CN110117137B - Method and system for treating sinomenine hydrochloride production sewage - Google Patents
Method and system for treating sinomenine hydrochloride production sewage Download PDFInfo
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- CN110117137B CN110117137B CN201910490215.9A CN201910490215A CN110117137B CN 110117137 B CN110117137 B CN 110117137B CN 201910490215 A CN201910490215 A CN 201910490215A CN 110117137 B CN110117137 B CN 110117137B
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- 239000010865 sewage Substances 0.000 title claims abstract description 204
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 73
- 238000000034 method Methods 0.000 title claims abstract description 49
- INYYVPJSBIVGPH-UHFFFAOYSA-N 14-episinomenine Natural products C1CN(C)C2CC3=CC=C(OC)C(O)=C3C31C2C=C(OC)C(=O)C3 INYYVPJSBIVGPH-UHFFFAOYSA-N 0.000 title claims abstract description 39
- REKJPVUFKQYMHW-UHFFFAOYSA-N 2-methyl-4-(trifluoromethyl)-1,3-thiazole-5-carboxylic acid Chemical compound CC1=NC(C(F)(F)F)=C(C(O)=O)S1 REKJPVUFKQYMHW-UHFFFAOYSA-N 0.000 title claims abstract description 39
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 claims abstract description 164
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 95
- 238000004062 sedimentation Methods 0.000 claims abstract description 73
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 51
- 230000020477 pH reduction Effects 0.000 claims abstract description 41
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract description 40
- 230000001112 coagulating effect Effects 0.000 claims abstract description 40
- 230000003301 hydrolyzing effect Effects 0.000 claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 90
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 39
- 239000010802 sludge Substances 0.000 claims description 37
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 34
- 239000002245 particle Substances 0.000 claims description 32
- 238000006243 chemical reaction Methods 0.000 claims description 28
- 239000000945 filler Substances 0.000 claims description 26
- 230000001105 regulatory effect Effects 0.000 claims description 26
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 25
- 229910052742 iron Inorganic materials 0.000 claims description 18
- 230000007062 hydrolysis Effects 0.000 claims description 15
- 238000006460 hydrolysis reaction Methods 0.000 claims description 15
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims description 14
- 238000001556 precipitation Methods 0.000 claims description 12
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical group [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims description 10
- 239000000701 coagulant Substances 0.000 claims description 9
- 241000894006 Bacteria Species 0.000 claims description 8
- 238000005842 biochemical reaction Methods 0.000 claims description 8
- 239000003245 coal Substances 0.000 claims description 8
- 239000002023 wood Substances 0.000 claims description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 7
- 230000007935 neutral effect Effects 0.000 claims description 7
- 239000004952 Polyamide Substances 0.000 claims description 6
- 229920002647 polyamide Polymers 0.000 claims description 6
- 239000004743 Polypropylene Substances 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 5
- 230000001376 precipitating effect Effects 0.000 claims description 5
- 239000006228 supernatant Substances 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 4
- -1 polypropylene Polymers 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 13
- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 description 13
- 239000000126 substance Substances 0.000 description 13
- 230000018044 dehydration Effects 0.000 description 9
- 238000006297 dehydration reaction Methods 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 230000000694 effects Effects 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 238000005345 coagulation Methods 0.000 description 5
- 230000015271 coagulation Effects 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 208000034699 Vitreous floaters Diseases 0.000 description 4
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 4
- 230000001680 brushing effect Effects 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 239000011150 reinforced concrete Substances 0.000 description 4
- 239000002910 solid waste Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 229910001018 Cast iron Inorganic materials 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 229910000975 Carbon steel Inorganic materials 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000010962 carbon steel Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000005536 corrosion prevention Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000011152 fibreglass Substances 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 2
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229920002521 macromolecule Polymers 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 2
- 244000025254 Cannabis sativa Species 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000000202 analgesic effect Effects 0.000 description 1
- 230000003288 anthiarrhythmic effect Effects 0.000 description 1
- 230000003276 anti-hypertensive effect Effects 0.000 description 1
- 230000003110 anti-inflammatory effect Effects 0.000 description 1
- 239000003416 antiarrhythmic agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- OWAQXCQNWNJICI-UHFFFAOYSA-N benzene;chloroform Chemical compound ClC(Cl)Cl.C1=CC=CC=C1 OWAQXCQNWNJICI-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003574 free electron Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 238000005325 percolation Methods 0.000 description 1
- 230000000144 pharmacologic effect Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000036647 reaction Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 201000003068 rheumatic fever Diseases 0.000 description 1
- 206010039073 rheumatoid arthritis Diseases 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000003809 water extraction Methods 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46176—Galvanic cells
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/70—Treatment of water, waste water, or sewage by reduction
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/125—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using screw filters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/343—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the pharmaceutical industry, e.g. containing antibiotics
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/29—Chlorine compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention provides a method and a system for treating sinomenine hydrochloride production sewage, which are characterized in that sewage generated in each production stage of sinomenine hydrochloride is firstly divided into chloroform sewage, ethanol and other production sewage, the chloroform sewage is subjected to catalytic reduction special treatment to decompose high-content chloroform, and then the chloroform sewage, ethanol and other production sewage after catalytic reduction treatment are subjected to micro-electrolysis, pH callback, coagulating sedimentation, hydrolytic acidification and biochemical treatment, so that the sinomenine hydrochloride production sewage can reach the discharge standard only by once treatment, the daily treatment capacity can reach 150 tons, wherein the chloroform sewage is 75t/d, the ethanol and other production sewage are 75t/d, the sewage treatment efficiency is obviously improved, and the sinomenine hydrochloride production is facilitated.
Description
[ Field of technology ]
The invention belongs to the technical field of sewage treatment, and particularly relates to a method and a system for treating sinomenine hydrochloride production sewage.
[ Background Art ]
Sinomenine hydrochloride has the pharmacological actions of anti-inflammatory, analgesic, antihypertensive, antiarrhythmic and the like, and various preparations are applied to clinic at present and are used for treating rheumatic arthritis, rheumatoid arthritis and the like. The current sinomenine hydrochloride preparation method mainly comprises an alkalization water extraction method and a hydrochloric acid percolation and chloroform extraction method provided by a patent CN201110361882.0, and the specific preparation and production processes of the sinomenine hydrochloride provided by a patent CN201110361882.0 comprise the following steps: hydrochloric acid wetting, hydrochloric acid soaking, hydrochloric acid diacolation, alkalization, filtration, chloroform extraction, water washing, dehydration, concentration, crystallization, drying, decarbonization (reflux by ethanol), crystallization, centrifugation and drying, and a certain amount of sewage is generated in each stage of sinomenine hydrochloride production, especially diacolation, extraction stage and decarbonization stage. The requirements of the sewage discharge water quality are shown in the table 1 according to the specification of the three-level standard of the integrated sewage discharge standard GB 8978-1996:
TABLE 1 Water quality requirements for wastewater discharge (Unit: mg/L, pH excluded)
Project | pH | CODcr | BOD5 | SS | Ammonia nitrogen | Containing chloroform |
Standard limit value | 6-9 | ≤400 | ≤150 | ≤250 | ≤30 | ≤1.0 |
The pharmaceutical sewage treatment method in the prior art mainly comprises the following steps: firstly, removing large-particle suspended matters in sewage by adopting a grid well, then improving biodegradability by electrolysis, and then removing COD and BOD in the sewage by biochemical treatment so as to reach the emission standard; a Chinese medicine sewage treatment system and a method for treating Chinese medicine sewage as disclosed in patent CN201310474536.2, and a domestic sewage treatment device as disclosed in patent CN 201610611940.3; or a combined treatment method of chemical pharmaceutical sewage as disclosed in patent CN201110247905.5 is added with an ABR acidification tank to carry out hydrolytic acidification on indissolvable substances in the sewage, thereby improving the treatment efficiency. However, the prior art including the above patent cannot achieve good effect when applied to the sewage treatment process of sinomenine hydrochloride production, the sewage needs repeated treatment for many times, the treatment efficiency is low, and the daily throughput is about 30t.
[ Invention ]
The invention aims to provide a method and a system for treating sinomenine hydrochloride production sewage, which are used for solving the defects in the prior art, can treat 150 tons of sinomenine hydrochloride production sewage in a day, and remarkably improve the sewage treatment efficiency.
The invention aims at solving the problems through the following technical scheme:
A method for treating sinomenine hydrochloride production sewage comprises the following steps:
The method comprises the steps of (1) respectively removing large-particle suspended matters in chloroform sewage, ethanol and other production sewage generated in each stage of sinomenine hydrochloride production, then enabling the chloroform sewage, ethanol and other production sewage to enter a water quality and water quantity adjusting unit for water quality and water quantity adjustment, enabling the chloroform sewage to enter a catalytic reduction unit in the step (2), and enabling the ethanol and other production sewage to enter a micro-electrolysis reaction unit in the step (3);
(2) The chloroform sewage after water quality and water quantity adjustment enters the catalytic reduction unit, and is decomposed under the action of iron, carbon filler and hydrogen peroxide in the catalytic reduction unit, and then enters the micro-electrolysis reaction unit;
(3) In the micro-electrolysis reaction unit, carrying out micro-electrolysis on the ethanol and other production sewage subjected to water quality and water quality adjustment and the chloroform sewage subjected to catalytic reduction, and then entering a pH callback unit;
(4) The pH of the sewage in the pH callback unit is regulated by alkali, the pH is regulated to be neutral, and then the sewage enters a coagulating sedimentation unit;
(5) Adding a coagulant into the coagulating sedimentation unit for coagulating sedimentation, and then entering a hydrolysis acidification unit;
(6) The hydrolytic acidification unit adopts hydrolytic acidification bacteria to carry out hydrolytic acidification on the sewage after coagulating sedimentation, and then the sewage enters a biochemical treatment unit;
(7) And performing biochemical treatment in the biochemical treatment unit, and precipitating, wherein the clear water after precipitation reaches the discharge standard.
Preferably, the catalytic reduction unit in the step (2) is a catalytic reduction reactor, the filler of the catalytic reduction reactor is wood shaving iron and coal granular activated carbon, and the feeding amount of the hydrogen peroxide is 1.2-1.5L/m 3.
Preferably, the micro-electrolysis reaction unit in the step (3) is a micro-electrolysis reactor, the filler of the micro-electrolysis reactor is iron-carbon filler, and the micro-electrolysis reaction is performed at a pH of 2-5.
Preferably, the coagulant in the step (5) is polyaluminum chloride, polyferric sulfate or a mixture of the polyaluminum chloride and the polyferric sulfate.
Preferably, the hydrolytic acidification unit in the step (6) is a hydrolytic acidification tank, and the hydrolytic acidification tank adopts polypropylene or polyamide three-dimensional elastic filler.
Preferably, the specific steps of performing biochemical treatment in the step (7) are as follows: firstly, anaerobic biochemical reaction is carried out in a UASB reactor, and then two-stage A-O reaction is carried out.
Preferably, the precipitated sludge generated in the step (5) and/or the step (7) enters a sludge tank for further precipitation, the supernatant after precipitation flows back to the water quality and water quantity adjusting unit in the step (1), and the precipitated sludge is dehydrated by a spiral shell overlapping dehydrator.
The invention also provides a sinomenine hydrochloride production sewage treatment system, which comprises:
large particle suspended matter removal unit: for removing large particle suspended matters in chloroform sewage, ethanol and other production sewage;
Water quality and quantity adjusting unit: the method is used for adjusting the water quality and the water quantity of chloroform sewage, ethanol and other production sewage after removing large-particle suspended matters;
Catalytic reduction unit: the method is used for decomposing chloroform in chloroform sewage after water quality and water quantity are regulated;
Micro-electrolysis reaction unit: the method is used for carrying out micro-electrolysis on the chloroform sewage after catalytic reduction and the ethanol and other production sewage after water quality and water quantity adjustment so as to improve the biodegradability;
a pH callback unit: the method is used for carrying out pH callback on the sewage after the micro-electrolysis reaction;
and (3) a coagulating sedimentation unit: the method is used for coagulating sedimentation of the sewage after the pH is adjusted back;
hydrolysis acidification unit: the method is used for hydrolyzing and acidifying substances which are difficult to biodegrade in the sewage after coagulating sedimentation;
biochemical treatment unit: the method is used for carrying out biochemical reaction treatment on the hydrolyzed and acidified sewage to remove COD and BOD, so that the water quality reaches the emission standard;
A sewage conveying unit: is connected with the units and is used for conveying sewage to circulate among the units.
Preferably, the large-particle suspended matter removing unit is a grid well with a rotating brush grid; the water quality and quantity adjusting unit is an adjusting tank; the catalytic reduction unit is a catalytic reduction reactor with filling materials of wood shavings iron and coal particles of activated carbon and a dosing device for adding hydrogen peroxide; the micro-electrolysis reaction unit is a micro-electrolysis reactor adopting iron-carbon filler; the pH callback unit is a pH callback tank, the coagulating sedimentation unit is a coagulating sedimentation tank, the hydrolysis acidification unit is a hydrolysis acidification tank with PP or polyamide three-dimensional elastic filler, and the biochemical treatment unit comprises a UASB reactor and a two-stage A-O reactor.
Preferably, the system further comprises a sludge precipitation unit and a dehydration unit, wherein the sludge precipitation unit is used for precipitating sludge generated by the coagulating sedimentation unit and/or the biochemical treatment unit, the dehydration unit is used for dehydrating the sludge precipitated by the sludge precipitation unit, and the dehydration unit is a spiral shell stacking dehydrator.
The invention divides sewage generated in each production stage of sinomenine hydrochloride into chloroform sewage, ethanol and other production sewage, carries out catalytic reduction special treatment on the chloroform sewage to decompose high-content chloroform, and then carries out micro-electrolysis, pH callback, coagulating sedimentation, hydrolytic acidification and biochemical treatment on the chloroform sewage, ethanol and other production sewage after catalytic reduction treatment to ensure that the sinomenine hydrochloride production sewage can reach the emission standard only by once treatment, the daily treatment capacity can reach 150 tons, wherein the chloroform sewage is 75t/d, the ethanol and other production sewage are 75t/d, and the sewage treatment efficiency is obviously improved, thereby being beneficial to sinomenine hydrochloride production.
[ Description of the drawings ]
FIG. 1 is a schematic diagram of a sinomenine hydrochloride production sewage treatment system.
[ Detailed description ] of the invention
The invention will be further described with reference to the drawings and embodiments.
The chloroform content of the sewage generated in the extraction stage in the sinomenine hydrochloride production process is very high and can reach 1000mg/L, the COD and BOD content is also several times that of the sewage generated in other stages, and if the sewage is treated together with other production sewage, the chloroform cannot be completely decomposed, so that the sewage treatment needs to be repeated for many times. The water quality of chloroform sewage, ethanol and other production sewage generated in the sinomenine hydrochloride production process is shown in table 2:
TABLE 2 quality of sinomenine hydrochloride production wastewater (Unit: mg/L, pH excluded)
Therefore, the invention divides the sewage generated in each stage of sinomenine hydrochloride production into chloroform sewage, ethanol and other production sewage, and carries out separate treatment in the early stage so as to improve the sewage treatment efficiency, and the method for treating the sinomenine hydrochloride production sewage comprises the following steps:
The method comprises the steps of (1) respectively removing large-particle suspended matters in chloroform sewage, ethanol and other production sewage generated in each stage of sinomenine hydrochloride production, then enabling the chloroform sewage, ethanol and other production sewage to enter a water quality and water quantity adjusting unit for water quality and water quantity adjustment, enabling the chloroform sewage to enter a catalytic reduction unit in the step (2), and enabling the ethanol and other production sewage to enter a micro-electrolysis reaction unit in the step (3); the step of removing the large-particle suspended matters can adopt a grid well, and the grid well can be provided with a rotating brush grid, so that the large-particle solid suspended matters can be removed more conveniently; the water quality and water quantity adjusting unit can adopt an adjusting tank, and can ensure continuous and uniform operation of the subsequent treatment process by adjusting the water quality and water quantity; the two grille wells and the two regulating tanks can be respectively used for treating chloroform sewage, ethanol and other production sewage;
(2) In the step, the chloroform sewage is subjected to strong oxidation reduction under the catalysis of iron and carbon in a catalytic reduction unit and the catalysis of hydrogen peroxide, so that chloroform is decomposed, chloroform in the sewage is effectively reduced, the pH value is slightly reduced, the biodegradability of the sewage is greatly improved, the aim of reducing COD C r is fulfilled, and then the step (3) is carried out; the principle of reducing chloroform in sewage is as follows:
chloroform is insoluble in water and soluble in alcohol, ether and benzene; chloroform can be oxidized into hydrogen chloride and phosgene by oxygen in the air, hydrogen peroxide is utilized to accelerate the reaction in an iron-carbon catalyst, and the chloroform and the hydrogen peroxide directly react to generate phosgene, wherein the reaction formula is shown as follows;
CHCl 3+H2O2=HCl+H2O+COCl2 (iron carbon catalyst)
Phosgene, also called phosgene, has high chemical reactivity and strong corrosiveness after meeting water. Phosgene is colorless gas at normal temperature, has the taste of humic grass, is yellow green liquid at low temperature, has unstable chemical property, and is rapidly hydrolyzed when meeting water to generate hydrogen chloride; after the phosgene leaks, the phosgene is absorbed by water mist, the phosgene is easy to hydrolyze, and the reaction formula of the phosgene and water is as follows:
COCl2+H2O=2HCl+CO2
Therefore, the chloroform firstly generates phosgene with higher reaction activity with hydrogen peroxide under the catalysis of the iron carbon, and then the phosgene and water can be rapidly decomposed into hydrochloric acid and carbon dioxide, so that the chloroform is successfully decomposed; the catalytic reduction unit can adopt a catalytic reduction reactor, the filler of the catalytic reduction reactor is preferably wood shavings iron and coal particles activated carbon, and the catalytic reduction unit is provided with a dosing device for dosing hydrogen peroxide, wherein the dosing amount of the hydrogen peroxide is determined according to the chloroform content in chloroform wastewater, and is generally 1.2-1.5L/m 3.
(3) In the micro-electrolysis reaction unit, carrying out micro-electrolysis on ethanol and other production sewage and chloroform sewage to improve the biodegradability of the sewage; then, a step (4) of a pH callback unit is carried out; in this step, for convenience of treatment, ethanol and other production wastewater may be first mixed with chloroform wastewater and then enter a micro-electrolysis reaction unit, or may not be separately treated; the step of sewage can generate an electrolytic reaction in a primary cell under an acidic environment through micro-electrolysis, free electrons in the primary cell reaction are utilized to break down hydroxyl in ethanol in the sewage, the residual hydrogen peroxide in the catalytic reduction reaction in the previous step is utilized to further completely degrade chloroform in the sewage while reducing the influence of the ethanol on subsequent microbial treatment, the salt content in sinomenine hydrochloride production sewage is higher, the biodegradability of the sewage under high salinity can be greatly improved through micro-electrolysis, and the decoloring and filtering effects can be realized; therefore, the aim of reducing COD Cr can be achieved through micro-electrolysis, simultaneously the biodegradability of the sewage is greatly improved, and the water quality is close to the neutrality from weak acidity; the micro-electrolysis reaction unit can adopt a micro-electrolysis reactor, the micro-electrolysis reactor filler is preferably an iron-carbon filler, the iron-carbon filler can adopt cast iron particle balls containing 75% of iron and 25% of carbon, and can also adopt scrap iron and activated carbon particles with the same proportion; the microelectrolysis is preferably carried out at a pH of 2 to 5;
(4) In the step of pH callback unit, alkali is used for adjusting the pH of the sewage to be neutral, specifically between 6.8 and 7.2, and then the sewage enters the step of coagulating sedimentation unit (5); the pH callback unit can adopt a pH callback pool; the sewage is regulated to be neutral, so that the subsequent coagulating sedimentation is facilitated, and the anaerobic bacteria growth and survival method is suitable for subsequent biochemical treatment;
(5) In the coagulating sedimentation unit, coagulant is added into sewage to carry out coagulation reaction; then entering a hydrolysis acidification unit in the step (6); the purpose of coagulating sedimentation is mainly to coagulate macromolecular organic matters through coagulating bridge, thereby forming large particles to be separated from water and reduce COD concentration; the coagulating sedimentation unit can adopt a coagulating sedimentation tank, the coagulant can be polyaluminium chloride (PAC), polymeric ferric sulfate or a mixture of the polyaluminium chloride and the polymeric ferric sulfate, and the coagulating agent is added until no sediment is generated; partial soluble iron ions are generated in the catalytic reduction reaction unit and the micro-electrolysis reaction unit, and after the pH is regulated by the pH callback unit, the partial soluble iron ions and PAC act together to play a good role in coagulation;
(6) In the hydrolysis acidification unit, hydrolysis acidification is carried out on substances which are difficult to biodegrade in sewage by adopting hydrolysis acidification bacteria, and then the substances enter the biochemical treatment unit in the step (7); the hydrolytic acidification bacteria is anaerobic bacteria, can generate extracellular enzyme to hydrolyze under the condition of low dissolved oxygen (0.1-0.5 mg/l), degrade polymer and cyclic macromolecular organic matters which are difficult to biodegrade into single molecules or even low molecular organic matters such as acetic acid, improve the biodegradability of sewage, remove the organic matters and ensure that the treatment effect of subsequent biochemical treatment is optimal; the hydrolytic acidification unit can adopt a hydrolytic acidification tank, the hydrolytic acidification tank filler can adopt a PP or polyamide three-dimensional elastic filler, hydrolytic acidification bacteria are easy to attach, and the bearing capacity is large;
(7) In the biochemical treatment unit, biochemical treatment is carried out on sewage to remove COD and BOD, then sedimentation is carried out, and the clear water after sedimentation can reach the discharge standard; after the treatment of the six steps, chloroform and other organic substances in the sewage are obviously decomposed, and the biodegradability is improved to the greatest extent. Therefore, through the biochemical treatment of the step, pollutants such as COD, BOD, ammonia nitrogen and the like in the sewage can be removed, so that the water quality reaches the standard; after the treatment, the chloroform content can be reduced to 0.4-0.49mg/L.
The biochemical treatment can be carried out by adopting a sewage biochemical treatment method in the prior art, the anaerobic biochemical reaction is preferably carried out in a UASB reactor, then two-stage A-O reaction is carried out, the anaerobic biochemical reaction is carried out in the UASB reactor, COD can be greatly reduced, and because the anaerobic reaction does not need power such as air blast, the high-efficiency anaerobic reaction can save a large amount of energy consumption, the anaerobic reaction is carried out by two-stage AO reaction, A/O (anoxic/aerobic) is a continuous water inlet and outlet process, the A pool and the O pool are connected in series, and meanwhile, a sedimentation tank is arranged, specifically, an intermediate sedimentation tank is arranged behind the A1 pool and the O1 pool, a secondary sedimentation tank is arranged behind the A2 pool, nitrifying liquid and sludge reflux are needed when nitrogen removal is carried out, and the reflux ratio can be determined according to the concentration of ammonia nitrogen and the total nitrogen removal requirement of inflowing water; the anoxic and aerobic states of the sewage in the reaction system are partitioned by space, the content of the dissolved oxygen in the sewage can more easily reach the method requirement, the method control is facilitated, and the treatment efficiency is higher.
The sewage can be circulated in the steps through the water pump; and the power is transmitted by using a blower in the micro-electrolysis reactor, the coagulating sedimentation tank, the O1 tank, the O2 tank and the secondary sedimentation tank.
And (3) performing coagulating sedimentation in the step (5) and performing UASB reaction and A-O reaction in the biochemical treatment in the step (7) to generate precipitated sludge, enabling the generated precipitated sludge to enter a sludge tank for further sedimentation, enabling supernatant after sedimentation to flow back to a water quality and water quantity regulating unit in the step (1), repeatedly performing treatment, dehydrating the precipitated sludge by a spiral shell stacking dehydrator, and collecting and externally transporting the sludge for landfill.
Therefore, the method for treating sinomenine hydrochloride production sewage firstly divides sewage into chloroform sewage, ethanol and other production sewage, the chloroform sewage firstly enters a grid well, large-particle solid waste and floaters are removed by rotating and brushing the grid, and then enters a chloroform regulating tank, the water quality and the water quantity are regulated, and the continuous and uniform operation of the subsequent treatment process is ensured. The chloroform sewage is evenly lifted by a water pump to enter a catalytic reduction reactor, and under the action of wood shaving iron, coal particle activated carbon filler and hydrogen peroxide, the strong oxidation-reduction reaction and chloroform decomposition occur, the pH value is slightly reduced, the biodegradability of the sewage is greatly improved, and the aim of reducing COD Cr is fulfilled.
Ethanol and other production sewage enter a grid well together, large-particle solid waste and floaters are removed by rotating and brushing the grid, and then the ethanol enters an ethanol adjusting tank, so that the water quality and the water quantity are adjusted, and the continuous and uniform operation of the subsequent treatment process is ensured. And then the sewage pump uniformly lifts the ethanol, other production sewage and the chloroform sewage after catalytic reduction into a micro-electrolysis reactor for micro-electrolysis, the biodegradability of the sewage can be greatly improved through micro-electrolysis, the aim of reducing COD Cr is fulfilled, and the water quality is close to neutral from weak acidity. And the residual hydrogen peroxide in the catalytic reduction reaction in the last step can be utilized to further completely degrade chloroform in the sewage.
The chloroform sewage, ethanol and other production sewage after micro-electrolysis treatment enter a pH callback tank, the sewage is regulated to be neutral, then a coagulant is added into a coagulating sedimentation tank for further coagulation reaction, and macromolecular organic matters are coagulated through coagulation bridge, so that large particles are formed and separated from water, and the COD concentration is further reduced.
And (5) enabling the effluent of the coagulating sedimentation tank to enter a hydrolysis acidification tank. The hydrolytic acidification bacteria break the organic macromolecular substances which are difficult to be biologically degraded into organic micromolecular organic substances, further improve the biodegradability of sewage, remove the organic substances and optimize the subsequent biochemical treatment effect.
The sewage is lifted to a UASB pool for anaerobic biochemical reaction by a water pump after being treated by a hydrolytic acidification pool, and COD is greatly reduced; because the anaerobic reaction does not need power such as blast air, the efficient anaerobic reaction can save a great deal of energy consumption.
The effluent from the anaerobic reaction flows into an A1 pool, is subjected to two-stage AO reaction, enters a secondary sedimentation tank for sedimentation, and then enters a clean water pool for standard discharge.
In the sewage treatment process, sludge generated by the UASB reactor, the middle sedimentation tank, the secondary sedimentation tank and the coagulating sedimentation tank enters a sludge tank for sedimentation, supernatant after sedimentation flows back to an ethanol regulating tank for repeated treatment, the precipitated sludge can be sent into a spiral shell stacking dehydrator for dehydration through a sludge pump, and mud cakes can be collected for external transportation and landfill.
Based on the method, the invention also provides a sinomenine hydrochloride production sewage treatment system, which is shown in figure 1 and comprises the following steps:
large particle suspended matter removal unit: for removing large particle suspended matters in chloroform sewage, ethanol and other production sewage; the unit can adopt two grid wells which are preferably used for treating chloroform sewage, ethanol and other production sewage respectively; the grid well can be provided with a rotating brush grid, so that the removal of large-particle solid suspended matters is facilitated;
water quality and quantity adjusting unit: the method is used for adjusting the water quality and the water quantity of chloroform sewage, ethanol and other production sewage after removing large-particle suspended matters; the unit can adopt regulating tanks and can be provided with two groups of regulating tanks for respectively treating chloroform sewage, ethanol and other production sewage;
Catalytic reduction unit: the method is used for decomposing chloroform in chloroform sewage after water quality and water quantity are regulated; the unit can adopt a catalytic reduction reactor with filling materials of wood shavings iron and coal particles of active carbon and a dosing device for adding hydrogen peroxide;
Micro-electrolysis reaction unit: the method is used for carrying out micro-electrolysis on the chloroform sewage after catalytic reduction and the ethanol and other production sewage after water quality and water quantity adjustment so as to improve the biodegradability; the unit can adopt a micro-electrolysis reactor with iron-carbon filler, wherein the iron-carbon filler can adopt cast iron particle balls containing 75% of iron and 25% of carbon, or iron filings and activated carbon particles with the same proportion, and the micro-electrolysis is preferably carried out under the condition of pH value of 2-5;
a pH callback unit: the method is used for carrying out pH callback on the sewage after the micro-electrolysis reaction; the unit can adopt a pH callback pool;
And (3) a coagulating sedimentation unit: the method is used for coagulating sedimentation of the sewage after the pH is adjusted back; the unit can adopt a coagulating sedimentation tank;
hydrolysis acidification unit: the method is used for hydrolyzing and acidifying substances which are difficult to biodegrade in the sewage after coagulating sedimentation; the unit can adopt a hydrolytic acidification tank with PP or polyamide stereo elastic biological filler; the filler is easy to attach hydrolytic acidification bacteria and has large bearing capacity;
Biochemical treatment unit: the method is used for carrying out biochemical reaction treatment on the hydrolyzed and acidified sewage to remove COD and BOD, so that the water quality reaches the emission standard; this unit may include a UASB reactor and a two-stage A-O reactor; the A-O reactor comprises A, O tanks which are connected in series, a sedimentation tank is arranged behind the A, O tanks, a middle sedimentation tank is arranged behind the specific A1 tank and the specific O1 tank, and a secondary sedimentation tank is arranged behind the A2 tank and the specific O2 tank; and the clear water after the secondary sedimentation tank enters a clear water tank for discharging.
A sewage conveying unit: the sewage treatment device is connected with the units and used for conveying sewage to circulate among the units, and the units can adopt a water pump to convey sewage.
The sewage treatment system can further comprise a power transmission unit, wherein the power transmission unit is preferably a blower and is used for carrying out power transmission on the micro-electrolysis reactor, the coagulating sedimentation tank, the O1 tank, the O2 tank and the secondary sedimentation tank.
The sewage treatment system can further comprise a sludge precipitation unit and a dehydration unit, wherein the sludge precipitation unit is used for precipitating sludge generated by the coagulating sedimentation unit and/or the biochemical treatment unit, the dehydration unit is used for dehydrating the sludge precipitated by the sludge precipitation unit, and the dehydration unit is preferably a spiral shell overlapping dehydrator.
The embodiment of the invention provides a sinomenine hydrochloride production sewage treatment system, wherein a preferable embodiment is shown in a figure 1, and the system specifically comprises:
2 grid wells; one for treating chloroform sewage and the other for treating ethanol and other production sewage, each designed flow q=75m 3/d, hydraulic retention time hrt=29 h; size: 7.24X15.0X15.0m adopts underground reinforced concrete structure, and is lined with glass fiber reinforced plastic for corrosion protection, firstly, 1 rotating brush grille is configured, the grille clearance is 0.8mm, the grille length is 1500mm, and the power is 0.75kw;
A chloroform regulating tank and an ethanol regulating tank;
a catalytic reduction reactor; external dimensions: The method is characterized in that wood shaving iron and coal particle activated carbon filler are arranged in the carbon steel to prevent corrosion, and a dosing device is arranged to dose hydrogen peroxide according to the chloroform content in chloroform wastewater, wherein the dosing amount is generally 1.2-1.5L/m 3;
A micro-electrolysis reactor; design flow q=150m 3/d, external dimensions: Cast iron particle ball filler with 75% of iron and 25% of carbon is arranged in the steel, and the carbon steel is corrosion-resistant;
A pH callback pool;
A coagulating sedimentation tank; design flow q=150 m 3/d; size: 4.0x2.5x5.0m, half overground reinforced concrete structure;
A hydrolytic acidification tank; design flow q=150 m 3/d, size: 5.0x4.0x5.0m, underground reinforced concrete structure; polyamide biofilm carrier attached with hydrolytic acidification 60m 3, phi 150mm, l=3m;
A UASB reactor; adopting a steel structure for corrosion prevention;
a1, a pool;
An O1 pool;
A medium sedimentation tank;
A pool A2;
an O2 pool;
A secondary sedimentation tank;
a clean water tank;
A sludge pool; is connected with a coagulating sedimentation tank, a UASB reactor, a middle sedimentation tank and a secondary sedimentation tank through a plurality of delivery pumps, for precipitating the sludge they produce;
a spiral shell stacking dehydrator; sludge treatment capacity is 50kg/h, and total power is 1.5kw;
The sewage or sludge is conveyed among the devices through a plurality of conveying water pumps (particularly comprising a chloroform sewage pump, a lifting pump and the like);
a blower; and the power is transmitted by connecting the transmission pipeline with the micro-electrolysis reactor, the coagulating sedimentation tank, the O1 tank and the O2 tank.
Any prior art product which can achieve the purpose of the invention can be adopted by the regulating tank, the pH callback tank, the UASB reactor, the A1 tank, the O1 tank, the middle sedimentation tank, the A2 tank, the O2 tank, the secondary sedimentation tank, the clean water tank, the sludge tank and the like. Wherein the pH callback tank, the A1 tank, the O1 tank, the middle sedimentation tank, the A2 tank, the O2 tank, the secondary sedimentation tank, the clean water tank and the sludge tank adopt reinforced concrete structure tanks, and the pH callback tank is additionally provided with glass fiber reinforced plastics for corrosion prevention.
The sewage treatment system of the embodiment comprises the following treatment methods:
The chloroform sewage generated by sinomenine hydrochloride firstly enters a grid well, large-particle solid waste and floaters are removed by rotating and brushing the grid, and then enters a chloroform regulating tank, so that the water quality and the water quantity are regulated, and the continuous and uniform operation of the subsequent treatment process is ensured. The chloroform sewage is evenly lifted by a chloroform sewage pump to enter a catalytic reduction reactor, under the action of wood shaving iron, coal particles, activated carbon filler and hydrogen peroxide (the feeding amount of the hydrogen peroxide is 1.4L/m 3), the strong oxidation-reduction reaction is carried out, the chloroform is decomposed, the pH value is slightly reduced, the biodegradability of the sewage is greatly improved, and the aim of reducing COD Cr is fulfilled.
Ethanol produced by sinomenine hydrochloride and other production sewage enter a grid well together, large-particle solid waste and floaters are removed by rotating and brushing the grid, and then enter an ethanol regulating tank, so that the water quality and the water quantity are regulated, and the continuous and uniform operation of the subsequent treatment process is ensured. And then the sewage pump uniformly lifts the ethanol, other production sewage and the chloroform sewage after catalytic reduction into a micro-electrolysis reactor for micro-electrolysis, so that the biodegradability of the sewage can be greatly improved, the aim of reducing COD Cr is fulfilled, and the water quality is close to neutrality from weak acidity. And the residual hydrogen peroxide in the catalytic reduction reaction in the last step can be utilized to further completely degrade chloroform in the sewage.
Mixing chloroform sewage, ethanol and other production sewage after micro-electrolysis treatment into mixed sewage, feeding the mixed sewage into a pH callback tank, regulating the sewage to be neutral, and then adding a coagulant (adopting polyaluminium chloride) into a coagulating sedimentation tank for further coagulation reaction.
And (5) water is discharged from the coagulating sedimentation tank and enters the hydrolysis acidification tank. The hydrolytic acidification bacteria break the organic macromolecular substances which are difficult to be biodegraded into organic micromolecular organic substances, so that the biodegradability of sewage is improved, the organic substances are removed, and the subsequent biochemical treatment effect is optimal.
The sewage is treated by the hydrolytic acidification tank and then is lifted to the UASB tank by the lifting pump to carry out anaerobic biochemical reaction, and the COD is greatly reduced; because the anaerobic reaction does not need power such as blast air, the high-efficiency anaerobic reaction can save a great deal of energy consumption for the system.
Anaerobic reaction effluent flows into an A1 pool, passes through two-stage AO reactions of A1, O1, a middle sedimentation pool, A2 and O2, enters a secondary sedimentation pool for sedimentation after the AO reactions, and then enters a clean water pool for standard discharge (the discharge outlet water detection results are shown in Table 3).
In the sewage treatment process, sludge generated by the UASB reactor, the middle sedimentation tank, the secondary sedimentation tank and the coagulating sedimentation tank enters a sludge tank for sedimentation, supernatant fluid after sedimentation flows back to an ethanol regulating tank for repeated treatment, the precipitated sludge is sent into a spiral shell stacking dehydrator for dehydration through a sludge pump, and sludge cakes can be collected for external transportation and landfill.
With the sewage treatment system provided by the embodiment, the sewage produced by sinomenine hydrochloride can reach the discharge standard after only one treatment, the daily treatment of the sewage can reach 150t,
TABLE 3 effluent pollutant content at the discharge ports
Pollutant name | pH | CODcr | BOD5 | SS | Ammonia nitrogen | Containing chloroform |
Content (mg/L) | 7.3-7.44 | 384 | 120 | 50 | 6.97 | 0.42 |
While the invention has been described with respect to the above embodiments, it should be noted that modifications can be made by those skilled in the art without departing from the inventive concept, and these are all within the scope of the invention.
Claims (4)
1. The method for treating the sinomenine hydrochloride production sewage is characterized by comprising the following steps of:
The method comprises the steps of (1) respectively removing large-particle suspended matters in chloroform sewage, ethanol and other production sewage generated in each stage of sinomenine hydrochloride production, then enabling the chloroform sewage, ethanol and other production sewage to enter a water quality and water quantity adjusting unit for water quality and water quantity adjustment, enabling the chloroform sewage to enter a catalytic reduction unit in the step (2), and enabling the ethanol and other production sewage to enter a micro-electrolysis reaction unit in the step (3); the pH of the chloroform sewage is 7.6; (2) The chloroform sewage after water quality and water quantity adjustment enters the catalytic reduction unit, and is decomposed under the action of iron, carbon filler and hydrogen peroxide in the catalytic reduction unit, so that the chloroform in the sewage is effectively reduced, and the pH value of the sewage is slightly reduced; then entering the micro-electrolysis reaction unit; the catalytic reduction unit is a catalytic reduction reactor, the filler of the catalytic reduction reactor is wood shaving iron and coal particles activated carbon, and the feeding amount of the hydrogen peroxide is 1.2-1.5L/m 3; (3) In the micro-electrolysis reaction unit, carrying out micro-electrolysis on the ethanol and other production sewage subjected to water quality and water quality adjustment and the chloroform sewage subjected to catalytic reduction, and then entering a pH callback unit; the micro-electrolysis reaction unit is a micro-electrolysis reactor, the filler of the micro-electrolysis reactor is iron-carbon filler, and the micro-electrolysis reaction is carried out at pH 2-5;
(4) The pH of the sewage in the pH callback unit is regulated by alkali, the pH is regulated to be neutral, and then the sewage enters a coagulating sedimentation unit;
(5) Adding a coagulant into the coagulating sedimentation unit for coagulating sedimentation, and then entering a hydrolysis acidification unit;
(6) The hydrolytic acidification unit adopts hydrolytic acidification bacteria to carry out hydrolytic acidification on the sewage after coagulating sedimentation, and then the sewage enters a biochemical treatment unit;
(7) Performing biochemical treatment in the biochemical treatment unit, and precipitating, wherein the clear water after precipitation reaches the discharge standard; the specific steps of biochemical treatment are as follows: firstly, anaerobic biochemical reaction is carried out in a UASB reactor, and then two-stage A-O reaction is carried out.
2. The method for treating sinomenine hydrochloride production sewage according to claim 1, wherein the coagulant in the step (5) is polyaluminum chloride, polyferric sulfate or a mixture of the polyaluminum chloride and the polyferric sulfate.
3. The method for treating sinomenine hydrochloride production sewage according to claim 1, wherein the hydrolysis acidification unit in the step (6) is a hydrolysis acidification tank, and the hydrolysis acidification tank adopts polypropylene or polyamide three-dimensional elastic filler.
4. A method for treating sinomenine hydrochloride production sewage according to any one of claims 1-3, characterized in that the precipitated sludge produced in the step (5) and/or the step (7) enters a sludge tank for further precipitation, the supernatant after precipitation flows back to the water quality and water quantity regulating unit in the step (1), and the precipitated sludge is dehydrated by a lap screw dehydrator.
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