CN1029834C - Apparatus and process for treatment of wastewater - Google Patents
Apparatus and process for treatment of wastewater Download PDFInfo
- Publication number
- CN1029834C CN1029834C CN89102147A CN89102147A CN1029834C CN 1029834 C CN1029834 C CN 1029834C CN 89102147 A CN89102147 A CN 89102147A CN 89102147 A CN89102147 A CN 89102147A CN 1029834 C CN1029834 C CN 1029834C
- Authority
- CN
- China
- Prior art keywords
- effluent
- solution
- gas
- reactor
- waste water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 238000000034 method Methods 0.000 title claims abstract description 62
- 230000008569 process Effects 0.000 title claims abstract description 29
- 239000002351 wastewater Substances 0.000 title claims description 58
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 82
- 239000000203 mixture Substances 0.000 claims abstract description 43
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 20
- 150000007524 organic acids Chemical class 0.000 claims abstract description 20
- 239000007789 gas Substances 0.000 claims description 86
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical group C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 65
- 235000011089 carbon dioxide Nutrition 0.000 claims description 44
- 239000007788 liquid Substances 0.000 claims description 32
- 239000000243 solution Substances 0.000 claims description 31
- 239000002253 acid Substances 0.000 claims description 26
- 239000000463 material Substances 0.000 claims description 17
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 claims description 13
- 230000002378 acidificating effect Effects 0.000 claims description 12
- 239000003513 alkali Substances 0.000 claims description 8
- 150000001875 compounds Chemical class 0.000 claims description 8
- 230000004060 metabolic process Effects 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 239000011159 matrix material Substances 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 6
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 claims description 6
- 150000001720 carbohydrates Chemical class 0.000 claims description 5
- 238000000354 decomposition reaction Methods 0.000 claims description 5
- 239000007853 buffer solution Substances 0.000 claims description 4
- 230000015556 catabolic process Effects 0.000 claims description 4
- 230000014509 gene expression Effects 0.000 claims description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 3
- 238000006731 degradation reaction Methods 0.000 claims description 3
- 238000004065 wastewater treatment Methods 0.000 claims description 3
- 230000029087 digestion Effects 0.000 claims description 2
- 239000000284 extract Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 239000004215 Carbon black (E152) Substances 0.000 claims 2
- 229930195733 hydrocarbon Natural products 0.000 claims 2
- 150000002430 hydrocarbons Chemical class 0.000 claims 2
- 229920000642 polymer Polymers 0.000 claims 2
- 238000005273 aeration Methods 0.000 claims 1
- 230000007306 turnover Effects 0.000 claims 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 14
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 12
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 10
- 238000009776 industrial production Methods 0.000 description 10
- 239000000758 substrate Substances 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 230000008859 change Effects 0.000 description 8
- 239000002699 waste material Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 7
- 238000007667 floating Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 238000012545 processing Methods 0.000 description 7
- 238000005276 aerator Methods 0.000 description 6
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 description 6
- 239000000470 constituent Substances 0.000 description 5
- 239000000945 filler Substances 0.000 description 5
- 238000005507 spraying Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000001580 bacterial effect Effects 0.000 description 4
- 239000011324 bead Substances 0.000 description 4
- 235000014633 carbohydrates Nutrition 0.000 description 4
- 230000007935 neutral effect Effects 0.000 description 4
- 238000007789 sealing Methods 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 239000004575 stone Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000013022 venting Methods 0.000 description 4
- 241001112741 Bacillaceae Species 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 3
- 239000003518 caustics Substances 0.000 description 3
- QQVIHTHCMHWDBS-UHFFFAOYSA-N isophthalic acid Chemical compound OC(=O)C1=CC=CC(C(O)=O)=C1 QQVIHTHCMHWDBS-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000011368 organic material Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- MGMNPSAERQZUIM-UHFFFAOYSA-N 2-(hydroxymethyl)benzoic acid Chemical compound OCC1=CC=CC=C1C(O)=O MGMNPSAERQZUIM-UHFFFAOYSA-N 0.000 description 2
- XFEGRFIENDJTCK-UHFFFAOYSA-N 2-phenyl-2,3-dihydroindene-1,1-dicarboxylic acid Chemical compound C1C2=CC=CC=C2C(C(=O)O)(C(O)=O)C1C1=CC=CC=C1 XFEGRFIENDJTCK-UHFFFAOYSA-N 0.000 description 2
- GOUHYARYYWKXHS-UHFFFAOYSA-N 4-formylbenzoic acid Chemical compound OC(=O)C1=CC=C(C=O)C=C1 GOUHYARYYWKXHS-UHFFFAOYSA-N 0.000 description 2
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- VZCYOOQTPOCHFL-OWOJBTEDSA-N Fumaric acid Chemical compound OC(=O)\C=C\C(O)=O VZCYOOQTPOCHFL-OWOJBTEDSA-N 0.000 description 2
- 241000190932 Rhodopseudomonas Species 0.000 description 2
- UJMDYLWCYJJYMO-UHFFFAOYSA-N benzene-1,2,3-tricarboxylic acid Chemical compound OC(=O)C1=CC=CC(C(O)=O)=C1C(O)=O UJMDYLWCYJJYMO-UHFFFAOYSA-N 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- JFCQEDHGNNZCLN-UHFFFAOYSA-N glutaric acid Chemical compound OC(=O)CCCC(O)=O JFCQEDHGNNZCLN-UHFFFAOYSA-N 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 239000010815 organic waste Substances 0.000 description 2
- LPNBBFKOUUSUDB-UHFFFAOYSA-N p-toluic acid Chemical compound CC1=CC=C(C(O)=O)C=C1 LPNBBFKOUUSUDB-UHFFFAOYSA-N 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- ARCGXLSVLAOJQL-UHFFFAOYSA-N trimellitic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C(C(O)=O)=C1 ARCGXLSVLAOJQL-UHFFFAOYSA-N 0.000 description 2
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N valeric acid Chemical compound CCCCC(O)=O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 description 2
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 2
- RPAJSBKBKSSMLJ-DFWYDOINSA-N (2s)-2-aminopentanedioic acid;hydrochloride Chemical compound Cl.OC(=O)[C@@H](N)CCC(O)=O RPAJSBKBKSSMLJ-DFWYDOINSA-N 0.000 description 1
- RBNPOMFGQQGHHO-UHFFFAOYSA-N -2,3-Dihydroxypropanoic acid Natural products OCC(O)C(O)=O RBNPOMFGQQGHHO-UHFFFAOYSA-N 0.000 description 1
- QPGBFKDHRXJSIK-UHFFFAOYSA-N 2-tert-butylbenzene-1,3-dicarboxylic acid Chemical compound CC(C)(C)C1=C(C(O)=O)C=CC=C1C(O)=O QPGBFKDHRXJSIK-UHFFFAOYSA-N 0.000 description 1
- ALRHLSYJTWAHJZ-UHFFFAOYSA-N 3-hydroxypropionic acid Chemical compound OCCC(O)=O ALRHLSYJTWAHJZ-UHFFFAOYSA-N 0.000 description 1
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N Acrylic acid Chemical compound OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- 241000607534 Aeromonas Species 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- RBNPOMFGQQGHHO-UWTATZPHSA-N D-glyceric acid Chemical compound OC[C@@H](O)C(O)=O RBNPOMFGQQGHHO-UWTATZPHSA-N 0.000 description 1
- 241000605716 Desulfovibrio Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 241000186660 Lactobacillus Species 0.000 description 1
- 241000202974 Methanobacterium Species 0.000 description 1
- 241000736192 Ostrya virginiana Species 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 241000191940 Staphylococcus Species 0.000 description 1
- 241000191967 Staphylococcus aureus Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 229920001617 Vinyon Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003929 acidic solution Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 159000000032 aromatic acids Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000003637 basic solution Substances 0.000 description 1
- UHOVQNZJYSORNB-UHFFFAOYSA-N benzene Substances C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000000872 buffer Substances 0.000 description 1
- KDRIEERWEFJUSB-UHFFFAOYSA-N carbon dioxide;methane Chemical compound C.O=C=O KDRIEERWEFJUSB-UHFFFAOYSA-N 0.000 description 1
- SQXFNEDZVPHSPV-UHFFFAOYSA-N carbon dioxide;urea Chemical compound O=C=O.NC(N)=O SQXFNEDZVPHSPV-UHFFFAOYSA-N 0.000 description 1
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 230000001925 catabolic effect Effects 0.000 description 1
- 238000003486 chemical etching Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 239000001530 fumaric acid Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 239000003102 growth factor Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 229940039696 lactobacillus Drugs 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 206010025482 malaise Diseases 0.000 description 1
- VZCYOOQTPOCHFL-UPHRSURJSA-N maleic acid Chemical compound OC(=O)\C=C/C(O)=O VZCYOOQTPOCHFL-UPHRSURJSA-N 0.000 description 1
- 238000013178 mathematical model Methods 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000007269 microbial metabolism Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- ZWLPBLYKEWSWPD-UHFFFAOYSA-N o-toluic acid Chemical compound CC1=CC=CC=C1C(O)=O ZWLPBLYKEWSWPD-UHFFFAOYSA-N 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 1
- 238000009790 rate-determining step (RDS) Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- -1 t-butyl m-phthalic acid Chemical compound 0.000 description 1
- 238000012549 training Methods 0.000 description 1
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 229940005605 valeric acid Drugs 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 230000003442 weekly effect Effects 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Degasification And Air Bubble Elimination (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Physical Water Treatments (AREA)
Abstract
The present invention relates to a method and equipment for an anaerobic process, effluent which can dissolve carbon dioxide and come from an anaerobic reactor and fresh feed containing organic acid are combined, the carbon dioxide is extracted from the mixture to increase the pH value so that the alkaline consumption in a system is reduced, and the solution of the organic acid with limited solubility is promoted.
Description
The present invention relates to the processing of waste water or sewage,, remove aerobic impurity wherein so that before waste water stream drains into environment.More particularly, the organic constituent that the invention relates to the need alkali of minimizing in anaerobic treatment stream is metabolised to the method and apparatus of methane and carbonic acid gas.
Many industry produce acid waste liquid, and its organic constituent of this waste liquid is quite high, thereby need a large amount of oxygen to combine with waste water, so do not allow usually it is entered in lake or the rivers.ENVIRONMENTAL LAW and regulations of rules the content range of existing chemistry and aerobic material biology in the waste water before allowing to enter public waterway.
Removing a kind of method with aerobic material biology chemistry is by aerobic and anaerobism method, comes these materials of metabolic degradation with bacterium, and the present invention mainly is applicable to anaerobic process, is specially adapted to the acid waste water of limited solubility.
In the typical anaerobic filtration method, by an anaerobic reactor, the organic substrate in the microbial metabolism waste water in this reactor in the anaerobism medium also produces methane and carbonic acid gas to waste water by directly.Typical reactor is actually the container of a sealing, and it is suitable for accepting waste water stream.Reactor can comprise one deck packing material, and it can be stained with microorganism.Packing material can be annular material for example with holes arbitrarily or directed filler, or as is the stopping composition of trade mark sale with Vinyl Core and Koro-Z on the market.
In general, DESIGN OF REACTOR can be divided into two classes according to the flow performance that it comprises liquid.Common waste water enters and moves up from the bottom section of enclosed reaction vessel in upflow-type reactor.Methane and carbon dioxide also move along with liquid flows to go up, when gas arrives the surface, because the effect of pressure reduction and separation factor is a gas phase by liquid phase separation.Filterable liquid is taken away from the liquid level top.Container top has the gas skirt of the sealing of an essentially no liquid, so that collect gas.
In downflow reactor, waste water enters and moves down from reactor head usually, and methane and carbon dioxide move up against liquid stream.Yet liquid moves down, constantly increases because of the degree of depth increases pressure, soluble gas is retained in forms acidic buffer solution in the liquid.Equally, the container top gas skirt that does not have liquid basically that is provided with an envelope group is used for collecting gas.
In up-flow and downflow system system, the liquid stream person who leaves anaerobic reactor enters settling tank through a degasser.And methane gas is recovered as a kind of energy.The mud that produces in treating processes sinks at the bottom of the settling tank, can be repeated circulation, also can be for further processing, so that last the disposal.
Anaerobic process will produce carbonic acid gas when under normal circumstances, reactor moves.The carbonic acid gas that is produced by anaerobic reaction forms a dividing potential drop, carbonic acid gas is dissolved in the water-bearing media and formation carbonic acid.Carbonic acid that forms and the acetic acid that forms in carbohydrate waste water can make the pH value in the reactor descend, and will add caustic soda this moment to keep reactor in the pH of normal running value 6.8 or bigger pH value.In high-concentration waste water,, cause constant demand to caustic soda owing to lack shock absorption.The caustic soda that adds is the factor that makes the anaerobic process process cost the most expensive.
The design of downflow reactor also may form sour environment in reactor.The continuous metabolism of organic materials may form the pH gradient in container.The zone of orientating reaction device bottom has been stopped the variety of way that carbonic acid gas releases, thereby has been had higher carbonate concentration under the effect of the pressure that liquid depth produces.
When the waste water of input itself was acidity, the problem that forms acid in reactor was just even more serious.In fact, other organic waste that all may produce organic acid in several industrial production and be suspended in the limited solubility on the waste water stream are arranged.Below be as above-mentioned industrial nonrestrictive example: a kind of waste material that produces when production is used for the terephthalic acid of plastics industry just includes acetic acid, phenylformic acid, terephthalic acid, m-phthalic acid, phthalic acid, P-toluic acid 1,2,4-benzenetricarboxylic acid, 4-carboxyl benzaldehyde and hydroxymethyl-benzoic acid.In these aromatic acids, some may be present in the waste liquid with the concentration greater than its solubleness.When this situation occurring, aromatic acid makes waste liquid become acid charging, thereby must be with its neutralization before decomposition.When aromatic acid enters the reactor of low pH value, may from solution, be precipitated out, reduce the effect of the organic constituents of anaerobic process in metabolism waste water stream.
Reactor bottom zone with carbonic acid of high density is the potential substantially source of getting rid of carbonic acid.Thereby, if the sewage in the reactor is cushioned roughly neutral pH value, then get rid of the basic solution that generation be can be used for making behind carbonic acid or the carbonic acid gas acid charging neutralisation.
In addition, the original feed of coming out in many industrial production since the restriction of temperature be unwell to biolytic.In typical production process, stable pond or the groove to provide charging anaerobic process to use in the settling pond is provided the charging in the industrial production.To reach envrionment temperature substantially in order making, the aerating apparatus that comprises atomizer or sinking baffle plate also to be housed in the settling pond by the high temperature original feed of coming in the industrial production.
The control of temperature in the anaerobic process and pH value needs high-energy and big expense.It seems that some up-flow reactors be the solution that recycling processing is crossed from reactor, and remove to cushion the waste water stream of input with these solution with cardinal principle neutral pH value.See the people's such as training profit that on February 4th, 1986 issued No. 4568464 United States Patent (USP)s; The Wei top grade people's that on January 26th, 1977 announced No. 19176/75 UK Patent Application: and the article of on May 23rd, 1979 chemical 42 phases of weekly " anaerobic filter reduces expense, produces energy ".
It seems that some downflow reactor systems be to use a kind of recirculation system to improve the uniform distribution of the liquid of whole reactor.This people's such as grade of Berne base that issue January 19 nineteen eighty-two No. 4311593 United States Patent (USP)s.
Sieve husband's No. 4530767 United States Patent (USP)s have been described the method that the gas skirt gas from the up-flow reactor operating process that utilizes reactor is carried carbonic acid gas.
No. 3981800 of Otto and No. 3939066 United States Patent (USP)s of Bauer have been described the method for utilizing pressure discharging separating carbon dioxide from anaerobic process.
No. 3980556 United States Patent (USP)s of Pei Xike have been described the method that from the active sediment stripping nitrogen and twice-laid stuff recirculation are gone into reactor.
No. 4375412 United States Patent (USP)s of Shi Kaimaier have been described the method that reclaims nitrogen under the vacuum action.
Yet above-mentioned data does not all propose by control pH value and controlled temperature the acidic waste of limited solubility to be carried out the method and apparatus of anaerobic treatment.
The invention is characterized in a kind of acid concentration that is used to reduce and controls the industrial liquid stream of anaerobic, improve the method and the equipment thereof of the feeding temperature of the solvability of acidic components of limited solubility and control input reactor.
A kind of embodiment of the present invention comprises an anaerobic treatment method.This method may further comprise the steps, and under anaerobic decomposes the matrix in the anaerobism medium.The anaerobic metabolism effect produces a kind of gaseous compound that can be dissolved in the medium in this process, thereby forms a kind of acidic buffer solution.Contact with a kind of substantial rare gas element with recovery above-mentioned gas compound to major general part acidic buffer.This solution is to comprising that the further processing of introducing reactor again is useful.
Preferably this solution is comprised the matrix phase combination of input to form a kind of charging mixed solution with a part at least.The organic acid that comprises limited solubility in matrix is removed gaseous compound wherein, will improve the organic acid solvability.
When the gaseous constituent that produces acidic conditions in the anaerobic reactor comprised carbonic acid gas, then a part of acidic solution can be summarized with following system of equations with the contacted chemical process of a kind of substantial rare gas element, and equation is with S
1And S
2Expression
Like this, by stripping, reduced the hydrogen ion concentration of solution to the acid solution of carbonic acid gas.
Hydrogen ion concentration is also relevant with the organic acid solubleness that is included in the waste water stream in many industrial production.Solid organic acid enters the equation of solution can be with following with D
1, D
2And D
3One prescription formula of expression is summarized:
In the superincumbent equation, OA represents a kind of organic acid, may comprise following: aromatic acid as nonrestrictive example, such as phenylformic acid, toluic acid, terephthalic acid, m-phthalic acid, phthalic acid, benzenetricarboxylic acid, 1,2,4,5-pyromellitic acid, 4-carboxyl benzaldehyde, hydroxymethyl-benzoic acid, t-butyl m-phthalic acid and phenyl indane dicarboxylic acid.
Equation S
1Be the function of pH, its balance is considered to be actually instantaneous foundation.Equation S
2Comprise a phase change process, and be considered to rate-controlling.With this understanding, can from acid solution, discharge carbon dioxide for one, can control with carbonic acid for one and form relevant hydrionic concentration.
The second prescription formula relates to the dissolving function, also relates to the pH value.Equation D
2And D
3Be the function of pH, its balance is considered to be actually instantaneous foundation.Equation D
1Comprising a phase change process and with to be considered in dissolution process be rate-controlling, is that the feature by particle limits basically.Provide yet basic starting force is the pH value by solution, this pH value can go out carbon dioxide by stripping from the acidic mixture that comprises solid organic acid and change.
A kind of embodiment of the present invention comprises usefulness methane as substantial rare gas element, so comprise the effluent with organic substrate mixture and reactor among the embodiment, contacts with methane in the environment of sealing basically.First-selection will be removed carbonic acid gas in the methane that produce in the anaerobic process, and the mixture with organic substrate and reactor effluent contacts then.The carbonic acid gas distribution enters in the methane gas, and methane and carbon dioxide are useful to further processing.
A kind of embodiment of the present invention, its characteristics are to be convenient to remove carbonic acid gas from the mixture of organic substrate and reactor effluent.The characteristic of this embodiment is that the reactor effluent that will be rich in carbonic acid gas contacts with the time material of sending here in the industrial production that is higher than envrionment temperature.This high temperature helps removing carbonic acid gas, and it is evaporated from mixture.
The synthermal higher charging of the sewage that temperature is lower mixes the mixture that forms a kind of medium temperature mutually.This mixture contacted with substantial rare gas element further reduce its temperature.In a tightness system, can include the methane that obtains as the reaction product in the anaerobic process in the gas.Yet, be not that all application all must have a closed system.
An embodiment of the present invention, its treating processes are the temperature that may command flows into the charging of anaerobic reactor.This embodiment includes such step, and it can adopt suitable mode that the mixture of organic substrate and reactor effluent is contacted with a kind of substantial rare gas element.These modes comprise mixture are atomized in air, mixture is flow through a series ofly be arranged on airborne baffle plate, and in mixture the air-blowing bubble.Control the temperature of mixture with the quantity that increases or the minimizing rare gas element contacts with mixture.
Be used for the gas of charging of separating carbon dioxide or cooling heat, preferably such gas, it does not disturb anaerobic process or can be separated basically, maybe can remove from anaerobic process, it is not easy to enter solution, or makes the biological degradation reduction of matrix in some way with substrate reaction.The preferred gas that adopts comprises methane and atmosphere.
A kind of embodiment of the present invention, it comprises separating carbon dioxide from methane-carbon dioxide mixture that anaerobic reactor discharges, and is used as a kind of substantial rare gas element to produce a certain amount of methane.At first, remove carbonic acid gas, methane is separated with carbon dioxide, for example have under the situation of water by pressure change with method well known in the art, or adding caustic alkali; Then methane is contacted to remove carbonic acid gas with waste water.Methane-carbon dioxide mixture is to comprising the recirculation separating carbon dioxide or all being useful as a kind of further processing of the energy.
The characteristics of embodiments of the invention also are its equipment, and this equipment can reduce and control the acid concentration of anaerobic process liquid stream, improve the solvability and the control input temperature of charge of the acid constituents with limited solubility.
A kind of embodiment of the present invention, its characteristics are its equipment, and this equipment has a system that is suitable for decomposing the anaerobic reactor of organic substrate in treating processes, and this reactor can produce the gaseous compound that is dissolvable in water liquid.Anaerobic reactor also comprises receiving trap, wherein contains the pipeline of organic substrate being introduced reactor.This reactor also comprises discharge equipment, and it contains the pipeline that gives off waste water from reactor.This system also includes the stripping that communicates with a receiving trap and described discharge equipment-dissolving tower.This stripping dissolving tower is suitable for waste water and the reactor effluent accepting to import, and effluent is contacted with a kind of substantial rare gas element, and making, the dissolved gases mixture can be dispensed into substantial rare gas element.Stripping-dissolving the tower that communicates with the reactor receiving trap is suitable for the mixture of charging and effluent is drained into reactor.
The operation pH value that the characteristics of embodiments of the invention are to keep when its method and apparatus can reduce the alkali consumption anaerobic process liquid stream normally.The consumption of alkali can reduce 40-60%, and carbonic acid gas reduces to 20% from about 30% in escaping gas, and the performance of anaerobic process is unaffected.
The characteristics of embodiments of the invention are to be specially adapted to downflow reactor.This reactor is because the energy of flow accumulation of pressure effect and solution or raising carbonic acid gas-carbonic acid gradient.According to the present invention, from a part of reactor effluent of reactor bottom by a minute inflow stripping-dissolving tower.Because carbonic acid gas concentrates in this strand effluent, just less with the carbonic acid gas that methane is discharged together, this just makes methane more valuable as a kind of energy.
Its characteristics of a kind of embodiment of the present invention are that stripping-dissolving tower includes a sealed vessel, and this container has a receiving trap, accept the effluent from anaerobic reactor.This container also includes discharge equipment and is used for the effluent of discharging container.This container also has the gas receiving trap, the substantial rare gas element in the receiving vessel.Final container also includes with gas receiving trap and or the Liqiud-gas mixing device that communicates of effluent receiving device.Following as a kind of non-limiting example of the present invention, this embodiment can include the spraying gun, the aerating system that communicate with the effluent receiving device, a plurality of venting ports that this system includes a gas blower and communicates with the gas receiving trap, a gas stone or a gas charging stone (gas stone) that communicates with the gas receiving trap, gas stone wherein is to be immersed in the waste water and to be contained in the container, a series of baffle plates that communicate with the effluent receiving device, it has increased sewage with the degree that is in contact with one another that enters the gas of container, or other combination of said system.
