CN104193037A - Tar wastewater purification device capable of producing asphalt - Google Patents
Tar wastewater purification device capable of producing asphalt Download PDFInfo
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- CN104193037A CN104193037A CN201410470143.9A CN201410470143A CN104193037A CN 104193037 A CN104193037 A CN 104193037A CN 201410470143 A CN201410470143 A CN 201410470143A CN 104193037 A CN104193037 A CN 104193037A
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- reaction kettle
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- 239000002351 wastewater Substances 0.000 title claims abstract description 37
- 238000000746 purification Methods 0.000 title abstract description 6
- 239000010426 asphalt Substances 0.000 title abstract 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000003756 stirring Methods 0.000 claims abstract description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 11
- 239000003054 catalyst Substances 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 238000002156 mixing Methods 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 230000008676 import Effects 0.000 claims description 27
- 238000001179 sorption measurement Methods 0.000 claims description 24
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 claims description 21
- 229920002545 silicone oil Polymers 0.000 claims description 21
- 230000007062 hydrolysis Effects 0.000 claims description 18
- 238000006460 hydrolysis reaction Methods 0.000 claims description 18
- 239000000463 material Substances 0.000 claims description 18
- 230000020477 pH reduction Effects 0.000 claims description 17
- 238000001556 precipitation Methods 0.000 claims description 17
- 239000003921 oil Substances 0.000 claims description 16
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 14
- 239000000839 emulsion Substances 0.000 claims description 12
- 238000005188 flotation Methods 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 238000009875 water degumming Methods 0.000 claims description 7
- JZZIHCLFHIXETF-UHFFFAOYSA-N dimethylsilicon Chemical compound C[Si]C JZZIHCLFHIXETF-UHFFFAOYSA-N 0.000 claims description 6
- FAQYAMRNWDIXMY-UHFFFAOYSA-N trichloroborane Chemical compound ClB(Cl)Cl FAQYAMRNWDIXMY-UHFFFAOYSA-N 0.000 claims description 5
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 239000006229 carbon black Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 238000000151 deposition Methods 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 abstract description 8
- 238000000034 method Methods 0.000 abstract description 7
- 239000011269 tar Substances 0.000 description 36
- 239000011280 coal tar Substances 0.000 description 7
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 6
- GLDOVTGHNKAZLK-UHFFFAOYSA-N octadecan-1-ol Chemical compound CCCCCCCCCCCCCCCCCCO GLDOVTGHNKAZLK-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- GOQYKNQRPGWPLP-UHFFFAOYSA-N n-heptadecyl alcohol Natural products CCCCCCCCCCCCCCCCCO GOQYKNQRPGWPLP-UHFFFAOYSA-N 0.000 description 3
- 238000006068 polycondensation reaction Methods 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 229920002503 polyoxyethylene-polyoxypropylene Polymers 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 150000001299 aldehydes Chemical class 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
Landscapes
- Water Treatment By Sorption (AREA)
Abstract
The invention discloses a tar wastewater purification device capable of producing asphalt. The tar wastewater purification device comprises a raw water pond, a settling pond and a mixing-liquid separation tank which are connected in sequence, wherein the mixing-liquid separation tank is connected with a dimethylsilicone oil tank; a stirring paddle is arranged in the mixing-liquid separation tank; the stirring paddle is started for mixing dimethylsilicone oil with water in the tank, and after the stirring paddle is stopped and the standing process is finished, a dimethylsilicone oil region at the upper part and a water region at the lower part are formed in the tank; an outlet in the bottom of the mixing-liquid separation tank is connected with the inlet of a water storage pond and the inlet of a catalytic reaction kettle with the heating temperature of 180-300 DEG C; a nitrogen inlet and a catalyst inlet are formed in the catalytic reaction kettle; a catalyst tank is arranged at the catalyst inlet; the inlet of a cooler is connected with the outlet of the catalytic reaction kettle; the inlet of a filter is connected with the outlet of the cooler. The tar wastewater purification device is suitable for treating tar wastewater to greatly reduce the content of tar in a water body.
Description
Technical field
The present invention relates to tar and waste water purification techniques field, be specifically related to a kind of tar and waste water refining plant of producing pitch.
Background technology
The process of manufacture of the mineral substance such as oil, coal often relates to washing to be processed, and easily produces a large amount of tar and waste waters in water washing process.As its name suggests, the objectionable constituent in tar and waste water are mainly tar, and tar is a kind of complex compound that contains 100 Multiple components, comprises the organism such as alkane, aromatic hydrocarbon and colloid.When washing is processed, part tar material enters in water body, forms tar and waste water.Outside tar removing, in tar and waste water, also contain aldehydes matter, ammonia nitrogen substances, prussiate and solid particulate matter.
The purification of tar and waste water mainly for be to remove tar material, conventional tar material removal device comprises gravity separation equipment, an adsorption device etc. at present, but the tar clearance of these devices is only 20-30% (weight percent), in water body, still there is a large amount of tar material.The waste water that these are contained to tar is directly introduced subsequent handling, tar material can affect microbial growth in follow-up biochemical treatment system, make follow-up Biochemical Treatment not good, ammonia nitrogen substances in waste water, aldehydes matter are difficult to further removal, water body COD degraded not exclusively, cannot reach national water quality standard requirement.Therefore, to purify the particularly removal of the coal-tar middle oil material of waste water be all a difficult problem of water treatment field to tar and waste water all the time.
Summary of the invention
For this reason, a technical problem to be solved by this invention is that prior art is low to the tar clearance of tar and waste water, cause the water quality after processing cannot reach national water quality standard requirement, thereby propose the tar and waste water refining plant of the pitch produced that a kind of tar clearance is high.
For solving the problems of the technologies described above, the present invention proposes a kind of tar and waste water refining plant of producing pitch, comprise, and former pond and settling bowl, the outlet in described former pond is connected with the import of settling bowl; Dimethyl-silicon oil tank and mixing-minute flow container, the described mixing-fluid inlet of minute flow container is connected with the liquid outlet of settling bowl, and the oil-in of described mixing-minute flow container is connected with the outlet of dimethyl-silicon oil tank; In described mixing-minute flow container, be provided with able to turn on or off stirring rake, open stirring rake, described mixing-minute flow container is used for mixing dimethyl silicone oil and water, closes stirring rake, and described mixing-minute flow container is for the dimethyl silicone oil district on standing rear formation top and the pool of bottom; Tank, temperature of reaction are the catalytic reaction kettle of 180-300 ℃ and for depositing the catalyst tank of aluminum chloride or boron chloride, the outlet of described mixing-separatory pot bottom is connected with the import of tank and the import of catalytic reaction kettle successively, for first pool material being introduced to tank, Zai Jiang dimethyl silicone oil district material is introduced in catalytic reaction kettle, and described catalyst tank adds entrance with catalyzer in catalytic reaction kettle and is connected; In described catalytic reaction kettle, be provided with nitrogen inlet, for blast nitrogen in still; Water cooler and strainer, the import of described water cooler is connected with the outlet of catalytic reaction kettle, and the import of described strainer is connected with the outlet of water cooler.
Also comprise emulsion splitter tank, be connected with the emulsion splitter entrance of tank.
Also comprise air flotation pool, be connected with the outlet of tank.
Also comprise hydrolysis acidification pool, the import of described hydrolysis acidification pool is connected with the liquid outlet of air flotation pool.
Also comprise precipitation adsorption tank, the import of described precipitation adsorption tank is connected with the outlet of hydrolysis acidification pool.
Also comprise Aerobic Pond, be arranged between hydrolysis acidification pool and precipitation adsorption tank, the outlet of described hydrolysis acidification pool is connected with the import of Aerobic Pond, and the outlet of described Aerobic Pond is connected with the import of precipitation adsorption tank.
In described precipitation adsorption tank, be filled with adsorption particle, described adsorption particle is the graphitized carbon black of 50-100 μ m and the mixture of 100-250 μ m gac.
In described mixing-minute flow container, be provided with tank contents gauge, be used to indicate the position of water-oil interface.
The outside cover of described catalytic reaction kettle has Resistant heating chuck.
Technique scheme of the present invention has the following advantages compared to existing technology,
Former water is introduced in mixing-separating tank and is mixed with dimethyl silicone oil after settling bowl sedimentation, dimethyl silicone oil extracts most of tar ingredients in water, the coal-tar middle oil clearance of measuring water, up to more than 90% (weight percentage), is divided into top containing dimethyl silicone oil district and the pool, bottom of tar in standing rear mixing-separating tank.After separation, pool material enters in tank, and dimethyl silicone oil district material enters enclosed oxygen isolation catalyzed polymerization in catalytic reaction kettle, and the catalyzer using is aluminum chloride or boron chloride, and polymkeric substance enters water cooler and forms solid, obtains after filtering pitch.The present invention can be converted into the tar material in waste water the pitch of direct use by simple operation.
Wherein, nitrogen can avoid tar material oxidized in polycondensation process, can avoid dimethyl silicone oil deterioration by oxidation simultaneously, makes dimethyl silicone oil can continue to use.
Accompanying drawing explanation
For content of the present invention is more likely to be clearly understood, below according to a particular embodiment of the invention and by reference to the accompanying drawings, the present invention is further detailed explanation, wherein
Fig. 1 is the structural representation of tar and waste water refining plant of the present invention.
Embodiment
The tar and waste water refining plant of producing pitch of the present invention, comprises, former pond and settling bowl, and the outlet in described former pond is connected with the import of settling bowl; Dimethyl-silicon oil tank and mixing-minute flow container, the described mixing-fluid inlet of minute flow container is connected with the liquid outlet of settling bowl, and the oil-in of described mixing-minute flow container is connected with the outlet of dimethyl-silicon oil tank; In described mixing-minute flow container, be provided with able to turn on or off stirring rake, open stirring rake, described mixing-minute flow container is used for mixing dimethyl silicone oil and water, closes stirring rake, and described mixing-minute flow container is for the dimethyl silicone oil district on standing rear formation top and the pool of bottom; Tank, temperature of reaction are the catalytic reaction kettle of 180-300 ℃ and for depositing the catalyst tank of aluminum chloride or boron chloride, the outlet of described mixing-separatory pot bottom is connected with the import of tank and the import of catalytic reaction kettle successively, for first pool material being introduced to tank, Zai Jiang dimethyl silicone oil district material is introduced in catalytic reaction kettle, and described catalyst tank adds entrance with catalyzer in catalytic reaction kettle and is connected; In described catalytic reaction kettle, be provided with nitrogen inlet, for blast nitrogen in still; Water cooler and strainer, the import of described water cooler is connected with the outlet of catalytic reaction kettle, and the import of described strainer is connected with the outlet of water cooler.
Former water is introduced in mixing-separating tank and is mixed with dimethyl silicone oil after settling bowl sedimentation, dimethyl silicone oil extracts most of tar ingredients in water, the coal-tar middle oil clearance of measuring water, up to more than 90% (weight percentage), is divided into top containing dimethyl silicone oil district and the pool, bottom of tar in standing rear mixing-separating tank.After separation, pool material enters in tank, dimethyl silicone oil district material enters enclosed oxygen isolation catalyzed polymerization in catalytic reaction kettle, polymerization temperature is 180-300 ℃, the catalyzer using is aluminum chloride or boron chloride, polymkeric substance enters water cooler and forms solid, obtains after filtering the pitch that can directly use.
On this basis, in one embodiment of the present of invention, also comprise emulsion splitter tank, be connected with the emulsion splitter entrance of tank.Emulsion splitter is acted on to a small amount of emulsion in tank, make emulsion change water, oily two-phase into, contribute to the separation of two-phase, the emulsion splitter using is polyoxyethylene polyoxypropylene stearyl alcohol ether.
On the basis of the above, in one embodiment of the present of invention, also comprise air flotation pool, be connected with the outlet of tank.Air flotation pool utilizes micro-bubble oil phase thing and the granule foreign a small amount of in water for carrier sticks of high dispersing, makes its density reduce to float up to the water surface, is striking off, thereby realize the object of removing residual greasy dirt and granule foreign by Despumation device.
On above basis, in one embodiment of the present of invention, also comprise hydrolysis acidification pool, the import of described hydrolysis acidification pool is connected with the outlet of air flotation pool.The hydrolysis bacterium and the acid-producing bacteria that in hydrolysis acidification pool, contain mixing, the waste water after air supporting is processed in 30-35 ℃ of processing 7-9h, can be decomposed into small-molecule substance at hydrolysis acidification pool by the larger molecular organics in waste water, reduces the COD of water body.
In one embodiment of the present of invention, also comprise precipitation adsorption tank, the import of described precipitation adsorption tank is connected with the outlet of hydrolysis acidification pool.In precipitation adsorption tank, be filled with adsorption particle, described adsorption particle is the graphitized carbon black of 50-100 μ m and the mixture of 100-250 μ m gac.Adsorption particle can make the throw out adsorption and sedimentation that cannot precipitate in waste water.
In one embodiment of the present of invention, as shown in Figure 1, also comprise Aerobic Pond, be arranged between hydrolysis acidification pool and precipitation adsorption tank, the outlet of described hydrolysis acidification pool is connected with the import of Aerobic Pond, and the outlet of described Aerobic Pond is connected with the import of precipitation adsorption tank.Under aerobic condition, utilize the pollutent in the microbiological deterioration waste water in the aerobic sludge of cultivating, thereby further reduce the COD of waste water.In described mixing-minute flow container, be provided with tank contents gauge, for representing the position of water-oil interface.The outside cover of described catalytic reaction kettle has Resistant heating chuck.
Adopt the device shown in above-mentioned Fig. 1 to process 14L Coal Tar Wastewater, use 1L dimethyl silicone oil hybrid extraction, the tar clearance in Coal Tar Wastewater is up to 91.7%.Isolated oil phase, in catalytic reaction kettle, adds aluminum chloride catalyst 1g, is heated to 180-200 ℃ of polycondensation 7-8h, and nitrogen flow is 30mL/min, is cooled to normal temperature filtration and obtains pitch I.In isolated water, add polyoxyethylene polyoxypropylene stearyl alcohol ether emulsion splitter to mix, again after air supporting, acidication, aerobic treatment and precipitation absorption, after final processing, the indices of water body meets the requirement of GB8978-1996 < < integrated wastewater discharge standard > >, can qualified discharge.
Adopt the device shown in above-mentioned Fig. 1 to process 35L petroleum tar waste water, use 1L dimethyl silicone oil hybrid extraction, the tar clearance in Coal Tar Wastewater is up to 85.7%.The nitrogen protection in catalytic reaction kettle of isolated oil phase is airtight is heated to 270-300 ℃ of polycondensation 4-5h, the aluminum chloride that the catalyzer adding is 8.2g, and nitrogen flow is 100mL/min, is cooled to normal temperature and filters and obtain pitch II.In isolated water, add polyoxyethylene polyoxypropylene stearyl alcohol ether emulsion splitter to mix, again after air supporting, acidication, aerobic treatment and precipitation absorption, after final processing, the indices of water body meets the requirement of GB8978-1996 < < integrated wastewater discharge standard > >, can qualified discharge.
The character of the Coal Tar Wastewater relating in above-described embodiment and petroleum tar waste water is as follows:
As follows according to penetration degree, ductility and the softening temperature of the method detection pitch I-II of GB/T 4509, GB/T 4508, GB/T 4507 respectively:
| ? | Pitch I | Pitch II |
| Penetration degree (25 ℃, 100g, 5s), 1/10mm | 90-100 | 80-90 |
| Ductility (15 ℃), cm is not less than | 99 | 85 |
| Softening temperature, ℃ | 40-45 | 38-44 |
Obviously, above-described embodiment is only for example is clearly described, and the not restriction to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without also giving all embodiments.And the apparent variation of being extended out thus or change are still among the protection domain in the invention.
Claims (9)
1. the tar and waste water refining plant that can produce pitch, is characterized in that, comprises,
Former pond and settling bowl, the outlet in described former pond is connected with the import of settling bowl;
Dimethyl-silicon oil tank and mixing-minute flow container, the described mixing-fluid inlet of minute flow container is connected with the liquid outlet of settling bowl, and the oil-in of described mixing-minute flow container is connected with the outlet of dimethyl-silicon oil tank;
In described mixing-minute flow container, be provided with able to turn on or off stirring rake, open stirring rake, described mixing-minute flow container is used for mixing dimethyl silicone oil and water, closes stirring rake, and described mixing-minute flow container is for the dimethyl silicone oil district on standing rear formation top and the pool of bottom;
Tank, temperature of reaction are the catalytic reaction kettle of 180-300 ℃ and for depositing the catalyst tank of aluminum chloride or boron chloride, the outlet of described mixing-separatory pot bottom is connected with the import of tank and the import of catalytic reaction kettle successively, for first pool material being introduced to tank, Zai Jiang dimethyl silicone oil district material is introduced in catalytic reaction kettle, and described catalyst tank adds entrance with catalyzer in catalytic reaction kettle and is connected;
In described catalytic reaction kettle, be provided with nitrogen inlet, for blast nitrogen in still;
Water cooler and strainer, the import of described water cooler is connected with the outlet of catalytic reaction kettle, and the import of described strainer is connected with the outlet of water cooler.
2. device according to claim 1, is characterized in that, also comprises emulsion splitter tank, is connected with the emulsion splitter entrance of tank.
3. device according to claim 1 and 2, is characterized in that, also comprises air flotation pool, is connected with the outlet of tank.
4. device according to claim 3, is characterized in that, also comprises hydrolysis acidification pool, and the import of described hydrolysis acidification pool is connected with the liquid outlet of air flotation pool.
5. device according to claim 4, is characterized in that, also comprises precipitation adsorption tank, and the import of described precipitation adsorption tank is connected with the outlet of hydrolysis acidification pool.
6. device according to claim 5, it is characterized in that, also comprise Aerobic Pond, be arranged between hydrolysis acidification pool and precipitation adsorption tank, the outlet of described hydrolysis acidification pool is connected with the import of Aerobic Pond, and the outlet of described Aerobic Pond is connected with the import of precipitation adsorption tank.
7. device according to claim 5, is characterized in that, in described precipitation adsorption tank, is filled with adsorption particle, and described adsorption particle is the graphitized carbon black of 50-100 μ m and the mixture of 100-250 μ m gac.
8. device according to claim 1 and 2, is characterized in that, in described mixing-minute flow container, is provided with tank contents gauge, is used to indicate the position of water-oil interface.
9. device according to claim 1 and 2, is characterized in that, the outside cover of described catalytic reaction kettle has Resistant heating chuck.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410470143.9A CN104193037B (en) | 2014-09-16 | 2014-09-16 | A kind of tar and waste water refining plant producing pitch |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410470143.9A CN104193037B (en) | 2014-09-16 | 2014-09-16 | A kind of tar and waste water refining plant producing pitch |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104193037A true CN104193037A (en) | 2014-12-10 |
| CN104193037B CN104193037B (en) | 2016-01-27 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201410470143.9A Expired - Fee Related CN104193037B (en) | 2014-09-16 | 2014-09-16 | A kind of tar and waste water refining plant producing pitch |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5346152A (en) * | 1976-10-08 | 1978-04-25 | Showa Denko Kk | Process for treating waste water |
| US4241227A (en) * | 1976-05-05 | 1980-12-23 | Metallgesellschaft Aktiengesellschaft | Process for reducing biological oxygen demand of gas condensate |
| CN101607780A (en) * | 2009-07-22 | 2009-12-23 | 顾利平 | A kind of technology of handling tar product wastewater |
| CN102585871A (en) * | 2012-01-09 | 2012-07-18 | 常州黑玛新型碳材料工程技术研究中心有限公司 | Mesophase pitch and preparation method thereof |
| CN102690672A (en) * | 2012-06-18 | 2012-09-26 | 辽宁科技大学 | Preparing method for coal tar refined pitch |
| CN202785898U (en) * | 2012-05-02 | 2013-03-13 | 中环辽宁工程技术股份有限公司 | Device for treating and recycling wastewater from processing of coal tar |
| CN204198511U (en) * | 2014-09-16 | 2015-03-11 | 王茜茜 | The tar and waste water refining plant of pitch can be produced |
-
2014
- 2014-09-16 CN CN201410470143.9A patent/CN104193037B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4241227A (en) * | 1976-05-05 | 1980-12-23 | Metallgesellschaft Aktiengesellschaft | Process for reducing biological oxygen demand of gas condensate |
| JPS5346152A (en) * | 1976-10-08 | 1978-04-25 | Showa Denko Kk | Process for treating waste water |
| CN101607780A (en) * | 2009-07-22 | 2009-12-23 | 顾利平 | A kind of technology of handling tar product wastewater |
| CN102585871A (en) * | 2012-01-09 | 2012-07-18 | 常州黑玛新型碳材料工程技术研究中心有限公司 | Mesophase pitch and preparation method thereof |
| CN202785898U (en) * | 2012-05-02 | 2013-03-13 | 中环辽宁工程技术股份有限公司 | Device for treating and recycling wastewater from processing of coal tar |
| CN102690672A (en) * | 2012-06-18 | 2012-09-26 | 辽宁科技大学 | Preparing method for coal tar refined pitch |
| CN204198511U (en) * | 2014-09-16 | 2015-03-11 | 王茜茜 | The tar and waste water refining plant of pitch can be produced |
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| CN104193037B (en) | 2016-01-27 |
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Effective date of registration: 20170609 Address after: 510623, 601-CB02, room 30, Zhujiang East Road, Guangzhou, Tianhe District, Guangdong Patentee after: Guangzhou Environmental Protection Technology Co., Ltd. michiyasu Address before: 325025 Zhejiang City, Wenzhou Province Economic and Technological Development Zone, Binhai Road, Binhai District, No. 15, No. 2, No. 529 Patentee before: Wang Qianqian |
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