CN102092875B - Chemical waste water treatment method in the process of producing 2,6 acid - Google Patents
Chemical waste water treatment method in the process of producing 2,6 acid Download PDFInfo
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- CN102092875B CN102092875B CN2010105804237A CN201010580423A CN102092875B CN 102092875 B CN102092875 B CN 102092875B CN 2010105804237 A CN2010105804237 A CN 2010105804237A CN 201010580423 A CN201010580423 A CN 201010580423A CN 102092875 B CN102092875 B CN 102092875B
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- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000002253 acid Substances 0.000 title claims description 36
- 238000004065 wastewater treatment Methods 0.000 title abstract 3
- 239000002894 chemical waste Substances 0.000 title 1
- 239000002351 wastewater Substances 0.000 claims abstract description 34
- 229920005989 resin Polymers 0.000 claims abstract description 28
- 239000011347 resin Substances 0.000 claims abstract description 28
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 20
- 239000000126 substance Substances 0.000 claims abstract description 19
- 238000003795 desorption Methods 0.000 claims abstract description 15
- 238000001704 evaporation Methods 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000003513 alkali Substances 0.000 claims abstract description 5
- 238000001914 filtration Methods 0.000 claims abstract description 5
- 239000012670 alkaline solution Substances 0.000 claims abstract description 3
- 238000007599 discharging Methods 0.000 claims abstract description 3
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 3
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 3
- 239000000243 solution Substances 0.000 claims abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 21
- PJKVFARRVXDXAD-UHFFFAOYSA-N 2-naphthaldehyde Chemical compound C1=CC=CC2=CC(C=O)=CC=C21 PJKVFARRVXDXAD-UHFFFAOYSA-N 0.000 claims description 19
- 238000010521 absorption reaction Methods 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 14
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical group OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 9
- 230000008020 evaporation Effects 0.000 claims description 8
- 208000006558 Dental Calculus Diseases 0.000 claims description 6
- 239000003463 adsorbent Substances 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical class C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 claims description 4
- 239000013078 crystal Substances 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical group [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 4
- 150000001298 alcohols Chemical class 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- NIXOWILDQLNWCW-UHFFFAOYSA-N Acrylic acid Chemical class OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 2
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical class C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 2
- 238000007334 copolymerization reaction Methods 0.000 claims description 2
- 150000002148 esters Chemical class 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 2
- 230000007935 neutral effect Effects 0.000 claims description 2
- 239000003352 sequestering agent Substances 0.000 claims description 2
- 150000003568 thioethers Chemical group 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- KAUQJMHLAFIZDU-UHFFFAOYSA-N 6-Hydroxy-2-naphthoic acid Chemical compound C1=C(O)C=CC2=CC(C(=O)O)=CC=C21 KAUQJMHLAFIZDU-UHFFFAOYSA-N 0.000 abstract description 6
- 238000001179 sorption measurement Methods 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000001816 cooling Methods 0.000 abstract description 2
- 239000012452 mother liquor Substances 0.000 abstract description 2
- JWAZRIHNYRIHIV-UHFFFAOYSA-N 2-naphthol Chemical compound C1=CC=CC2=CC(O)=CC=C21 JWAZRIHNYRIHIV-UHFFFAOYSA-N 0.000 abstract 6
- 229950011260 betanaphthol Drugs 0.000 abstract 3
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 abstract 2
- 229910052939 potassium sulfate Inorganic materials 0.000 abstract 2
- 235000011151 potassium sulphates Nutrition 0.000 abstract 2
- 238000004062 sedimentation Methods 0.000 abstract 2
- 239000000706 filtrate Substances 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- 229920000106 Liquid crystal polymer Polymers 0.000 description 3
- 239000004977 Liquid-crystal polymers (LCPs) Substances 0.000 description 3
- 239000012065 filter cake Substances 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 239000001103 potassium chloride Substances 0.000 description 2
- 235000011164 potassium chloride Nutrition 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 101100412856 Mus musculus Rhod gene Proteins 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 230000021523 carboxylation Effects 0.000 description 1
- 238000006473 carboxylation reaction Methods 0.000 description 1
- 229920001429 chelating resin Polymers 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
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- 239000000047 product Substances 0.000 description 1
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- Water Treatment By Sorption (AREA)
Abstract
A wastewater treatment method relates to a treatment method of the chemical wastewater generated in the production of 6-hydroxy-2-naphthalene carboxylic acid. The method comprises the following steps: firstly, cooling the wastewater to the room temperature, filtering to obtain partial 2-hydroxy naphthalene and partial 6-hydroxy-2-naphthalene carboxylic acid; secondly, sending a filtrate to a resin adsorption tower, eluting with an alkaline solution or alcohol after the saturation adsorption of resins, treating a high concentration desorption solution to obtain 2-hydroxy naphthalene and 6-hydroxy-2-naphthalene carboxylic acid; and finally sending the treated mother liquor to a sedimentation tank, adding a sedimentation agent to remove heavy metals, adding alkali for neutralization, evaporating to obtain potassium sulfate and recycling or discharging the treated effluent. By adopting the wastewater treatment method, the chemical wastewater generated in the production of 6-hydroxy-2-naphthalene carboxylic acid is fully treated, meets the environmental standard and can be directly discharged; and useful resources such as 2-hydroxy naphthalene, 6-hydroxy-2-naphthalene carboxylic acid, potassium sulfate and the like can be recycled, the discharged water and resources can be reused and the production cost can be effectively reduced.
Description
Technical field
The present invention relates to the improvement method of waste water, specially refer to the improvement method of the chemical wastewater in 2,6 productions.
Background technology
At present.2; 6 acid are that 2-hydroxyl 6-naphthoic acid (HNA) is a kind of emerging fine-chemical intermediate; Not only be widely used in the industry of medicine industry and pigment dyestuff, and aspect II type heat modification liquid crystal polymer (Thermotropic Liquid Crystallicin Polymer is called for short TLCP) synthetic, more fine application prospect arranged.This kind liquid crystal polymer has good heat-resistant and processing characteristics, in recent years along with the develop rapidly of electronics and IT industry, and the demand rapid growth of liquid crystal polymer; The also accelerated growth of demand of 2,6 acid, according to statistics; The growth of whole world annual requirement keeps the double-digit growth rate; More keep the rapid growth rate in the area, Asia, rate of increase is up to 30%, and this rapid growth rate will be kept in nearly 10 years.Yet, use Koble-Schmitt reaction with beta naphthal as raw material production 2,6 sour processes in, the sylvite that utilizes beta naphthal at high temperature and carbonic acid gas carry out the sylvite that the carbon carboxylation obtains 2,6 acid, carry out acidifying again and obtain 2,6 acid.But because the yield factor of the generation of chemical reaction and raising reaction, production process will inevitably produce chemical wastewater.These chemical wastewaters are yellow acidic liq, Ph1～2, and containing acid concentration is 0.05～0.1%, does not meet requirement on environmental protection, must administer.Contain useful resource such as beta naphthal, 2,6 acid, vitriolate of tartar in these chemical wastewaters simultaneously, reclaim these resources, particularly reclaim the domestic comparatively potassium resource of shortage, bigger realistic meaning is arranged.
Summary of the invention
The technical problem that the present invention will solve is to overcome deficiency of the prior art, proposes a kind of improvement method of waste water, has both reduced the organic impurity in the waste water, makes it to reach emission standard; Reclaim the efficient resource in the waste water again, reduce the production cost of 2,6 acid.
The present invention realizes through following technical measures.The improvement method of the chemical wastewater during a kind of 2,6 acid are produced,
(1) waste water is cooled to normal temperature, and filters, crystal block section is beta naphthal and 2,6 acid;
(2) filtrating is sent into the resin absorption tower, use is directly discharged or reclaimed to absorption effluent;
(3) after resin absorption is saturated, carry out wash-out with desorbing agent, described desorbing agent is alkaline solution or alcohols, and high concentration desorption liquid obtains beta naphthal and 2,6 acid through handling, and light concentration desorption liquid then is used to prepare the next batch desorbing agent;
(4) above-mentioned treated high concentration desorption liquid gets into settling bowl, adds sinking agent and removes heavy metal, adds the alkali neutralization, obtains vitriolate of tartar through evaporation, steams the then recyclable or discharging of water.
At this, represent the precedence of these reactions step with (1)～(3).
Required protection domain of the present invention though claims of the present invention particularly point out and know, should believe that description will understand the present invention better.
Resin as absorption is the product that vinylbenzene, divinylbenzene, vinylformic acid or ester derivative homopolymerization or copolymerization obtain, and what preferentially select is the macroporous adsorbent resin of non-ionic type.Like the Amberlite XAD series of U.S. Rhom and Hass, the HP series of Mitsubishi Chemical, the polymeric adsorbent that home-made DA201 is serial and similar etc.
Temperature 0-60 ℃ of absorption, flow velocity be (0.5-20) * resin bed volume/hour, adsorbing wastewater volume is (5-40) * resin bed volume.
Described desorbing agent is the sodium hydroxide solution of concentration between 1%-20%, and eluting temperature is 20-90 ℃, flow velocity be (0.5-10) * resin bed volume/hour.High concentration desorption liquid can reclaim beta naphthal and 2,6 acid through acid out and filtering mode.
Described desorbing agent is pure time-like, and desorbing agent is methyl alcohol and ethanol, and when using the alcohols desorbing agent, its desorption temperature is controlled at than low 5-20 ℃ of this pure boiling point.High concentration desorption liquid can separate pure and mild recovery beta naphthal and 2,6 acid through evaporation mode.
Described sinking agent is sequestrant and gacs such as sulphide salt, EDTA.
Described sinking agent is a Sodium Sulphide.
As neutral alkali is Pottasium Hydroxide or sodium hydroxide.
After the present invention adopted abovementioned technology, the chemical wastewater in 2,6 acid are produced was administered fully, can directly discharge after reaching environmental protection standard.At the same time, useful resource such as beta naphthal, 2,6 acid, vitriolate of tartar obtain reclaiming, and the particularly domestic comparatively recovery of the potassium resource of shortage has bigger realistic meaning.These resource reusings in production, can be reduced production costs.
Description of drawings
Accompanying drawing 1 is the front-end process synoptic diagram of the embodiment of the invention 1.
Accompanying drawing 2 is the rear end schematic flow sheet of the embodiment of the invention 1.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is described further.
Embodiment 1:
Get the waste water that 2000 milliliter of 2,6 acid produces in producing, wastewater temperature is more than 40 ℃, and outward appearance be yellow, and pH value is at 1-2, (the about 1.2g/L of beta naphthal in interior, 2,6 sour about 0.6g/L).At first waste water is cooled to normal temperature, and filters, the crystal block section of acquisition is beta naphthal 0.4g and 2,6 sour 0.2g.Still contain the about 0.8g/L of beta naphthal in the filtrating, the about 0.4g/L of 2,6 acid, COD is about 8000.Filtrating is through resin tower under 0.5* resin bed volume/hour (50ml/hr) flow conditions at 25 ℃, flow velocity; The glass adsorption column of the φ 30 * 300mm that has chuck and the DA201-B macroporous adsorbent resin of the 100ml that packs into are arranged in the resin tower, and absorption effluent COD can directly discharge below 100; Through 4 hours absorption, resin absorption was saturated.Carry out wash-out with 5% sodium hydroxide, 80 ℃ of eluting temperatures, flow velocity are 1* resin bed volume/hour (300ml/hr), and wash-out finishes after 2 hours, and elutriant is high dense desorption liquid; Use the 200ml water elution then, elutriant can be used for preparing diluted alkaline as the next batch elutriant for low dense desorption liquid.High dense desorption liquid is used 30% sulfuric acid acidation, filters, and reclaims in the filter cake and obtains beta naphthal 0.8g, 2,6 sour 0.4g once more.The mother liquor waste water that filtration finishes adds 1g Sodium Sulphide, stirs, and drips 30% sodium hydroxide adjusting PH to 7, filters again, and filter cake is the solid waste of otherwise processed; Filtrating then evaporation obtains the 92.6g vitriolate of tartar, and the water COD that evaporation obtains can reclaim use below 50.
Embodiment 2:
Get the waste water that 4000 milliliter of 2,6 acid produces in producing, wastewater temperature is more than 40 ℃, and outward appearance be yellow, and pH value is at 1-2, (the about 2.4g/L of beta naphthal in interior, 2,6 sour about 1.2g/L).At first waste water is cooled to normal temperature, and filters, the crystal block section of acquisition is beta naphthal 0.8g and 2,6 sour 0.4g.Still contain the about 1.6g/L of beta naphthal in the filtrating, the about 0.8g/L of 2,6 acid, COD is about 8000.Filtrating is through resin tower under 10* resin bed volume/hour (2000ml/Hr) flow conditions at 25 ℃, flow velocity; The glass adsorption column of the φ 40 * 500mm that has chuck and the DA201-B macroporous adsorbent resin of the 200ml that packs into are arranged in the resin tower, and absorption effluent COD can directly discharge below 100; Through 2 hours absorption, resin absorption was saturated.Carry out wash-out with methyl alcohol, 45 ℃ of eluting temperatures, flow velocity are 1* resin bed volume/hour (200ml/hr), and wash-out finishes after 2 hours.Elutriant evaporates, and the methyl alcohol-conduct that obtains out recycles, and the cooling of distillation remaining liq, filtration obtain solid and contain 1.6g2-naphthols and 0.8g2,6 acid.
The waste water that absorption finishes adds 2g Sodium Sulphide, stirs, and drips 30% sodium hydroxide adjusting PH to 7, filters, and filter cake is the solid waste of otherwise processed; Filtrating then evaporation obtains about 190g vitriolate of tartar, and the water COD that evaporation obtains can qualified discharge below 50.
Above-described only is preferred implementation of the present invention.Should be pointed out that for the person of ordinary skill of the art under the prerequisite that does not break away from the principle of the invention, can also make some modification and improvement, these also should be regarded as belonging to protection scope of the present invention.
Claims (9)
1. the improvement method of the chemical wastewater during an acid is produced is characterized in that:
(1) waste water is cooled to normal temperature, and filters, crystal block section is beta naphthal and 2,6 acid;
(2) filtrating is sent into the resin absorption tower, after resin absorption is saturated, carry out wash-out with desorbing agent; Described desorbing agent is alkaline solution or alcohols, and high concentration desorption liquid obtains beta naphthal and 2 through handling; 6 acid, light concentration desorption liquid then are used to prepare the next batch desorbing agent;
(3) above-mentioned treated high concentration desorption liquid gets into settling bowl, adds sinking agent and removes heavy metal, adds the alkali neutralization, obtains vitriolate of tartar through evaporation, steams the then recyclable or discharging of water;
At this, represent the precedence of these reactions step with (1)～(3).
2. the improvement method of the chemical wastewater during a kind of 2,6 acid according to claim 1 are produced, it is characterized in that: the resin as absorption is the product that vinylbenzene, divinylbenzene, vinylformic acid or ester derivative homopolymerization or copolymerization obtain.
3. the improvement method of the chemical wastewater during a kind of 2,6 acid according to claim 1 are produced, it is characterized in that: the resin as absorption is the macroporous adsorbent resin of non-ionic type.
4. the improvement method of the chemical wastewater during a kind of 2,6 acid according to claim 1 are produced, it is characterized in that: the temperature of absorption is 0-60 ℃, flow velocity be (0.5-20) * resin bed volume/hour.
5. according to claim 1 a kind of 2; The improvement method of the chemical wastewater during 6 acid are produced; It is characterized in that: described desorbing agent is the sodium hydroxide solution of concentration between 1%-20%, and eluting temperature is 20-90 ℃, flow velocity be (0.5-10) * resin bed volume/hour; High concentration desorption liquid reclaims beta naphthal and 2,6 acid through acid out and filtering mode.
6. according to claim 1 a kind of 2; The improvement method of the chemical wastewater during 6 acid are produced, it is characterized in that: described desorbing agent is pure time-like, desorbing agent is methyl alcohol and ethanol; High concentration desorption liquid separates pure and mild recovery beta naphthal and 2,6 acid through evaporation mode.
7. the improvement method of the chemical wastewater during a kind of 2,6 acid according to claim 1 are produced, it is characterized in that: described sinking agent is sulphide salt, EDTA sequestrant and gac.
8. the improvement method of the chemical wastewater during a kind of 2,6 acid according to claim 1 are produced, it is characterized in that: described sinking agent is a Sodium Sulphide.
9. the improvement method of the chemical wastewater during a kind of 2,6 acid according to claim 1 are produced, it is characterized in that: as neutral alkali is Pottasium Hydroxide or sodium hydroxide.
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Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102659576A (en) * | 2012-05-02 | 2012-09-12 | 苏州思睿屹新材料股份有限公司 | Refining method for 2-hydroxyl-6-naphthoic acid |
| CN102963960B (en) * | 2012-12-21 | 2014-07-16 | 南京大学 | Method for simultaneously recycling sulfuric acid and organic substances in m-cresol production wastewater |
| CN103848472B (en) * | 2014-01-13 | 2016-03-09 | 洛阳智方环保技术有限公司 | A kind of phenolic wastewater removes device and removing process thereof |
| CN104826376A (en) * | 2015-04-30 | 2015-08-12 | 安徽扬子化工有限公司 | Waste liquid filtering equipment |
| CN106565052A (en) * | 2015-10-09 | 2017-04-19 | 杭州天创环境科技股份有限公司 | Technological processing method for phenolic wastewater in petrochemical engineering production |
| CN105481156A (en) * | 2015-12-11 | 2016-04-13 | 凯天环保科技股份有限公司 | Chemical waste water treatment method |
| CN108840497A (en) * | 2018-06-04 | 2018-11-20 | 宿迁新亚科技有限公司 | A method of sewage middle and high concentration ammonia nitrogen is removed with large aperture synthetic resin |
| CN109534528B (en) * | 2018-11-20 | 2021-11-12 | 新昌县泰如科技有限公司 | Method for treating ciprofibrate process wastewater |
| CN111573943A (en) * | 2020-03-22 | 2020-08-25 | 萧县沃德化工科技有限公司 | Comprehensive treatment technology for 2-naphthol production wastewater |
| CN114212934A (en) * | 2021-11-29 | 2022-03-22 | 张家界久瑞生物科技有限公司 | Treatment process for methyl 3,4, 5-trimethoxybenzoate wastewater with high salinity and high COD (chemical oxygen demand) |
| CN114573188A (en) * | 2022-03-15 | 2022-06-03 | 宿迁思睿屹新材料有限公司 | P hydroxybenzoic acid waste water processing system |
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| WO2007133299A3 (en) * | 2006-01-11 | 2008-07-17 | Archer Daniels Midland Co | Simultaneous synthesis and purification of a fatty acid monoester biodiesel fuel |
| CN101798101A (en) * | 2009-02-10 | 2010-08-11 | 项文远 | Process for preparing potassium sulfate crystal by utilizing industrial wastewater from 26 acid production |
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Patent Citations (4)
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| CN1265376A (en) * | 2000-03-13 | 2000-09-06 | 南京大学 | Treatment of 2,3-acid producing waste water and resource recovering and utilizing method |
| WO2007133299A3 (en) * | 2006-01-11 | 2008-07-17 | Archer Daniels Midland Co | Simultaneous synthesis and purification of a fatty acid monoester biodiesel fuel |
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| CN101798101A (en) * | 2009-02-10 | 2010-08-11 | 项文远 | Process for preparing potassium sulfate crystal by utilizing industrial wastewater from 26 acid production |
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| 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 | ||
| C56 | Change in the name or address of the patentee |
Owner name: SUZHOU 3E NEW MATERIAL CORPORATION Free format text: FORMER NAME: SUZHOU LINTONG NEW MATERIAL TECHNOLOGY CO., LTD. |
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| CP01 | Change in the name or title of a patent holder |
Address after: Suzhou Wuzhong District City, Jiangsu province 215124 Yin Bridge Patentee after: SUZHOU 3E NEW MATERIAL Corp. Address before: Suzhou Wuzhong District City, Jiangsu province 215124 Yin Bridge Patentee before: SUZHOU LINTONG NEW MATERIAL TECHNOLOGY Co.,Ltd. |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20221024 Address after: 223800 No.36 Yangzi Road, eco Chemical Technology Industrial Park, Suqian City, Jiangsu Province Patentee after: SUQIAN SIRUI YIXIN MATERIAL CO.,LTD. Address before: 215124 Yinshan Bridge, Wuzhong District, Suzhou City, Jiangsu Province Patentee before: SUZHOU 3E NEW MATERIAL Corp. |
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| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 223800 No.36 Yangzi Road, eco Chemical Technology Industrial Park, Suqian City, Jiangsu Province Patentee after: Suqian Siruiyi New Materials Co.,Ltd. Address before: 223800 No.36 Yangzi Road, eco Chemical Technology Industrial Park, Suqian City, Jiangsu Province Patentee before: SUQIAN SIRUI YIXIN MATERIAL CO.,LTD. |