An illustrated embodiments, wherein include a stripping-dissolving tower, this stripping-dissolving tower has the charging receiving device, and this device includes pipeline, it is suitable for charging is mixed with effluent, so that improve the solvability of matrix when removing carbonic acid gas from effluent.
An illustrated embodiments of the present invention also includes a reactor and a stripping-dissolving tower, and reactor wherein comprises the device that receives methane.And stripping-dissolving tower also includes the device of the reception methane that communicates with the gas receiving trap, and this device is used for separating carbonic acid gas from reactor effluent.
Its characteristics of embodiments of the invention are to be suitable for controlling the temperature of the waste water stream that enters reactor and to be convenient to remove carbonic acid gas.So effluent joined to separating with the charging that comparatively high temps arranged carbonic acid gas is separated from effluent, and the temperature of having regulated mixture.In addition, input expects that closely contacting the cooling that makes mixture with the mixture of waste water with substantial rare gas element can finish substantially.The cooling of said mixture can be regulated by the exposure level that changes between gas and liquid.Below be as nonrestrictive example: can strengthen cooling by the air-flow that increases by stripping-dissolving tower.
Characteristics of the present invention are to be specially adapted to have in the lower zone of reactor the downflow reactor of high carbonic acid gas-carbonate concentration.In addition, downflow reactor helps to remove the carbonic acid gas in the effluent, and the result can be more suitable for as a kind of energy the methane that produces in the anaerobic process.The characteristics of embodiments of the invention are to adopt open system, separating carbon dioxide from effluent, thereby also have the characteristics of vaporization function, it will reduce the flow that waste water flows.
The characteristics of these and other will become very clear by accompanying drawing and going through of following.Accompanying drawing and discussion, the most preferred embodiment of the present invention that they are described proposes as an example, is not to be limitation of the present invention.
Consult Fig. 1 now, it with the formal specification of schematic diagram anaerobism Waste Water Treatment and with 11 these systems of expression.Anaerobism Waste Water Treatment 11 is made up of anaerobic reactor 13 and stripping-15 two major partss of dissolving tower.
Anaerobic reactor 13 is accepted the waste water feeding of stripping-dissolving tower 15 by pipeline 31.These waste water may comprise such as carboxylic acid, xitix, acetic acid, propionic acid, vinylformic acid, oxyacetic acid, toxilic acid, hexanodioic acid, phenylformic acid, butyric acid, valeric acid, hydroxy-propionic acid, R-Glyceric acid, succsinic acid, fumaric acid, pentanedioic acid, phthalic acid, m-phthalic acid, terephthalic acid, t-butyl iso-phthalic acid, 1,2,4,5, organic acids such as-benzene tertacarbonic acid, phenyl indane dicarboxylic acid; And comprise other organic alcohol, ketone, ester, aldehyde and phenol.The organic acid that enters reactor may have limited solubleness.
Be subjected to the metabolism of bacterial flora after these acid organic substrates are accepted by reactor there, these bacteriums comprise Bacillaceae, green dense Rhodopseudomonas, the plain Rhodopseudomonas of chlorine, starch liquefacation Bacillaceae, various staphylococcus kind, Desulfovibrio, air balls bacterial classification genus, Aeromonas kind, streptococcus aureus, cud lactobacillus genus, formic acid Methanobacterium and free methane Bacillaceae.
During organic materials decomposed in reactor, bacterial flora association produced methane and carbonic acid gas.These carbonic acid gas can generate carbonic acid with the water reaction.
Reactor 13 is the containers of sealing basically, and it comprises 33, one diapires 35 of vertical wall and a floating top cover collector 37 of one garden tubular.
Floating top cover collector 37 is parts of gas gathering system 38.The shape of floating top cover collector 37 is rescinded angle tapers, has radially towards the surface 39 that has a down dip.The external diameter edge-perpendicular of floating top cover collector 37 is extended, and forms the vertical bead 41 of a circle, it and inner garden tubular wall 33 sealed engagement.Vertical bead 41 is located in the cantilever bead 43 of the operation that cooperatively interacts, cantilever bead 43 from garden synform wall 33 radial to projecting inward.
The methane gas that produces during the anaerobic digestion organic materials in reactor passes the aqueous solution in the container and floats up and be collected in the vacuum area that is limited by floating top cover gas trap 37.Floating top cover gas trap 37 is by moving the volume that can change it up along cylinder wall 33, to hold the additional volume of methane gas.
Methane gas in floating top cover gas trap 37 communicates with compressor 47 by pipeline 49 and control valve 51.And these are exactly all parts of gas gathering system 38.In a single day system 38 comprises a control valve 51 that communicates with safe head light 53 by pipeline 55, in order to the usefulness that must discharge methane gas from gas gathering system 38.Safety flare 53 can fall unnecessary methyl hydride combustion.
There is one deck stopping composition 45 inside of anaerobic reactor 13, and it has huge surface-area to be used for adhering to and grow for bacterial flora.These media can be directed arbitrarily materials, such as rock and annular material with holes, also can be directional materials, such as the bundle or the piece that with Vinyl Core and Koro-Z are the vinyon of trade mark sale.Stopping composition 45 is bearing on the reactor frame 59, is used for collecting the effluent of purifying substantially so that a space 61 to be provided.
Waste water enters reactor 13 by waste water collection device, and collection device comprises reactor water inlet pipe 31 and distributed network 65, and distributed network can make the waste water of input be evenly distributed on the upper surface of filler 45 substantially.Like this, the waste water of input is introduced into the top of filler 45, flow through filler 45 and give the chance that the organic substrate that has in a metabolism and the water of decomposition solution is provided attached to the anaerobic bacterium on the filler 45 down, waste water continues to flow downward, enter area of space 61 by reactor 13, and from reactor, discharge by the wastewater discharge device that comprises reactor effluent pipeline 69.
Part reactor effluent reaches interface 71 and is divided into two-way by interface by pipeline 69 outflow reactors.One route pipeline 73 is represented the further treatment steps of guiding or is discharged in the general environment.Following as non-limitative example: pipeline 73 may lead to an aerobic biooxidation (biox) system, to finish the decomposition of organic waste materials.The aerobic biooxidation system may comprise that also employing mud storage pool or similar fashion are to carry out the step of further purifying treatment.
Second passage by pipeline 75 expressions is introduced stripping-dissolving tower 15 with the part of reactor effluent.The reactor effluent of being carried by pipeline 75 is rich in carbonic acid gas.
In general, the decomposition of aromatic acid can not make the pH value in the reactor significantly reduce than the value of charging, because aromatic acid has disappeared when forming carbonic acid.In aromatic acid decomposed, rate-limiting step was in initial stage chemical etching ring structure.Do not have other acid intermediate product this moment or pay product and form significantly.
On the contrary, the breakdown of carbohydrates that the suctions waste water pH value that may induce reaction in the device is lower than the value of charging.Why processed waste water has than high acid concentration has several factors.The carbohydrate waste material is neutral basically, and its complete metabolism causes the generation that forms the acidic substance carbonic acid gas.And carbohydrate is very fast in initial catabolic phase process, forms the slower intermediate material of metabolism.These intermediate materials may comprise that acidic cpd is such as acetic acid.
Stripping-dissolving tower 15 utilizes the neutralizing agent of the effluent of reactor 13 as acidic waste, and the effluent of reactor is to be approximately 7 with its pH value that carbonic acid cushioned.In one embodiment, a part of effluent of reactor 13 is directly to introduce stripping-dissolving tower 15.Stripping-dissolving tower 15 is suitable for accepting effluent and these effluents is contacted with substantial rare gas element.
As shown in the figure, stripping-dissolving tower 15 comprises a container 83, and it is suitable for accepting liquid, comprises the effluent of acceptable response device 13.Make effluent comprise spraying gun 85, aerator 87 and a series of stepwise baffle plate (not shown) with the contacted device of rare gas element.
Spraying gun 85 communicates with reactor 13 by pipeline 75 and 69.Spraying gun 85 is suitable for accepting liquid and liquid is sowed in the rare gas element in the container 83.
Aerator 87 is suitable for accepting a kind of substantial rare gas element and they is blown broadcasting in the liquid, and it comprises the reactor effluent that holds in the container 83.Aerator 87 communicates with gas blower 89 by conduit 91.
Gas blower 89 can extract atmosphere, yet it can help to give aerator 87 transport methane through the conduit (not shown) that communicates with gas gathering system 38 in closed system.Methane is being used as under the situation of rare gas element, and aerator 87 preferably communicates with compressor 47 and urea carbon dioxide stripper (not shown).Carbonic acid gas can adopt the whole bag of tricks to separate from methane or other gas, comprise with mode well known in the art in water to gaseous mixture pressurization or add a kind of basic additive.
Stripping-dissolving tower 15 also comprises the device of emission gases from the container 83 that includes venting port 93.Venting port 93 opens wide to atmosphere as shown in the figure in an open system.In a closed system, venting port 93 communicates with reactor methane collection system 38 by closing the device that contains the pipeline (not shown) that moves.
Effluent contacts gradually with substantial rare gas element in stripping-dissolving tower 15.Incidental carbon dioxide separation becomes gas phase in the effluent, has improved the pH value of the liquid that stays.The liquid that stays can emit from stripping dissolving tower 15 through a delivery pipe, for further processing, comprises it is sent back in the reactor 13.
One embodiment of the present of invention comprise a stripping-dissolving tower 15 that is suitable for accepting fresh feed next from industrial production.As shown in the figure, the pipeline 75 that connects stripping-dissolving tower 15 comprises an interface 97, is used for accepting the fresh feed of sending here from the industrial production of input channel 99.Input channel 99 can directly communicate with industrial production, also can accept the waste water that comes from storage pool.For ease of new charging and reactor effluent are mixed, pipeline 75 comprises a line mixer 101.
The mixture of charging and effluent is accepted by stripping-dissolving tower 15, and isolates carbonic acid gas in the mixture by it, to improve the pH value of mixture.Under the situation of the aromatic acid that contains limited solubility in the mixture, the pH value that improves mixture will force solid to become solution.
Those skilled in the art that will recognize that the mixing of charging and effluent can be before removing carbonic acid gas, also can be after removing carbonic acid gas.Yet,, before removing carbonic acid gas, charging and effluent mixing are convenient to carry out stripping by distillating carbonic acid gas if the temperature of charging is higher than effluent.
For instance, pH value by the input waste water that comes in the Production of Terephthalic Acid commercial run may be 4.0 to 4.5, the pH value of reactor effluent may be about 7, and the pH value from stripping-dissolving tower 15 to the output mixture of reactor 13 is 6.0 to 7.5, in neutral scope basically.
Suppose that reactor 13 is an equilibrated with gas-liquid in stripping-dissolving tower mutually, can set up the mathematical model of stripping-dissolving tower so, wherein:
When using above-mentioned formula, the project definition in the formula is as follows:
A. be the acid equivalent concentration of input waste water;
B. be base-material in reactor 13 with respect to the ratio of the acid of input in the waste water, B also can be expressed as the ratio of acid concentration in Na ion concentration in the reactor 13 and the input waste water;
E. be the percentage of carbonic acid gas that produce and that in stripping-dissolving tower 15, be separated in the reactor 13;
Hr. be the hydrogen ion concentration in the reactor 13;
Hs. be hydrogen ion concentration in stripping-dissolving tower 15;
Ka. be input acid balance constant;
Kc. be the carbonate equilibrium constant;
Kh. be the henry's law constant of carbonic acid gas;
N. be the mole number that per minute is separated the carbonic acid gas of monovalent acid generation;
P. be the carbon dioxide balance dividing potential drop of gas in stripping-dissolving tower 15;
X. be acid conversion percentage in the reactor 13;
Z. be the stripping-effluent of dissolving tower 15 and the ratio of charging.
Fig. 2 has illustrated to reaching the operational condition that different carbon dioxide separation rates needs.The relation of Z and P is by different E value representations.Z is the stripping-effluent of dissolving tower 15 and the ratio of charging; P is the carbon dioxide balance dividing potential drop of gas in stripping-dissolving tower 15, and E is the percentage of carbonic acid gas generation and that discharge in stripping-dissolving tower 15.Relation illustrated in fig. 2 is to be 1 * 10 to have Ka
-4.76Acetic acid be the basis as the waste water of main component.In Fig. 2, A is set to 0.08 equivalent concentration, and B is 0.1277, and Hr is 1 * 10
-7, Kc is 1 * 10
-6.46, Kh is 10
-1.57M/ATM, n are 1.66, X be 0.85 and Hr be 1 * 10
-7M.
The value of Fig. 2 mid point is represented specific Z and the E value pH value in the stripping tower down.Curve under the various E values tends to by maximum value, and recirculation ratio point Z that this place points out and partial pressure of carbon dioxide P are stripping-the most effective working points of dissolving tower.The loss of methane shows under high E value, and the lower E value between 0.25-0.5 is useful.Like this, best repeat cycle rate is between 1-6, and is best between 1.5 to 4.
Carbonic acid gas in a part of effluent that purge reactor comes, and it is mixed with fresh feed, the demand 20%-40% of alkali can be reduced.
The characteristics of embodiments of the invention are to control the temperature of the mixture of charging one effluent.For instance, making the wastewater temperature that comes in the industrial production of terephthalic acid may be between 130 °-140 °F, and the wastewater temperature that enters reactor 13 is gratifying about 100 °F.
Effluent and fresh feed mixed cause temperature to reduce, the further reduction of temperature is that liquid contacts with rare gas element in stripping-dissolving tower 15 and causes.In fact, when needs reduce the temperature of mixture of charging and effluent, can atmosphere be blown in stripping-dissolving tower 15 by aerator 87.The temperature of control in stripping-dissolving tower 15 and other apparatus and method step comprise spraying gun and at the storage pool of reactor 13 upstreams.
The most preferred embodiment of stripping in open system-dissolving tower 15, the general cooling tower that is suitable for accepting effluent and incoming mixture that adopts.But best cooling tower is the Ba Er hophornbeam likes T1000 type the 5th serial cooling tower that youngster (Baltimore Aircool) produces.
One embodiment of the present of invention, its characteristics are to allow requiring can to add nutrient substance and caustic alkali reagent to pH value replenishment control with for the microorganism of reactor 13 provides suitable growth factor.Nutrient substance and caustic alkali reagent can add by the pipeline 100 and 102 that same stripping-dissolving tower discharge tube 31 communicates respectively.
Steam-pipe 105 carries out heat exchange with stripping-dissolving tower delivery pipe 31, is suitable for pipeline 31 heating, and this contact further provides the thermal control to the material of input reactor 13.
The characteristics of illustrated embodiments of the present invention are to be equipped with the transmitter of valve and pH value, temperature, flow, material and tank fill level, monitor and control this system in mode well-known in the art.
Most preferred embodiment of the present invention also comprises pump and gas booster compressor, drives liquids and gases in mode well-known in the art.
Like this, illustrated and described illustrated embodiments, yet be appreciated that the present invention can change and change, so the present invention should not be subjected to the restriction of the details narrated in the above, and should comprise that all belong to variation and change in the following claim scope.
Claims (16)
1, a kind of method of anaerobic treatment of waste water the steps include:
A. under anaerobic, decompose roughly a kind of matrix in the mobile anaerobism medium down in a downflow reactor, wherein the anaerobic metabolism effect produces and a kind ofly can be dissolved in the gaseous compound that forms a kind of acidic buffer solution in the described medium;
B. the described liquid of a part that low collecting zone extracts to the described reactor of major general contacts with a kind of substantial rare gas element, isolates described gaseous compound, so that described solution reduces acidity; And
C. described solution is imported described anaerobism medium to reduce the demand of alkali.
2, according to the method described in the claim 1, wherein said solution combines with a kind of charging that contains organic acid matrix, forms a kind of solution feed mixture before described solution being imported described anaerobism medium, to improve described organic acid solvability.
3, according to the method described in the claim 1, wherein said gaseous compound is to be dissolved in the described solution and with water to react the carbonic acid gas that forms carbonic acid.
4, according to the method described in the claim 1, wherein said substantial rare gas element is a methane.
5, according to the method described in the claim 1, wherein said substantial rare gas element is an air.
6, according to the method described in the claim 1, wherein said solution is atomised in the zone of containing described rare gas element.
7, according to the method described in the claim 1, wherein said solution is with described rare gas element aeration.
8, according to the method described in the claim 1, wherein said solution contacts with described rare gas element by expanding its surface-area, and makes described solution stream cross one or more baffle plate, is exposed in the described rare gas element.
9, according to the method described in the claim 2, the temperature of wherein said charging is higher than the temperature of described solution, with described solution with before a substantial inert atmosphere contacts, described charging is mixed with solution to form the mixture of a kind of solution and charging.
10, according to the method described in the claim 9, the time that the mixture of wherein said solution and charging keeps in touch is by the temperature decision of described mixture.
11, according to the method described in the claim 10, the wherein said time is decided by that the temperature with described mixture is cooled to be roughly 100 time.
12, according to the method described in the claim 1, wherein said part solution is from the lower position of downflow reactor.
13, according to claim 2 contain the organic acid wastewater treatment method, this method comprises the steps:
(a) waste water is sent in the anaerobic reactor,, produced gas that comprises carbonic acid gas and the effluent that comprises carbonic acid with the organic acid of anaerobism method decomposition in the anaerobism medium;
(b) a part of at least effluent is mixed with original waste water;
(c) mixture with effluent and original waste water mixes with the gas in stripping effluent and the original waste water in stripping-dissolving tower with substantial rare gas element, and it is dissolved in the solution; And
(d) stripping mixture of effluent and original waste water is sent into be used for anaerobic degradation organic acid anaerobic reactor, wherein effluent and the ratio of sending into the original waste water of stripping-dissolving tower remain:
Wherein
B is the ratio of the acid of base-material in the anaerobism medium and original waste water charging;
Hr is the hydrogen ion concentration of anaerobic reactor;
Hs is a hydrogen ion concentration in stripping-dissolving tower;
Ka is the organic acid equilibrium constant;
Ke is the carbonate equilibrium constant;
N is the mole number that per minute is separated the carbonic acid gas of monovalent acid generation;
X is the sour turnover ratio of anaerobism medium;
E is the percentage of the gaseous compound that produces in the anaerobism medium, and its recovery is represented as following relational expression:
Wherein the definition of B, Hr, Hs, Ka, Kc, n and x is the same;
Kh is the henry 's law constant of carbonic acid gas;
A is the acid equivalent concentration of the original waste water of input;
Z is the ratio of the original waste water of effluent and input; And
Carbon dioxide balance dividing potential drop (p) in the gas of the mixture of effluent and original waste water charging is to be represented by the following relationship formula:
Wherein the definition of A, B, E, Hr, Hs, Kc, Kh, n, x and Z is the same.
14, the method that contains organic acid and/or hydrocarbon polymer of claim 2, this method may further comprise the steps:
(a) waste water is imported in the anaerobic reactor, and in anaerobic reactor, decomposed organic acid and/or hydrocarbon polymer, produce gas and effluent with anaerobic process;
(b) at least a portion effluent and substantial rare gas element are mixed, carry the gas that is dissolved in liquid in the effluent with gas;
(c) effluent carried of gas mixes with raw wastewater; And
(d) mixture of the effluent carried of gas and raw wastewater input anaerobic reactor carries out anaerobic digestion organic acid and/or carbohydrate.
15, according to the method described in the claim 13, wherein acidic buffer solution is about 1 to 6 to the ratio of charging.
16, according to the method described in the claim 15, wherein said ratio is between 1.5 and 4.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89102147A CN1029834C (en) | 1989-03-04 | 1989-03-04 | Apparatus and process for treatment of wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89102147A CN1029834C (en) | 1989-03-04 | 1989-03-04 | Apparatus and process for treatment of wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1045381A CN1045381A (en) | 1990-09-19 |
| CN1029834C true CN1029834C (en) | 1995-09-27 |
Family
ID=4854554
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89102147A Expired - Fee Related CN1029834C (en) | 1989-03-04 | 1989-03-04 | Apparatus and process for treatment of wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1029834C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BR9815459A (en) * | 1997-03-14 | 2001-10-16 | Du Pont | Process for the treatment of an effluent stream, process for the production of an aromatic carboxylic acid and plant for the production of an aromatic carboxylic acid |
| CN103693831B (en) * | 2013-12-13 | 2016-05-11 | 灵璧县林汇家禽育种有限责任公司 | For the treatment of the comprehensive utilization of resources system of fowl and animal excrement |
-
1989
- 1989-03-04 CN CN89102147A patent/CN1029834C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1045381A (en) | 1990-09-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1032527C (en) | Method of treating waste water and equipment therefor | |
| CN1198764C (en) | Method for removing sulfur compounds from wastewater | |
| US4231863A (en) | Method and apparatus for treating water | |
| CN1077551C (en) | Method and equipment for treating concentrated sewage | |
| CN104350012A (en) | Internal-circulation aeration anammox-membrane bioreactor | |
| US5419833A (en) | Apparatus for treatment of wastewater | |
| KR20120005857A (en) | Water treatment device and method | |
| CN108314255A (en) | A kind of efficient Chinese herbal medicine extraction sewage treatment process | |
| US7531087B2 (en) | System for treating wastewater | |
| CN101391853A (en) | Chemical wastewater recovery processing technique and apparatus | |
| CN101481197A (en) | Advanced treatment process and apparatus for oilfield heavy crude recovery sewerage | |
| CN208776514U (en) | Horizontal domestic sewage processing system | |
| CN109937191A (en) | Method and apparatus for handling the output water from oil field and gas field | |
| CN209974409U (en) | Anaerobic reactor for landfill leachate treatment | |
| CN1029834C (en) | Apparatus and process for treatment of wastewater | |
| CN110066076A (en) | A kind of deep denitrogenation process of low concentration total nitrogen waste water | |
| CN103043860A (en) | Leachate utilizing equipment and method in biomass landfilling process | |
| CN219620971U (en) | Device for purifying tail water of aquaculture | |
| CN220056517U (en) | Aerobic microorganism suspension filter tank purifying device | |
| CN206828316U (en) | A kind of cleaning system of marine alga processing sewage | |
| CN113800630A (en) | Anaerobic expansion bed device for treating high-concentration organic wastewater | |
| CN112225315A (en) | Packing fluidization dispersion type sewage treatment device | |
| CN210393863U (en) | Aquaculture wastewater ozone treatment equipment | |
| JP3706574B2 (en) | Waste water denitrification treatment method and treatment equipment | |
| CN2530947Y (en) | Internal recycling particle sludge bed nitrofication reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C15 | Extension of patent right duration from 15 to 20 years for appl. with date before 31.12.1992 and still valid on 11.12.2001 (patent law change 1993) | ||
| OR01 | Other related matters | ||
| C56 | Change in the name or address of the patentee |
Owner name: BP AMOCO CORP. Free format text: FORMER NAME OR ADDRESS: AMOCO CORP. Owner name: BRITISH PETROLEUM NORTH AMERICA LTD. Free format text: FORMER NAME OR ADDRESS: BP AMOCO CORP. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: Illinois State Patentee after: AMOCO Corp. Address before: Illinois State Patentee before: BP AMOCO Corp. Address after: Illinois State Patentee after: BP AMOCO Corp. Address before: Illinois State Patentee before: Amoco Corp. |
|
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |