 1 is about between 190～220 DEG C, top is provided with condensate pans 2, control its temperature between 105～120 DEG C, make the thermograde having 70～115 DEG C between the bottom of condenser and top, be 5:1～50:1 by its gas/liquid weight ratio of steam inlet flow-control。When polyester steam enters condenser, its steam rises from the bottom of tower to tower top, condenses layer by layer through column plate 6, makes gas phase mid-boiling point be transferred to liquid phase from gas phase gradually more than the Organic substance of water, and uncooled steam is discharged from outlet 3。Condensed liquid flows downward by after liquid re-distributor 5, after flowing through column plate 6, packing layer 7, enters seal pot 8, and a part of condensed liquid is back to condenser by refluxing opening 4 and is circulated, and liquid-phase reflux ratio is 1～50。Ranging for 90wt%～100wt% by content of organics in the liquid phase that discharging opening 9 place at the bottom of above-mentioned treating column generates, better value is 95wt%～100wt%。
Further illustrating the inventive method and effect by the examples below, wherein wt% is mass fraction, and v% is volume fraction。
Embodiment 1
The unsaturated polyester resin steam that polycondensation phase is produced by the technological process of Fig. 1 and the condenser of Fig. 2 is adopted to process。Unsaturated polyester resin is with diethylene glycol, ethylene glycol, propylene glycol, phthalic acid, maleic acid for main material production, and the discharge capacity of polyester steam is 500～3000Nm3/ h, in polyester steam, organic content is about 15wt%, and wherein the content of dihydroxylic alcohols is about the content of 12wt%, phthalic acid and maleic acid is 3wt%。Concrete operating condition and treatment effect are in Table 1。
Table 1 embodiment 1 main processing units and treatment effect
| Processing unit title | Process unit scale and mainly comprise | Main service condition and control parameter | Treatment effect |
| One-level condenses | First-stage condenser adopts the condensing tower of stainless steel, 16L, treating capacity 200Nm3/ H, with condensate pans and return-flow system, the number of plates is 6 pieces, adopts ceramic ring filler。 | Inlet temperature 200 DEG C, condensate pans temperature 120 DEG C, 160 DEG C of left sides of column bottom temperature The right side, gas/liquid weight ratio is 20:1, and liquid-phase reflux ratio is 10。 | In outlet vapor, glycol content is 0.8wt%, adjacent benzene two The content of formic acid and maleic acid is 0.1wt%, at the bottom of tower In liquid phase, content of organics is 95wt%。 |
| B-grade condensation | B-grade condensation is common condenser, and outside employing is cooling water circulation。 | Inlet temperature 120 DEG C, outlet temperature 60 DEG C, heat exchange area is 17.6 dm2。 | The waste water COD that condensation is formed is 12100 mg/L, BOD5 It is 5200 mg/L。 |
| Anaerobic treatment | Adopting UASB reactor, material is lucite, and reactor volume 40L mainly wraps Draw together water distributing plate, granule sludge bed, mud cushion, three phase separator, aerofluxus Pipe, drain pipe, screen cloth etc. are constituted。 | Inflow temperature is 38 DEG C, and volumetric loading is 8 kg COD/ (m3.D), waterpower is stopped Staying the time is 40 h, and collecting gases methane content is 60v%。 | Water outlet COD is less than 1200 mg/L, BOD5Less than 200 mg/L。 |
| Aerobic Process for Treatment | Adopting contact-oxidation pool, volume is 40L, hangs inside semi soft packing。Main bag Draw together water-distributing device, packing area, aerator and drainage system。 | Water inlet volumetric loading is 0.8 kg COD/ (m3.D), the time of staying is 9h, gas Water is than for 5:1。 | Water outlet COD is less than 100 mg/L, BOD5Less than 20 mg/ L。 |
| Precipitation filters | Adopt quartz sand filtration post, diameter 20 mm, high 50 mm。 | The rate of filtration is 20mL/min | Water outlet COD is less than 60 mg/L, BOD5Less than 20 mg/L。 |
Adopting the processing method of the present invention, water outlet COD is less than 60mg/L, BOD5Less than 20mg/L, it is possible to make the Organic substance in unsaturated polyester (UP) steam directly condense recovery when gas phase, the response rate is high。
Embodiment 2
Adopting the technological process of Fig. 1 and the condenser of Fig. 2, at different conditions the polyester steam identical with embodiment 1 is processed, concrete operating condition and treatment effect are in Table 2。
Table 2 embodiment 2 main processing units and treatment effect
| Processing unit name Claim | Process unit scale and mainly comprise | Main service condition and control parameter | Treatment effect |
| One-level condenses | First-stage condenser adopts stainless steel, 16L, treating capacity 200 Nm3/ h, with condensate pans With return-flow system, the number of plates is 6 pieces, adopts ceramic ring filler。 | Inlet temperature about 220 DEG C, condensate pans temperature 105 DEG C, column bottom temperature 140 DEG C, gas/liquid weight ratio is about 40:1, and reflux ratio is 50。 | In outlet vapor, glycol content is 0.6wt%, adjacent benzene two The content of formic acid and maleic acid is 0.08wt%, tower In end liquid phase, content of organics is 97.5wt%。 |
| B-grade condensation | Secondary condenser is common condenser, and outside employing is cooling water circulation。 | Inlet temperature 105 DEG C, outlet temperature 40 DEG C, heat exchange area is 17.6 dm2。 | The waste water COD that condensation is formed is 10500 mg/L, BOD5 It is 5000 mg/L。 |
| Anaerobic treatment | Adopting UASB anaerobic reactor, material is lucite, reactor volume 40L。Main bag Draw together water distributing plate, granule sludge bed, mud cushion, three phase separator, exhaustor, draining Pipe, screen cloth etc. are constituted。 | Inflow temperature is between 38 DEG C, and volumetric loading is 6 kg COD/ (m3.D), Hydraulic detention time is 53h, and collecting gases methane content is 68v%。 | Water outlet COD is less than 900 mg/L, BOD5Less than 180 mg/ L。 |
| Aerobic Process for Treatment | Adopting contact-oxidation pool, volume is 40L, hangs inside semi soft packing。Mainly include cloth Water device, packing area, aerator and drainage system。 | Water inlet volumetric loading is 0.6 kg COD/ (m3.D), the time of staying is 12h, gas-water ratio is 4:1。 | Water outlet COD is less than 80 mg/L, BOD5Less than 20 mg/L。 |
| Precipitation filters | Quartz sand filtration post, diameter 20 mm, high 50 mm。 | The rate of filtration is 20mL/min。 | Water outlet COD is less than 60 mg/L, BOD5Less than 20 mg/L。 |
Adopting the processing method of the present invention, it is possible to make the Organic substance in unsaturated polyester (UP) steam directly condense recovery when gas phase, the response rate is high, greatly reduces the energy consumption of subsequent treatment。Uncooled steam forms the polyester waste water of low concentration when time condensation, can reach first discharge standard after anaerobism, aerobic and filtration treatment。
Claims (9)
1. a processing method for unsaturated polyester (UP) steam, including herein below:
(1) one-level condensation, makes polyester steam mid-boiling point transfer to liquid phase higher than the Organic substance of water from gas phase, reduces organic concentration in steam；
(2) B-grade condensation, is condensed into low concentration polyester waste water by condensed for one-level steam；
(3) anaerobic treatment, after B-grade condensation, waste water carries out anaerobic treatment；
(4) Aerobic Process for Treatment, the waste water after anaerobic treatment carries out Aerobic Process for Treatment；
(5) precipitation filters, the discharge after precipitation, filtration of the water outlet after Aerobic Process for Treatment；
Described unsaturated polyester (UP) steam, from the polycondensation reaction stage in unsaturated polyester resin production process, mainly contains ethylene glycol, propylene glycol, diglycol, low molecule polyester monocase, phthalic acid and maleic acid。
2. in accordance with the method for claim 1, it is characterized in that: the one-level condensation described in step (1) adopts condensing tower, and tower top arranges condensate pans, and tower body adopts the form of column plate and filler combination, more than polyester steam inlet being combined column plate, theoretical cam curve is 3～15 pieces；It it is packing section below polyester steam inlet。
3. in accordance with the method for claim 2, it is characterised in that: the filler of packing section is stainless steel helices, ceramic ring filler or plastic filler。
4. in accordance with the method for claim 2, it is characterized in that: condensing tower entrance polyester vapor (steam) temperature is 190～220 DEG C, tower top temperature is 105～120 DEG C, and column bottom temperature is 140～170 DEG C, is 5:1～50:1 by its gas/liquid weight ratio of steam inlet flow-control。
5. the method described in claim 2 or 4, it is characterised in that: the condensed liquid phase Organic substance of one-level is back to tower top through packing section, and liquid-phase reflux ratio is 1～50。
6. in accordance with the method for claim 1, it is characterised in that: the B-grade condensation described in step (2) adopts common condenser, and inlet temperature is 105～120 DEG C, and outlet temperature is 40～60 DEG C, and heat exchange area is 15～25dm2。
7. the method described in claim 1 or 6, it is characterised in that: the waste water COD after B-grade condensation is 10000～20000mg/L, BOD5It is 4000～5600mg/L。
8. in accordance with the method for claim 1, it is characterised in that: the anaerobic treatment described in step (3) adopts anaerobic UASB reactor, and the water inlet volumetric loading of reactor is 4～10kgCOD/ (m3?D), retention time of sewage is 20～60h, and inflow temperature is 30～40 DEG C, and the methane gas content of collection is 55v%～70v%。
9. in accordance with the method for claim 1, it is characterised in that: the Aerobic Process for Treatment described in step (4) adopts contact-oxidation pool, and water inlet volumetric loading is 0.3～1.2kgCOD/ (m3?D), retention time of sewage is 6～12h, and gas-water ratio is 3:1～7:1。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210404075.7A CN103768822B (en) | 2012-10-23 | 2012-10-23 | A kind of processing method of unsaturated polyester (UP) steam |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210404075.7A CN103768822B (en) | 2012-10-23 | 2012-10-23 | A kind of processing method of unsaturated polyester (UP) steam |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103768822A CN103768822A (en) | 2014-05-07 |
| CN103768822B true CN103768822B (en) | 2016-06-22 |
Family
ID=50561864
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210404075.7A Active CN103768822B (en) | 2012-10-23 | 2012-10-23 | A kind of processing method of unsaturated polyester (UP) steam |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103768822B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104150679B (en) * | 2014-06-04 | 2015-12-30 | 广州擎天材料科技有限公司 | A kind ofly to save the area and the esterification waste water treatment system of the energy and method |
| CN115353261A (en) * | 2022-10-19 | 2022-11-18 | 威海蓝创环保设备有限公司 | Polyester waste water treatment system |
| CN115353262A (en) * | 2022-10-20 | 2022-11-18 | 威海蓝创环保设备有限公司 | Esterification wastewater treatment process |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1335197A (en) * | 2000-07-20 | 2002-02-13 | 中国石油化工集团公司 | Method of treating organic waste gas containing vapor |
| CN1458446A (en) * | 2002-05-15 | 2003-11-26 | 中国石油化工股份有限公司 | Method for purifying waste gas containing water soluble organism |
| CN1817417A (en) * | 2005-09-22 | 2006-08-16 | 中国石油化工股份有限公司 | Waste polyester gas purification |
| CN101456648A (en) * | 2008-12-30 | 2009-06-17 | 南京大学 | Polyester production waste water treatment method |
| CN101698556A (en) * | 2009-11-05 | 2010-04-28 | 北京美绿环境工程有限责任公司 | Treatment method and treatment device of wastewater from middle stage of wheat straw pulp paper-making |
| CN102504225A (en) * | 2011-10-23 | 2012-06-20 | 新疆蓝山屯河聚酯有限公司 | Vapor condensing and recovering device for use in production of polyester |
-
2012
- 2012-10-23 CN CN201210404075.7A patent/CN103768822B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1335197A (en) * | 2000-07-20 | 2002-02-13 | 中国石油化工集团公司 | Method of treating organic waste gas containing vapor |
| CN1458446A (en) * | 2002-05-15 | 2003-11-26 | 中国石油化工股份有限公司 | Method for purifying waste gas containing water soluble organism |
| CN1817417A (en) * | 2005-09-22 | 2006-08-16 | 中国石油化工股份有限公司 | Waste polyester gas purification |
| CN101456648A (en) * | 2008-12-30 | 2009-06-17 | 南京大学 | Polyester production waste water treatment method |
| CN101698556A (en) * | 2009-11-05 | 2010-04-28 | 北京美绿环境工程有限责任公司 | Treatment method and treatment device of wastewater from middle stage of wheat straw pulp paper-making |
| CN102504225A (en) * | 2011-10-23 | 2012-06-20 | 新疆蓝山屯河聚酯有限公司 | Vapor condensing and recovering device for use in production of polyester |
Non-Patent Citations (1)
| Title |
|---|
| 聚酯生产有机物废气催化燃烧处理工业应用;王新等;《当代化工》;20060830(第04期);第280页右栏第2-3段，图1，第281页左栏第4段 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103768822A (en) | 2014-05-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1298640C (en) | Resource process of inflitration liquid | |
| CN107244706B (en) | Treatment process of high-ammonia-nitrogen high-heavy-metal wastewater | |
| CN102167452B (en) | Method and system for treating landfill leachate | |
| CN101475280B (en) | Zero discharge wastewater treatment method, liquid membrane crystal wastewater evaporator and application system | |
| CN103224260A (en) | Wastewater treatment and recovery method | |
| WO2014094484A1 (en) | Garbage leachate treatment method and system | |
| CN105731724A (en) | Treating and recycling method for offshore-platform high-salt domestic wastewater | |
| CN105330110A (en) | Direct coal liquefaction sewage treatment system and method | |
| CN103288238B (en) | System for pure and impure printing and dyeing wastewater separation and wastewater recycling treatment | |
| CN107445802A (en) | A kind of method that ethylene glycol and acetaldehyde are reclaimed in polyester waste water | |
| CN104828887A (en) | Method for evaporative purifying treatment of wastewater by adopting solar combination heating, and system thereof | |
| CN103768822B (en) | A kind of processing method of unsaturated polyester (UP) steam | |
| CN101376550B (en) | Method for processing process waste water of dimethyl ether preparation by dehydrating methyl alcohol | |
| CN201280477Y (en) | HE-IC anaerobic reactor | |
| CN104628065A (en) | Chemical pharmaceutical wastewater treatment system and method | |
| CN105036325A (en) | Multi-phase reinforcement and guide type circular and anaerobic granulation reaction processing device | |
| CN205328797U (en) | Direct liquefaction of coal sewage treatment system | |
| CN106865858A (en) | Salty organic waste liquid processing method | |
| CN201292300Y (en) | Water producing and desalting integrated treatment apparatus for oil field | |
| CN205035148U (en) | Circulation anaerobism miniaturation reaction processing apparatus is led to heterogeneous intensive branch | |
| CN101475293A (en) | Wastewater treating and recycling process | |
| CN2598997Y (en) | Expansion particle sludge bed organic waste water anaerobic reactor | |
| CN103771649B (en) | Treatment method of 1,3-propanediol production wastewater | |
| CN110437052A (en) | System and preparation method that acetaldehyde prepares acetic acid are recycled from esterification waste water | |
| CN207227223U (en) | A kind of processing of gasification of poor coal waste water and recycle device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |