CN101152969B - Method of processing p-benzene dicarboxylic acid production wastewater - Google Patents
Method of processing p-benzene dicarboxylic acid production wastewater Download PDFInfo
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Abstract
The present invention provides a disposal method for wastewater produced by phthalic acid. The steps are as follows : a. the process wastewater exported from a refining process is filtered; filtrate and a solid-form object are gained; b. the filtrate is sent to and processed in a multi-effect evaporation system; steaming condensation water and condensation water with organic compound are gained; then the steaming condensation water is recycled back to the refining process and is reused; c. solid-liquid mixture is gained by adding acid to the condensation water and precipitating; the solid-form object and the filtrate are gained by processing a solid-liquid separation to the mixture; d. water and various organic compounds are gained by fractionating the filtrate; the water is recycled back to the refining process and is reused; the organic compounds are recycled back to a xylene oxidation process; e. various organic compounds are gained though the combination and re-crystallization of the solid-form object in the step a and the solid-form object in the step c. With the present invention, the majority of the PTA wastewater is capable of being recycled and reused in the production after being disposed; in addition, the majority of the organic compounds in wastewater are reclaimed. So the economical use of the PTA wastewater and the organic compounds in wastewater is realized.
Description
Technical field
The present invention relates to a kind of Industrial Wastewater Treatment and reuse method, the de-salted water in especially a kind of recovery pure terephthalic acid (being called for short PTA) factory effluent and the treatment process of organic materials.
Background technology
PTA is a kind of important chemical material, be widely used in the production of various synthetic resins, polyster fibre, plastics film, softening agent and coating, estimate in following 10 years, trevira, engineering plastics, powder coated resin will become a new consumption growth point in Chinese market, and their raw material all comes from PTA.
At present, the main production process of terephthalic acid is:
1. oxidation operation: raw material p-Xylol (PX) is made catalyzer with Cobaltous diacetate, manganese acetate in acetic aid medium, catalyzed oxidation is made the thick product of terephthalic acid (CTA).And therefore the p-methylbenzoic acid among the CTA (P-TA) and carboxyl benzaldehyde (4-CBA) intermediate product had a strong impact on the color and luster of esterification, polycondensation and polyester product in the follow-up polyester process must be removed.
2. refining step: CTA product and highly purified de-salted water that oxidation operation is obtained are mixed into slurry, under 280 ℃, the reaction conditions of 7-8MPa, with among the CTA the carboxyl benzaldehyde hydrogenating reduction is become p-methylbenzoic acid more soluble in water after, separate out the PTA crystal after step-down flash distillation step by step, the cooling.To contain PTA crystalline slurry and filter with Pressure Centrifuges, filter cake is delivered to the making beating jar and is pulled an oar once more with new de-salted water, and the impurity that remains among the TA is washed in the water, filters the back filter cake is carried out drying, obtains PTA.
Hydrofining reaction carries out under the catalysis of palladium charcoal (Pd/C) catalyzer, and this catalyzer costs an arm and a leg.As produce the device of 22.5 ten thousand tons of PTA per year, and generally needing to load 15 tons of catalyzer (being worth 5,280,000 yuan), be 1 year work-ing life the longest.The reason that causes catalyst deactivation is a lot, and wherein the water quality of process water has material impact to catalyst life.For the activity of guard catalyst and the work-ing life of prolongation catalyzer, in the PTA production technique, generally adopt highly purified de-salted water as solvent, therefore, refining step need use a large amount of de-salted waters.Under normal circumstances produce 1 ton of PTA and need consume de-salted water about 4 tons, the production equipment of 22.5 ten thousand tons of PTA/ of a cover output, annual about 1,000,000 tons of the de-salted water that consumes.After these de-salted waters used, water quality was polluted by the organism of technological process and inorganic salt, the annual unmanageable sewage of high density that produces about 1,000,000 tons.In the ordinary course of things, contain 0.5%-1% left and right sides TA, raw material and intermediate product in the high-concentration sewage that is produced, the about 5000-10000 ton organic materials of annual waste.
The sewage of PTA production process discharging is more unmanageable high density organic chemical industry sewage, pollutent mainly is terephthalic acid, p-Xylol, phenylformic acid, tolyl acid, phthalic acid, ritalin and a small amount of other organism, the chemical oxygen demand of sewage (COD) is generally the 2000-6000 mg/litre, and unstable, vary within wide limits.Because pollutent is constitutionally stable aromatics, than difficult for biological degradation, therefore, need to adopt the biochemical process of long flow process, just can make the sewage quality after the processing reach the environment protection emission requirement.In addition, owing to also contain metal ions such as certain density cobalt, manganese, calcium and magnesium in the water, cause the specific conductivity of water quality all higher.
At present, mainly be that the cooling back adopts active sludge treatment technology or employing anaerobic UASB+active contact oxidation technology to handle to these waste water that produce in the PTA production, make waste water quality satisfy emission request.Therefore, the water technology that adopts in PTA produces is not only wasted great lot of water resources, Chemicals and raw material, and is increased considerably the PTA production cost at present.
Domestic and foreign literature mainly contains following report to the treatment process of PTA factory effluent.
CN 1039784A proposes a kind of PTA Wastewater Treatment by pre-treatment, anaerobism, aerobic treatment combination, and process complexity, cycle are long.Processing intent is a qualified discharge, so processing requirements is lower.
CN 1033176A proposes a kind of method of terephthalic acid in the molysite preliminary sedimentation service water of using, and makes terephthalic acid become the terephthalic acid molysite deposition with ferric sulfate or iron trichloride, adds polyacrylamide and improves precipitation threshold, filters to remove and precipitates.The aromatic acid of this patent in can only preliminary sedimentation waste water there is no the removal effect to other organic impurity, and the iron ion of having brought at least 5 mg/litre in the water after handling into is given in the adding of molysite.
CN 1289725A complexometric extraction pretreating PTA waste water.At normal temperatures, select tributyl phosphate, trialkylphosphine oxide, trialkylamine as extraction agent, waste water is carried out multi-stage counter current extraction, making wherein, main component such as phenylformic acid and acetic acid is enriched in solvent phase, processed waste water COD
CrIt is original 1/6 that value is reduced to, and every index satisfies the requirement of biochemical processing process or other secondary method of edge treatment.This technology is a kind of preconditioning technique, and processing intent is qualified discharge equally.
US 4675108 proposes a kind of method of handling wash-down water in the crude terephthalic acid production process.Adopt the method for filtration, cationic exchange and anionresin to handle waste water.Though certain feasibility is arranged in theory, but practical application intermediate ion exchange resin is extremely tight to water quality requirement, suspended substance in the water and organism can be deposited on resin surface, cause that exchange capacity reduces and resin property damages, therefore general ion exchange bed allows water inlet COD value to be＜the 2-3 mg/litre, and the middle wash water of crude terephthalic acid production process contains a large amount of terephthalic acids, p-Xylol and other organic by-products, the COD value can't directly be carried out ion-exchange up to the 3000-8000 mg/litre at all.Therefore this patented technology realizes that industrialization acquires a certain degree of difficulty.
CN 1315295A, CN 1182053C respectively propose a kind of PTA production wastewater treatment method, adopt membrane sepn to separate with resin absorption, make to handle afterwards in the water COD value and reduce to 150mg/L.But membrane technique exists, and investment is high, working cost is high, operational conditions is harsh, require height and organism to the pollution of film and the problems such as work-ing life of film to influent quality, realize really that industrialization also needs to carry out macrocyclic experiment.
Above-mentioned document does not all relate to carrying out reuse after the wastewater treatment and reclaiming organic measure in the waste water.
Summary of the invention
The objective of the invention is the effluent reuse after handling to be made the de-salted water that technology requires for the waste water technology that overcomes existing treatment PTA generation, and can not reclaim organic deficiency in the waste water, propose a kind of most of waste water that PTA is produced and be back to production as the technology de-salted water after treatment, and the most of organism in the waste water can be reclaimed, realize the method for the organism recycling in PTA waste water and the waste water.
Production of Terephthalic Acid wastewater treatment method provided by the invention may further comprise the steps:
A. the processing wastewater of discharging from refining step obtains filtrate (1) and solid (2) after the filtration;
B. filtrate (1) is sent into multi-effect evaporation system and is carried out evaporation process, obtains steam condenses and contains organic concentrated solution (3);
C. concentrated solution (3) is added acid treatment, obtain solidliquid mixture (4), mixture is carried out solid-liquid separation, obtain solid (5) and filtrate (6);
D. filtrate (6) is carried out fractionation, obtain organism such as water and acetic acid, ritalin and p-Xylol respectively;
E. solid (2) and (5) are merged, carry out recrystallization, obtain various organism such as terephthalic acid, phenylformic acid, tolyl acid and phthalic acid respectively.
Wherein, among the step a, filtering system can be selected from least a in rotary vacuum filter, the Pressure Centrifuges etc.
Among the step b, filtrate can add alkali pH value of filtrate is transferred to 4～12 before sending into multi-effect evaporation system, and is preferred 6～9, to prevent the acetic acid evaporation in the filtrate and to cause the final organism amount that reclaims to reduce.Also can not add alkali.Alkali can be selected from least a in yellow soda ash, sodium hydroxide, sodium bicarbonate, the ammoniacal liquor etc.
Among the step b, multi-effect evaporation system is made up of 2～10 vaporizers, connects flow process between effect and can be following current, adverse current, advection or mixed flow.Preferred flow is the downflow system multiple-effect evaporator.The refining step filtrate filtered is pumped into first single-effect evaporator, final concentrated solution is imitated from the end and is discharged, because the filtrate temperature is higher, generally at 70～100 ℃, so multi-effect evaporation system does not need to use other heat energy or only needs a small amount of other heat energy, the secondary steam that first single-effect evaporator produces enters next and imitates as heating steam.Concentrated solution enters next and imitates the continuation evaporation under the differential pressure action between two effects.Each condensed water of imitating steam flows into corresponding flash tank, and the steam of generation also is introduced into next effect.So carry out imitating up to the end.Concentrated solution is finally imitated by the end and is discharged.2 to 10 condensed water of imitating the condenser generation are qualified process water, can turn back to exquisite operation and continue to use.
Among the step c, the acid that is added can be selected from least a in dilute sulphuric acid, hydrochloric acid, acetic acid, the nitric acid etc., below the pH regulator to 4 with concentrated solution, terephthaldehyde's Acid precipitation is separated out.
Steps d is carried out in separation column, and separation column can be packing tower or sieve-tray tower.The water that obtains can turn back to refining step and be used for making beating, and organism such as acetic acid, ritalin and p-Xylol can turn back to the p xylene oxidation operation and participate in reaction, still residual liquor discharge again;
In sum, the present invention possesses following outstanding advantage as can be seen:
1) compared with former method of wastewater treatment, the method of advanced treatment PTA factory effluent provided by the invention can realize that the PTA factory effluent is as technology de-salted water direct reuse, the rate of recovery of high-purity water is approximately 50～90%, realizes that process water truly recycles.
2) the present invention reclaims the organism in the refining step waste water, realizes the recycling of refuse.
3) the present invention is used for multi-effect evaporation system the processing of PTA waste water, and the temperature that has made full use of continuous waste water is imitated the thermal source that evaporates as first, therefore when high-purity water reuse, organism reclaim, realize energy recovery, improved the service efficiency of the energy.
4) technical process of the present invention is simple, treatment effect good, workable, wide to the water quality scope of application, working cost is lower, has also saved the expense of handling fresh process water simultaneously.
Description of drawings
Fig. 1 is a PTA production wastewater treatment process flow diagram provided by the invention.
Embodiment
Except as otherwise noted, the percentage ratio in each example is weight percentage.
Embodiment 1
1. raw material waste water is taken from the continuous waste water of refining step of PTA production equipment, and is mainly composed as follows:
Terephthalic acid 0.25%
P-methylbenzoic acid 0.079%
Phenylformic acid 0.007%
Acetic acid 0.1%～0.2%
pH ～2.5
COD ～2800mg/L
Raw material waste water at first filters through rotary vacuum filter, and vacuum tightness is elected (0.4～0.8) * 10 as
5Pa, filtering rate is 1.5m
3/ min.Obtain solid substance (2) and filtrate (1)
2. filtrate (1) is directly sent into 5 effect vapo(u)rization systems, and the gained condensed water is composed as follows behind the multiple-effect evaporation, can be used as process water and is back to use refining step, and the de-salted water rate of recovery is 80%.
Terephthalic acid～0
Specific conductivity≤1.0 μ s/cm
Copper≤0.2 mg/litre
Iron≤0.5 mg/litre
Silicide≤3.0 mg/litre
Sulfide is (with SO
4 2-Meter)≤60.0 mg/litre
Total solids≤5.0 mg/litre
Total metal (cobalt, manganese, nickel, chromium etc.) ,≤1.5 mg/litre
The gained concentrated solution is composed as follows:
Terephthalic acid 1.3%
P-methylbenzoic acid 0.4%
Phenylformic acid 0.04%
Acetic acid 0.5～1.0%
Concentrated solution is regulated pH＜4 with sulfuric acid, and the heavy after-filtration of acid obtains solid substance (5) and filtrate (6), and recrystallization is carried out in solid substance (2) and (5), reclaims organism such as terephthalic acid, phenylformic acid, p-methylbenzoic acid and phthalic acid wherein.Filtrate (6) send separation column further to separate, and acetic acid, ritalin and the p-Xylol that obtains is turned back to oxidation operation react again, and water turns back to refining step and is used for making beating, still residual liquor discharge.
Embodiment 2
1. raw material waste water is taken from the continuous waste water of refining step of PTA production equipment, and is composed as follows:
Terephthalic acid 0.47%
P-methylbenzoic acid 0.1%
Phenylformic acid 0.08%
Acetic acid 0.1%～0.2%
pH ～2.8
COD ～2500mg/L
Raw material waste water filters through vacuum filter, and filtering velocity is 1.8m
3/ min.The neutralization of repeated hydrogenation sodium oxide, transferring waste water ph is about 7.
2. in and after filtrate send into 2 and imitate vapo(u)rization systems, the gained condensed water is composed as follows behind the multiple-effect evaporation, can be used as process water and is back to use refining step, the de-salted water rate of recovery is 50%.
Terephthalic acid～0
Specific conductivity≤1.0 μ s/cm
Copper≤0.2 mg/litre
Iron≤0.5 mg/litre
Silicide≤2.0 mg/litre
Sulfide is (with SO
4 2-Meter)≤5.0 mg/litre
Total solids≤5.0 mg/litre
Total metal (cobalt, manganese, nickel, chromium etc.) ,≤1.5 mg/litre
The gained concentrated solution is composed as follows:
Terephthalic acid 1.0%
P-methylbenzoic acid 0.2%
Phenylformic acid 0.2%
Acetic acid 0.3%
Concentrated solution is transferred pH＜4 with acetic acid, the heavy back of acid according to the mode of embodiment 1 filter, recrystallization, reclaim organism such as terephthalic acid, phenylformic acid, p-methylbenzoic acid and phthalic acid wherein, filtrate is delivered to the sieve plate separation column and is further separated, acetic acid, ritalin and the p-Xylol that obtains turned back to oxidation operation react again, the still residual liquor discharge.
Embodiment 3
1. raw material waste water is taken from the continuous waste water of refining step of PTA production equipment, and is composed as follows:
Terephthalic acid 0.86%
P-methylbenzoic acid 0.15%
Phenylformic acid 0.06%
Acetic acid 0.1%～0.2%
pH ～2.8
COD ～2400mg/L
Raw material waste water separates solid substance through Pressure Centrifuges.
2. filtrate is sent into 10 effect vapo(u)rization systems, and the gained condensed water is composed as follows behind the multiple-effect evaporation, can be used as process water and is back to use refining step, and the de-salted water rate of recovery is 90%.
Terephthalic acid～0
Specific conductivity≤1.0 μ s/cm
Copper≤0.2 mg/litre
Iron≤0.5 mg/litre
Silicide≤3.0 mg/litre
Sulfide is (with SO
4 2-Meter)≤60.0 mg/litre
Total solids≤5.0 mg/litre
Total metal (cobalt, manganese, nickel, chromium etc.) ,≤1.5 mg/litre
The gained concentrated solution is composed as follows:
Terephthalic acid 8.6%
P-methylbenzoic acid 2.0%
Phenylformic acid 0.6%
Acetic acid 2.0%
Concentrated solution is transferred pH＜4 with hydrochloric acid, the heavy back of acid according to the mode of embodiment 1 filter, recrystallization, reclaim organism such as terephthalic acid, phenylformic acid, p-methylbenzoic acid and phthalic acid wherein, filtrate send separation column further to separate wherein partial organic substances.
Embodiment 4
1. raw material waste water is taken from the continuous waste water of refining step of PTA production equipment, and is composed as follows:
Terephthalic acid 0.36%
P-methylbenzoic acid 0.15%
Phenylformic acid 0.06%
Acetic acid 0.1%～0.2%
pH ～2.8
COD ～2400mg/L
Raw material waste water at first filters through rotary vacuum filter, and vacuum tightness is elected (0.4～0.8) * 10 as
5Pa, filtering velocity is 1.5m
3/ min.
2. filtrate is sent into 5 effect vapo(u)rization systems, and the gained condensed water is composed as follows behind the multiple-effect evaporation, can be used as process water and is back to use refining step, and the de-salted water rate of recovery is 80%.
Terephthalic acid～0
Specific conductivity≤1.0 μ s/cm
Copper≤0.2 mg/litre
Iron≤0.5 mg/litre
Silicide≤3.0 mg/litre
Sulfide is (with SO
4 2-Meter)≤60.0 mg/litre
Total solids≤5.0 mg/litre
Total metal (cobalt, manganese, nickel, chromium etc.) ,≤1.5 mg/litre
The gained concentrated solution is composed as follows:
Terephthalic acid 1.8%
P-methylbenzoic acid 0.8%
Phenylformic acid 0.3%
Acetic acid 0.4%
Concentrated solution is transferred pH＜4 with nitric acid, and the heavy back of acid is according to the mode filtered and recycled organism wherein of embodiment 1, and filtrate send separation column further to separate wherein partial organic substances.
Embodiment 5
1. raw material waste water is taken from the continuous waste water of refining step of PTA production equipment, and is composed as follows:
Terephthalic acid 0.32%
P-methylbenzoic acid 0.15%
Phenylformic acid 0.06%
Acetic acid 0.1%～0.2%
pH ～2.8
COD ～2400mg/L
Raw material waste water at first filters through rotary vacuum filter, and vacuum tightness is elected (0.4～0.8) * 10 as
5Pa, the filtration productive rate is 1.5m
3/ min.Filtrate is about 8 with the yellow soda ash adjust pH again.
2. in and after filtrate send into 3 and imitate vapo(u)rization systems, the gained condensed water is composed as follows behind the multiple-effect evaporation, can be used as process water and is back to use refining step, the de-salted water rate of recovery is 64%.
Terephthalic acid～0
Specific conductivity≤1.0 μ s/cm
Copper≤0.2 mg/litre
Iron≤0.5 mg/litre
Silicide≤3.0 mg/litre
Sulfide is (with SO
4 2-Meter)≤60.0 mg/litre
Total solids≤5.0 mg/litre
Total metal (cobalt, manganese, nickel, chromium etc.) ,≤1.5 mg/litre
The gained concentrated solution is composed as follows:
Terephthalic acid 1.0%
P-methylbenzoic acid 0.2%
Phenylformic acid 0.6%
Acetic acid 0.6%
Concentrated solution is regulated pH＜4 with sulfuric acid, and the heavy back of acid is according to the mode filtered and recycled organism wherein of embodiment 1, and filtrate send separation column further to handle.
Claims (9)
1. Production of Terephthalic Acid wastewater treatment method may further comprise the steps:
A. the processing wastewater of discharging from refining step filters, and obtains filtrate and solid;
B. filtrate is sent into multi-effect evaporation system and carried out evaporation process, obtain steam condenses and contain organic concentrated solution, steam condenses is back to use refining step, recycles as process water;
C. add acid with below the concentrated solution pH regulator to 4, separate out terephthaldehyde's Acid precipitation, obtain solidliquid mixture, mixture is carried out solid-liquid separation, obtain solid and filtrate;
D. filtrate is carried out fractionation, obtain water and various organism;
E. the solid with step a and step c merges, and carries out recrystallization, obtains various organism.
2. according to the described treatment process of claim 1, it is characterized in that among the step a, filtering system is selected from least a in rotary vacuum filter or the Pressure Centrifuges.
3. according to the described treatment process of claim 1, it is characterized in that among the step b, filtrate added alkali pH value of filtrate is transferred to 4～12 before sending into multi-effect evaporation system.
4. according to the described treatment process of claim 3, it is characterized in that, add alkali pH value of filtrate is transferred to 6～9.
5. according to the described treatment process of claim 1, it is characterized in that among the step b, multi-effect evaporation system is made up of 2～10 vaporizers.
6. according to the described treatment process of claim 1, it is characterized in that steps d is carried out in separation column.
7. according to the described treatment process of claim 6, it is characterized in that separation column is packing tower or sieve-tray tower.
8. according to the described treatment process of claim 1, it is characterized in that in the steps d, water turns back to refining step and is used for making beating.
9. according to the described treatment process of claim 1, it is characterized in that in the steps d, organism turns back to the p xylene oxidation operation and participates in reaction again.
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| CN2006101135001A CN101152969B (en) | 2006-09-29 | 2006-09-29 | Method of processing p-benzene dicarboxylic acid production wastewater |
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| CN2006101135001A CN101152969B (en) | 2006-09-29 | 2006-09-29 | Method of processing p-benzene dicarboxylic acid production wastewater |
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| CN101152969B true CN101152969B (en) | 2011-01-19 |
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Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102137707B (en) * | 2008-08-26 | 2013-08-21 | 瑞来斯实业公司 | Process and equipment for recovery of valuable materials from terephthalic acid manufacture |
| CN101928089B (en) * | 2009-06-26 | 2012-05-30 | 中国石油化工股份有限公司 | Method for disposing antiosmosis thick water out of purified terephthalic acid refined waste water |
| CN101941901B (en) * | 2010-08-16 | 2013-04-17 | 福州大学 | Method for recycling mother solid in PTA-refining wastewater |
| CN102249454A (en) * | 2011-05-17 | 2011-11-23 | 李大伟 | Method for comprehensively utilizing PTA (pure terephthalic acid) wastewater containing solid particles |
| CN102910778B (en) * | 2011-08-01 | 2014-07-23 | 施冬梅 | Terylene alkali reduction water resource recovery process |
| CN102875354A (en) * | 2012-10-31 | 2013-01-16 | 南京工业大学 | Method for recovering acetic acid from crude terephthalic acid filter cake |
| CN103482715B (en) * | 2013-09-16 | 2016-03-16 | 惠州Tcl环境科技有限公司 | A kind of high concentrated organic wastewater evaporation concentration treatment process |
| CN105585212B (en) * | 2015-12-24 | 2018-02-09 | 南京科技职业学院 | A kind of PTA produces waste water method for reusing synthesized |
| TWI574925B (en) * | 2016-03-09 | 2017-03-21 | Chung-Fu Wang | Treatment of Polycarboxylic Acid Residues |
| CN106219823A (en) * | 2016-08-31 | 2016-12-14 | 浙江奇彩环境科技股份有限公司 | A kind of processing method containing aminobenzoic acids waste water |
| CN106927633A (en) * | 2017-04-01 | 2017-07-07 | 来安县万博丰环保科技有限公司 | A kind of crude terephthalic acid production wastewater treatment system |
| CN111186948A (en) * | 2018-11-15 | 2020-05-22 | 中国石油天然气股份有限公司 | Treatment method of electric desalting and decalcification wastewater |
| CN112851492A (en) * | 2021-03-02 | 2021-05-28 | 天津科技大学 | Method for recovering benzoic acid from sodium benzoate-containing wastewater |
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| US4939297A (en) * | 1989-06-05 | 1990-07-03 | Eastman Kodak Company | Extraction process for removal of impurities from terephthalic acid filtrate |
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Correction item: Patentee|Address|Co-patentee Correct: Sinopec Corp.|100029 Beijing City, Chaoyang District Hui Street No. 6|SINOPEC Research Institute of Petroleum Processin False: SINOPEC Research Institute of Petroleum Processin|100083 No. 18, Haidian District, Beijing, Xueyuan Road Number: 03 Volume: 27 |
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Correction item: Patentee|Address|Co-patentee Correct: Sinopec Corp.|100029 Beijing City, Chaoyang District Hui Street No. 6|SINOPEC Research Institute of Petroleum Processin False: SINOPEC Research Institute of Petroleum Processin|100083 No. 18, Haidian District, Beijing, Xueyuan Road Number: 03 Page: The title page Volume: 27 |
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Free format text: CORRECT: PATENTEE; ADDRESS; CO-PATENTEE; FROM: SINOPEC CORP. RESEARCH INSTITUTE OF PETROLEUM PROCESSING;100083 NO. 18, XUEYUAN ROAD, HAIDIAN DISTRICT, BEIJING TO: CHINA PETROCHEMICAL CO., LTD.;100029 NO. 6-A, HUIXIN EAST STREET, CHAOYANG DISTRICT, BEIJING; SINOPEC CORP. RESEARCH INSTITUTE OF PETROLEUM PROCESSING |